TW200535232A - 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 25 DEG 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

200535232 IX. Description of the invention: [Technical field to which the invention belongs] The present invention generally relates to a system for processing a crude oil feed and to a composition made by, for example, materials and methods. Μ = of the specific examples described herein It is about the content of residue is: per: two: feed at least 0.2 grams of residual crude oil feed into tritium at 25. gram original: MPa is a liquid mixture, and (b) have-or more properties compared to the The same property of the original J feed is an improved system and method of crude oil products' ... [Previous Technology] Crude oil with-or more inappropriate properties that cannot allow crude oil to be economically transported or processed using traditional facilities, is commonly referred to as Disadvantaged crudes "~ Disadvantaged crudes often contain relatively high levels of residue. Such crude oils are often difficult and expensive to transport and / or process using traditional facilities. High-residue crude oil can be converted to coke after high temperature treatment. Or, high: two = Youtong ¥ 疋 treated with water at still temperature to produce a less viscous crude oil and / or crude oil mixture. During processing, it may be difficult to remove water from the less viscous crude oil and / or crude oil mixture using conventional means. Inferior crude oils may contain hydrogen deficient hydrogens. When processing hydrogen-lean hydrocarbons, it is often necessary to add a consistent amount of hydrogen, especially if unsaturated fragments due to the cracking process are produced. Hydrogenation during processing usually involves the use of active hydrogenation catalysts, possibly inhibiting the formation of coke from unsaturated fragments. The production and / or transportation of hydrogen to a processing facility is expensive. 200535232 Coke can form and / or deposit on the catalyst surface at a rapid rate during the processing of inferior crude oil. Catalysts to regenerate catalysts contaminated with coke can be expensive. The high temperatures used during regeneration may also weaken the catalyst's activity and / or degrade the catalyst. Inferior crudes may contain acidic components that contribute to the total acid number ("tan") of the crude feed. Inferior crude oils with a relatively high TAN can result in the degradation of metallic components during transportation and / or processing of inferior crude oils. Removal of acidic components from inferior crude oil may include chemically neutralizing the acidic components with various bases. Alternatively, anticorrosive attribution may be used in transportation equipment and / or processing equipment. The use of anti-corrosion metals often involves considerable costs ’, so the use of anti-corrosion metals in existing equipment may not be desirable. Another method of suppressing corruption can involve adding scum inhibitors to inferior crudes prior to transportation and / or processing of inferior crudes. The use of corrosion inhibitors may negatively affect the equipment used to process the crude oil and / or the quality of the products made from the crude oil. Inferior crude oils can contain relatively high amounts of metallic contaminants such as iron, rhenium, and / or iron. During the processing of such crude oils, metal contaminants and / or compounds of metal contaminants may be deposited on the surface of the catalyst or the void volume of the catalyst. Such deposits can cause low catalyst activity. Inferior crude oils often contain organically bonded heteroatoms (such as sulfur, oxygen, and nitrogen). Bonded heteroatoms may have adverse effects on the catalyst in some cases. Metal test salts and / or soil test metal salts have been used in the process of residue desulfurization. These procedures are prone to poor desulfurization efficiency, 'producing oil-insoluble mashes, poor demetallization efficiency, forming a substantially inseparable salt-oil mixture, using large amounts of hydrogen, and / or fairly high hydrogen pressure . 200535232 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 numbers: 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 to McCollum et al .; awarded to

McCollum et al. 3,960,708; awarded to Baird, Jr. et al. 4,1 19,528; awarded to Baird, Jr. et al. 4,127,470; awarded to Fujimori et al. 4,224,140; awarded to Heredy et al. 4,43 7,980; 4,591,426 to Krasuk%; 4,665,261 to Mazurek; 5,064,523 to Kretschmar et al; 5,166,118 to Kretschmar et al; 5,288,681 to Gatsis; Sudhakar to Sudhakar Et al. 6,547,957; and US Patent Application Publication Numbers: 20030000867 to Reynolds and 200301493 17 to Rendina, summarizing various methods and systems for processing crude oil. However, the methods, systems, and catalysts described in these patents have limited applicability due to the many technical issues mentioned above. In short, 'inferior crude oils generally have undesired properties (e.g., relatively high residues, a tendency to corrode equipment, and / or a tendency to consume a significant amount of hydrogen during processing). Other undesirable properties include relatively high amounts of unwanted constituents (eg ... quite high TAN, organically bonded heteroatoms and / or gold 200535232 genus / defectives). Stingy properties often cause problems in traditional transportation and / or processing facilities, including increased corrosivity, reduced catalyst life, and / or increased lice use during processing. Because of Λ, there is a clear economic and technical need for improved systems, methods and / or catalysts for converting inferior crude oil into crude oil 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 one or more catalysts to produce a complete product that includes crude oil products and, in some embodiments, non-condensable gases. . The invention described in this article is also generalized about Langzhong and its ancient details: 14, 4, 8 and / or 〒 has a novel combination of ingredients. Such compositions can be obtained by using the systems and methods described herein. The present invention provides a method for preparing a crude oil product, which comprises contacting a crude oil feed with a wind source in the presence of one or more angles: a right-side catalyst,卩 Manufacture of crude oil products, wherein one or more of the catalysts contain catalysts containing ". The invention also provides a method for manufacturing crude oil products, which includes crude oil feed and hydrogen source in the presence of one or more catalysts Contact: The complete product of the spoon eight crude oil product, wherein the crude oil product is a liquid mixture at 25. 2 MPa, at least one of the catalysts includes: ,, · 101 metal sulfide, and the crude oil feed has per gram Crude oil feed to 3 = residue content of excessive residue, as measured by ASTM & 0530. Restrict the contact conditions so that the crude oil product is per gram of crude oil product; and the controlled coke, crude oil product is Grams of crude oil products contain up to 2.05 light oils, and the light oils have an octane number of at least 70. The grams of the present invention also provide a method for preparing crude oil products including the 200535232 crude oil feed with a hydrogen source in Contact in the presence of one or more catalysts, _ Complete product of crude oil product, wherein the crude oil product is a liquid mixture at 25. 22 MPa, at least one of the catalysts is a metal sulfide, and the crude oil feed has a residue content per gram of crude oil feed to the transition residue For example, if the volatility method is used in the method of 仏 53〇7, so that the crude oil product contains kerosene, the kerosene system has at least 0.2 grams of aromatic compounds per gram: $, as determined by AS The kerosene has a freezing point at a temperature of at most _3 ..., and the crude oil product is 0.05 g of coke per gram of crude oil. 3 The present invention also provides a method for manufacturing a crude oil product, the crude oil feed Contact with a hydrogen source in the presence of-or multiple catalysts = the complete product of a crude product, where the crude product is a liquid mixture at 25. ^ = ㈣, at least one of the catalysts contains multiple = metal sulfides, and the crude The feed has at least a slag content per gram of crude feed; and controlled contact conditions such that the original :::::::: r °. ° 5 g of coke, of which the crude product: 2: Second: the sub-anodous-more " 5 '如 — 法 D673. The present invention also provides a Method for making crude oil product =: contacting a hydrogen source in the presence of-or multiple catalysts to produce a complete product of the second crude oil product, wherein the crude product is at least one of U. Sulfide, and the crude oil feed has a weight per gram of crude oil feed,… 200535232 Residue content owed / checked, as determined by ASTM method D5307, and the atomic hydrogen to atom in the crude oil feed The weight ratio of carbon (H / C) is at least 1.5; and the contact conditions are controlled so that the crude oil product has an atomic H / c ratio of 8 (M20% atomic H / C ratio of the crude oil feed, the crude oil product has at most Residue content of 30% of the residue content of the crude oil feed, as measured by the astm method D5307, 'crude oil product contains at least 0. 0 01 grams of light oil' per gram of crude oil product, and the light oil has At least 70 octane. 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 a crude oil product, wherein the crude oil product is at 25 ° C and 〇1〇1 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 grams of residue per gram of crude oil feed, such as in the ASTM method As determined by D5307; and controlling the exposure conditions so that the crude oil product contains at least ⑴ grams of light oil per gram of crude oil product, the light oil having an octane number of at least 70; kerosene of at least 0.001 The kerosene contains aromatic compounds, the kerosene system contains at least 0.2 grams of aromatic compounds per gram of kerosene, as measured by ASTM method D5186, and the kerosene has a freezing point at a temperature of at most 300 ° C, such as Measured by AStm method D2386; at least ο · οοι gram of vacuum gas oil (VG0), which VG0 contains at least 0.3 grams of aromatic compounds per gram VG0, such as ιρ and up to 0.05 grams of residue As in astm Measured by 3 6 8/90; Measured by method D5307. The present invention also provides a method for producing a crude oil product by using a crude oil feed and a hydrogen source, which comprises contacting one or more catalysts containing a transition metal sulfide catalyst 200535232 to produce a complete product including the crude oil product, Where =, the thing is at 25. . And 〇 〇] coffee is a liquid mixture, the transition: Shi Caohua catalyst per gram of total transition metal sulfide catalyst contains a total of ... 4 grams-or more transition metal sulfide, the crude oil is fed and has Each gram of crude oil is fed with at least 0.2 grams of stubble content, as measured by the ASTM method; and the contact conditions are controlled so that the crude oil product contains at most. .05 grams of coke 'and the crude product has a residual content that is the residual content of the crude feed, as determined by ASTM method D5307. The present invention also provides a method for manufacturing a crude oil product, i comprising contacting a material with a chlorine source under one or more catalysts containing a transition metal sulfide catalyst to produce a complete product containing a crude oil product, wherein the crude oil product is It is a liquid mixture at 25 ° C and O.ioi Mpa. The transition metal sulfide catalyst contains a total of at least 0.4 grams of-or more transition metal sulfides per gram of total transition metal sulfide catalyst, and the crude oil is fed. And has a gas content of at least 0.0001 grams of nitrogen per crude oil feed, and the crude oil feed has a residual content of at least 0.2 grams of residue per gram of crude oil feed; and controlling the contact bar to obtain a crude oil product having It is at most the random content of the nitrogen content of the crude feed, and the crude product has a residue content of at most 30% of the original feed content. The nitrogen content is as determined by ASTM method D5762. The crumb content is determined by ASTM method d53q7. 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 comprising a transition metal sulfide catalyst to produce a complete product comprising a crude oil product, wherein The 11 200535232 crude oil product is a liquid mixture at 25 and 0.101 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 total Ni / V / Fe content of at least 0.0001 grams of Ni / V / Fe per gram of crude oil feed, and

The crude oil feed has a residue content of at least 0.0001 grams of residue per gram of crude oil feed and controlled contact conditions 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 The Ni / V / Fe content is 90% of the total Ni / V / Fe content. The crude oil product has a residue content of at most 30% of the crude feed residue content. The Ni / V / Fe content is as follows. It is measured by ASTM method D5863, and the residue content is measured by ASTM 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—or a plurality of catalysts comprising a transition metal sulfide catalyst—to produce a complete product comprising a crude product, wherein The crude oil product is a liquid mixture at 25 and 0.1 (1). The transition metal sulfide catalyst contains at least one gram of transition metal sulfide per gram of total transition metal sulfide catalyst. And a sulfur content of at least 0.001 grams of sulfur per gram of crude oil feed, and the crude oil feed has at least a G · 2 ^ ㈣㈣ content per gram of crude oil feed; and controlling contact with spare parts so that the original source has · 1 The stone melon containing 70% of the sulfur content of the crude oil feed, and the crude oil product has a residual content of at most the residual content of the crude oil feed, wherein the sulfur content is such as by the astm method = 9 The test results are shown in Table 4, but the residues are determined; the test contents are as measured by ASTM method D53G7. This' X Ming also provides a 12 200535232 method of manufacturing a transition metal sulfide catalyst composition, including: mixing a transition metal oxide with a metal salt to form a transition metal oxide / metal salt mixture; The / metal salt mixture reacts with rhenium to form an intermediate; and the intermediate is reacted with sulfur in the presence of one or more smokes to produce a transition metal sulfide catalyst. 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 is at 25. . It is a liquid mixture with 0.101 Mpa. The transition metal M catalyst contains transition metal sulfide. 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 metal sulfide catalyst system is obtained as follows: a transition metal oxide and a metal salt ^ to form a transition A metal oxide / metal salt mixture; reacting the transition metal oxide / metal salt mixture with hydrogen to form an intermediate; and reacting the intermediate with sulfur in the presence of one or more hydrocarbons to produce a transition metal sulfide catalyst. The present invention also provides a method for manufacturing 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 and 0.101 Mpa Is a liquid mixture, and the crude oil feed contains at least 0.2 grams of residues per gram of crude feed, as determined by ASTM method D5307; the complete product of at least a fraction is made into a vapor; at 25 and 0.101 Mpa Undercooling 13 200535232 condenses at least a portion of the vapor; and forms a crude oil product, wherein the crude oil product contains per gram of crude oil product: at least 0 001 grams of light oil, the light oil having an octane number of at least 70; at least 0.00 1 gram of VG0, the mother gram of VGO has at least 〇3 grams of aromatic compounds, as determined by the IP method 368/90; and up to 0.05 grams of residue, such as by the ASTM method 503 Measured by. 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 a whole product including a crude oil product, wherein the crude oil feed has Residue content of at least 0.2 g of residue, as determined by ASTM method 05307, the crude product is a liquid mixture at 25 and 0-101 Mpa, and the crude product contains at least 0.00 per gram of crude product. 〇g of light oil, which contains at least Q g of monocyclic ring aromatic compounds per gram of light oil as measured by ASTM method D6730; ; And up to 0.05 g of residue, as measured by ASTM method D5307, this month also provides a method for manufacturing crude oil products, which includes: contacting a crude oil feed with a hydrogen source in the presence of an inorganic salt catalyst to Manufacture of a complete product comprising the original: product, where the crude feed has a residue content of 0.22 grams of residue per gram of crude feed, as determined by ASTM method β5307. The crude oil product was at 25. . It is a liquid mixture with 0.101 Mpa, and the crude oil product contains at least MM grams of diesel oil per gram of crude oil product ^ This diesel oil contains at least 0.3 grams of aromatic compounds per gram of diesel oil, as described in P method 368/90. Assayer; at least 001 grams, and the vg〇 14 200535232 grams of VGO 3 have at least 〇3 grams of aromatization; and at most gram of residual heart as measured by the method . — By ASTM method D53〇7 The present invention also provides a method for producing crude oil, crude oil feed and gas source in the presence of an inorganic salt catalyst = method 'which includes: the complete product of the oil product, f' to produce crude oil containing crude r 忑The product is a liquid mixture under 2 and the crude oil feed has a residual content of the factory. ⑼gram grams of residual fish, such as at least 0.2 Ge from the raw material / from the ASTM method D5307 crude oil feed has a crude oil feed per gram At most, the monocyclic cyclic aromatic compound of the substance is contained in a chemical compound, and the control contact is at most 0.2 g per gram of crude oil feed during the contact. . , 'Makes the formation of non-condensable hydrocarbons at ¥, such as mass and: make crude oil products have at least 5% greater than the crude feed feed monodiaryl = the compound contains fluorene-containing early ring aromatic compounds, of which the monocyclic ring Aromatic content is as measured by ASTM method D673. The present invention also provides a method for producing a crude oil product, which comprises: contacting a crude oil feed with a source of radon 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 25 ° C. with 〇i〇i —a is a liquid mixture, the crude feed has a residue content of at least grams of residue per gram of crude feed, as determined by ASTM method D5307, and the crude 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 olefin content of the crude feed, where the olefin content is as determined by the astm method D6730. 15 200535232 The present invention also provides a method for producing 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 comprising a crude oil product, wherein the crude oil product is reacted at 25 ° C with The composition is in liquid version under 010 MPa. The crude oil feed has at least 0.2 grams of slag per gram of crude oil feed, and the inorganic salt catalyst exhibits at 50. The turning point of the exhaust gas in the temperature range between and 5⑽, as measured by the product's Temporal Analysis 〇f Pr〇ducts (ΤΑρ); and control the contact bar #, so that the crude oil production bucket has at most The crude oil feed residue contains a residue content of 30%, which is expressed in grams per gram of crude residue per gram of crude oil product, wherein the residue content is determined by the 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 complete product including a crude oil product, wherein the crude oil product is at 25 and 0.101 Mpa as 'Liquid mixture' The crude oil feed has a residue content of at least 0.2 ^ residue per gram of crude oil feed, the inorganic salt catalyst contains at least two inorganic metal winds and the inorganic salt catalyst exhibits an exhaust gas in a temperature range. Exhaust gas turning point, as measured by Product Instantaneous Analysis (TAP), where the exhaust gas turning point temperature range is 0) DSC temperature to ^ of the two inorganic metal salts and (b) DSC temperature of the inorganic salt catalyst Between; and controlling the contact conditions so that the crude oil product has a residue content of at most 30% of the crude oil feed, which is expressed in grams of residue per gram of crude oil product, where the residue content is based on ASTM Assayed by Method D5307. The present invention also provides a method for manufacturing a crude oil product, which includes: contacting the 2005 200535232 crude oil feed with a hydrogen source in the presence of an inorganic salt catalyst, and the complete product of the oil product is formed in the bean & The intermediate crude oil product is at 25 ° C. With O.HHMpa-liquid admixture. The crude oil feed has a residual content of at least 克 grams of residue per gram of crude oil feed, as measured by ASTMD53, and the inorganic salt The catalyst exhibited a turning point in the exhaust gas from the limbs in the temperature range between 500 ° C and 500 ° C, as measured by Product Instantaneous Analysis (TAP); and the production of crude oil products at 25. . And 〇ι〇ι milk measurement: the volume of the crude oil product obtained at the time of limb accumulation is at least 5 volumes. 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 a complete product including a source / source product, wherein the continuous, Bajia 4 crude oil product A liquid mixture at 25 ° C and 0.001 Mpa, this crude oil feed has at least 02 per gram of crude oil feed. Gram residue's radon content ’and the inorganic salt catalyst exhibits an exhaust gas turning point of the exhaust gas in a temperature range between + ° C, such as the product

According to the transient analysis (TAP), the GWA and the contact conditions are controlled so that during the contact, there is at most 0.2 g per gram of crude oil feed at 25. . Formation of non-condensable hydrocarbons with 〇 ι〇ι ¥, 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 the crude oil product, wherein the crude oil product is at 25 ° C WiiMpa Is a liquid mixture, the crude oil feed has a residue content of at least 0.02 grams of residue per gram of crude oil feed, and the inorganic salt catalyst has a thermal transition in a temperature range between 2000% and 5000 ° C, As by differential scanning calorimetry 17 200535232

Dsc) Measured at a rate of 10 ° C per minute, and control the contact conditions so that the crude oil product has a residue content of at most 30% of the crude feed residue content, which is measured in grams of residue per gram of crude product Indicates that the content of the residue is as measured by ASTM method D5307. 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 a complete product comprising a crude oil product, wherein the crude oil product is at 25 ° C and 〇1〇 1 is a liquid mixture, the crude oil feed has a residue content of at least q.2 grams of residue per gram of crude oil feed, and the ionic conductivity of the inorganic salt catalyst is at least one of the inorganic salts in the inorganic salt catalyst in 300 ° C to 500 ° C. (: Ionic conductivity at a temperature in the range; and control of the contact conditions so that the crude oil product has a residue content of 3% of the crude feed residue content, which is expressed in grams of residue per gram of crude product, of which the residue The content is as determined by ASTM method D5 3 07. 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 a complete product containing the crude oil product. Product, wherein the crude oil product is a liquid mixture at 25% and Gi () i Mpa, the crude oil feed has a residual content of at least 0.2 grams of residue per gram of crude oil feed, the inorganic salt catalyst contains a metal test A salt, wherein at least one of the metal test rhenium is metal test rhenium carbonate, and the metal test has at least one atomic sequence of at least η and at least one metal test with at least ^ of the metal test at least one of the original metal test; Η — 禋 atomic ratio 疋 is in the range of 0.1 to 10; and controlling the contact conditions so that the crude oil product has at most feed for the crude oil

Residue content t 30% Residue content 'wherein the residue content is determined by ASTM 18 200535232 method D5307. The present 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 The residue content of the residue, the inorganic salt catalyst includes an alkali metal salt, at least one of the alkali metal salts in # is an alkali metal hydroxide, and the alkali metal has an atomic order of at least Η, and the atomic order is at least 丨 丨At least one atomic ratio of the alkali metal to the alkali metal having an atomic order greater than 1 is in. Within the range of 10 to 10; making at least: a portion of the complete product into a vapor; cooling at least a portion of the vapor at 25 and 001; and forming the crude product, wherein the crude product has at most the crude oil A residue content of 30% of the feed residue content. 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 production wherein the crude oil feed has at least 0.2 grams of residue per gram of crude oil feed Residue, amount, the inorganic salt catalyst contains an alkali metal salt, at least one of the alkali metal salts in * is an alkali metal hydride, and the alkali metal has at least u: subsequence 'and atomic sequence of at least 11 Alkali metals have a base with an atomic number greater than η: at least one atomic ratio of the genus is in the range of 〇1 to ι〇; at least one spoon of the product of Fanwang is made into radon; at 25 ℃ and 〇i〇i Condensing at least-a portion of the vapor; and a residue content that forms the crude oil product, #% crude oil produced, and is at least %% of the crude oil feed residue content. The present invention also provides a method for producing 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 whole product containing the original product, wherein the crude oil product is at 25. (: It is a liquid mixture with 0.101 Mpa 19 200535232. The crude oil feed has a residue content of at least 0.02 grams of residue per gram of crude oil feed. The inorganic salt catalyst contains-or more metal test salts,-or more earth test metals. Salt or a mixture thereof, wherein one of the metal test salts is an alkali metal carbonate, wherein the alkali metal has an atomic order of at least 丨 丨, and the contact conditions are controlled so that the crude oil product has at most 30% of the residue content of the crude oil feed The residual content is determined as described in ASTM method D5307. 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 a complete product containing a crude oil product, wherein the crude oil product is a liquid mixture at 100 MPa and 100 MPa, the crude oil feed has at least: slag content per gram of crude oil feed, and the inorganic salt catalyst contains-or more bases Metal hydrogen: "or more alkaline earth metal salts or mixtures thereof, in which the alkali metal I has an atomic sequence of less than 11; and controlling the contact conditions so that crude oil production is the same as the crude oil Residue content of 30% of the residue content of the material, the residue content in the basin is as measured by ASTM ^. _ :: Invention: Provide a method for manufacturing crude oil products, including the It is contacted in the presence of it to produce a complete product containing crude oil products. ^ The clothing was originally a night-hearted man, and the crude oil product was at 2 "c and 0.11Mpa ',' The crude oil feed has a residue of Hedan # — · 2 compounds per gram of crude oil fed to gram of residue; the organic salt catalyst contains-or more alkali metal hydrogens that have earth-to-earth soil metal salts or Mixture 'and wherein the metal test bean has an atomic sequence of 12; and controlling the contact conditions so that crude oil is produced, and the residue content of the crude oil feed residue content is 30%, 20 200535232 is based on per gram of crude oil product The number of grams of residue indicated that the content of 1 dan dry residue was determined by the AS TM method D 5 3 0 7. The present invention also provides a method for manufacturing gas, which includes: feeding crude oil and / or multiple Hydrocarbons are contacted in the presence of an inorganic salt catalyst and water, the hydrocarbons having a range of i to 6 The number of carbons in 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 discharge n of the discharged milk in a temperature range between 50 and 500 ° C. The turning point of the exhaust gas of the body, such as the product transient analysis (TAP) gas. The measured-and the generation of hydrogen. The invention also provides a method of manufacturing the original paint 4 ... The inorganic salt catalyst is contacted in the presence of steam to produce a milk machine that contains hydrogen for the gas stream, wherein the first crude oil feed has a residual content of at least 0 "grams of residue per gram of oil feed, such as using the eight coffee method called Sisuo The tester, and the inorganic salt catalyst showed at 50. 〇 and _. The exhaust gas of the exhaust gas in the temperature range, ΤΛηΛ has a turning point, as determined by the product transient analysis (TAP); the first Qiu Ba i π Shi Shi 7 Shi Xingdi catalyst at least at the mouth of the knife The complete product of the existing gas stream, 1 in ... produced ... widely contains the crude oil product "Original, from the product at 25 ° C and 0.101 Mpa in the liquid rib mixture; and control contact strip ,,,,,,,,,,, ... One or more properties of the crude oil product are compared to the respective individual of the second crude oil feed, which is at least 1G%. ^ Each of the multiple properties of the 'changes' The present invention also provides a method of generating a gas feed and Inorganic _ contact force γ, account for six…… make the crude oil contact per gram of h catalyst in the presence of b, where the crude oil is fed and at least 0.2 grams of crude gram crude feed

Dude, check the content of the residue, as determined by ASTM 21 200535232 method D5370; the ratio of carbon monoxide to carbon dioxide is at least 0.3. And generating a gas stream containing hydrogen, and carbon monoxide to carbon dioxide. The present invention also provides a method for manufacturing a crude oil product, which includes: adjusting P ..., catalyst I to make crude oil feed with hydrogen The source contacted M under the adjusted inorganic salt catalyst to make a complete product containing a crude oil product, wherein the crude oil product was a liquid mixture at 25 ° C and 0.11 Mpa, and the crude oil had a crude oil feed per gram of crude oil. At least 0.2 grams of crushed crushed content; and controlled contact conditions so that the crude oil product has a residue content of at most 30% of the crude feed residue, which is in grams per gram of crude product Table D, and dross content are measured by ASTM method D5307. The present invention also provides a crude oil composition, which includes 纟 0.ΗΗ MPa, fortifications whose range is between tc and 53rC (1, F.F), and which include hetero-chain and normal-chain hydrocarbons, among which The weight-to-weight ratio of heterogeneous hydrocarbons to positive bond burners is at most 14, as determined by ASTM method D6730. The present invention also provides a crude oil composition containing at least 0.001 grams of hydrocarbons having a boiling range distribution of at most 205 ° C (400 F) at 0.101 MPa per gram of the composition, and at least 0,001 grams in 0.01%. Hydrocarbons with a boiling range of 1 kPa between 204 ° C and 300 0c, at least 0.001 grams of boiling ranges distributed between 3000c and 4000 (: Hydrocarbons, and at least 0.001 grams of hydrocarbons with a boiling range distributed between 4000 c and MS c (1,000 ° F) at 0.11 MPa, with a boiling range distribution of at most 204 The hydrocarbons of C include isoparaffin and normal paraffin, wherein the weight ratio of isoparaffin to normal chain is at most 1.4, as determined by ASTM method D6730. 22 200535232 The present invention also provides a crude oil composition The composition of Gan-Shiqi mother gram contains: at least 0.001 grams of light oil, the light oil has an octane number of up to 70, and the light oil contains at most 0.15 grams per gram of light oil, Zanfanfan], as measured by ASTM method D6730; at least o.ool grams of Fan 7 medium oil, this kerosene contains at least 0.2 grams of aromatic oil per gram of kerosene Compounds, as measured by μ ASTM method D5186, and the kerosene has a freezing point of at most −30, p, w & /, as measured by ASTM method D23 86; and at most Wang Xi 0.05 g of residue, as measured by ASTM method D5307. The present invention also provides a crude oil composition containing per gram composition: up to 0.15 g of non-condensable flue gas at 25 V and 0.101 Mpa, the Non-condensable hydrocarbon gas system contains at most G3 grams of hydrocarbons with a carbon number of m (Ci to c3) per gram of non-condensable hydrocarbon gas; at least 0.001 grams of light oil having a scorch value of at least 70; at least grams of Kerosene, which has an SI point at most at a temperature 'as measured by ASTM & D2386, and the kerosene contains at least 0.2 grams of aromatic compounds per gram of kerosene, as measured by the astm method D5U6; and at most 0. 〇05 grams of residual fish, as determined by the method D5307. The present invention also provides a crude oil composition, each gram of composition contains: at most 0.05 grams of residue, as measured by ASTM method D53〇7 Measured by: > '0.001 g Boiling range distribution at 0.101 MPa is at most 204 .C (400 ° F) hydrocarbons; at least 0.001 g of hydrocarbons with a boiling range between 204 ° C and 300 ° C at 0 001 Mpa; at least 0.001 g at 0 ° C. The boiling range under iMpa is distributed between 300 ° C and 400. (: hydrocarbons between: at least 0.001 g of hydrocarbons with boiling range between 400 ℃ and 538 ℃ (23 200535232 ° F) at 0.101 MPa And hydrocarbons in the boiling range distribution between 20 ℃ and 204 0C include olefins with terminal double bonds and 晞 fe with intramolecular double bonds, where the dilute hydrocarbons with terminal double bonds have an intramolecular double bond The molar ratio of the dilute hydrocarbons of the bond is at least 0.4, as determined by ASTM method D6730. The present invention also provides a crude oil composition, each gram of which contains: at most 0.05 grams of residue, as determined by ASTM method D5307; and a boiling range of at least o.ool gram distribution over 20. Hydrocarbon mixtures between [and 538 〇c 〇〇〇〇〇〇F), as determined by ASTM method D5307, and the hydrocarbon mixture per gram of the hydrocarbon mixture contains: at least 0.001 g of chain Alkanes, as measured by ASTM method D6730; at least 0.001 grams of olefins, as measured by ASTM method D6730, and the olefins contain at least o.ool grams of terminal olefins per gram of olefin, such as Measured by ASTM method D673; at least 0.001 grams of light oil; at least 0.001 grams of kerosene, which is at least 0.2 grams of aromatic compounds per gram of kerosene a, as measured by astm method Or at least 0.001 grams of diesel, which contains at least 0.3 grams of aromatic compounds per gram of diesel, as determined by the Ip method 368/90; and at least G.GG 1 gram of vacuum gas oil (VGO ), The VG0 series contains at least 0.3 grams of aromatic compounds per gram of VG0 ·, as determined by IP "368/90 0 also provides a crude oil composition, which per gram composition contains: at most 0 · 05 g of residue, as determined by the astm method D53〇7; at least 0,001 g of boiling range distribution at 0. 101 MPa to Township 20CC (400 ° F) hydrocarbons; at least 0.0001 ^ υ · 010 grams of hydrocarbons with a boiling range of between 0.1 ° C and 300 ° C at 0.101 MPa; at least 0.00 〇1 grams of hydrocarbons with a boiling range between 300 and 400 at 〇ioi Mpa 24 200535232; and at least 0.001 grams with a boiling range of 400 and 538 ℃ (1,000 〇F) at 0.101 MPa ), As measured by ASTM method 02887, hydrocarbons with a boiling range distribution of up to 204 γ hydrocarbons with a boiling range distribution of up to 204 C per gram contain at least 0.001 g Olefins, as determined by aSTM method D6730; and at least 0.001 grams of bonded hydrocarbons, the bonded hydrocarbons containing isoparaffins and normal paraffins, wherein the weight ratio of isoparaffins to normal paraffins is at most 1 -4, as measured by ASTM method D673O. The present invention also provides a crude oil composition, each gram of which contains: at most 0.05 g of residue, as measured by ASTM method D5307; and at least 0.001 g of boiling range distribution at 0. MPa as Hydrocarbons up to 204 ° C (400 ° F); at least 0.001 g has a boiling range of 204 at 100 MPa. (: And 300. hydrocarbons between :: at least 0.001 g of hydrocarbons having a boiling range distributed between 3,000 c and 400% at 0.001 MPa; and to 0.001 g Hydrocarbons whose boiling range is distributed between 400 and 538 C (1,000 000 F) at 0.001 MPa, as determined by the astm method d⑽7; and where the boiling range is distributed at · 1 The hydrocarbons between 〇0 (: and 〇4〇c) contains a compound having a carbon number of 4 (G), and the C4 compound contains at least 0.000 g of butadiene per gram of the compound. A crude oil composition is also provided, which contains per gram of composition: at most 0.05 grams of remnants; at least 0.001 grams of hydrocarbons with a boiling range distribution of at most 20CC (40 (KF), at least 0 at 0.001 Mpa) 001 grams of hydrocarbons with a boiling range between 204 and 300 at 0101 MPa, at least 0.001 grams of 300c and 4000c with a boiling range at 0.101 MPa 25 200535232 Hydrocarbons and hydrocarbons with a boiling range of at least 0 ° C and 538 ° C • 101 MPa; and greater than 0 g but less than 0.01 gen. There is at least one or more gold assays. The present invention also provides one or more refined linseed "feeds" with the root method or composition which: has not been used in U, therapy and / or fractionation; (b) contains + / Knife with a carbon number 刀 4 or more, and the crude oil feed contains at least 0.5 grams of this significant component per gram of crude oil feed; (C) contains a furnace _-.; 3 ^ lock 'Some of which have: at 0.101 MPa Under-, 100 c / Furten range distribution, between 10000 c and 0 ° C at 001 MPa, Folten range distribution, at 0 ° C and 300 ° C at ⑻MPa The boiling range distribution between the boiling range distribution between 300 ° C and 4000 ° C at 0.101 MPa and the boiling range distribution between 400 ° 'and 7GG ° C at 0.101 MPa; W per A gram of crude oil feed contains: at least 0.001 grams of hydrocarbons with a boiling range distribution below 0.100 MPa at 0.101 MPa, at least o.ool grams of Fotent distribution at 0.101 MPa at 200 ° C Intermediate hydrocarbons, at least 0.001 () 1 g boiling range at 001 Mpa distribution in 200. (: hydrocarbons between and 3,000 c, at least 0.001 g at 0.101 MPa Boiling Range distribution between 300.00 and 40,000 (: enthalpy species, and at least 0.001 grams of hydrocarbons with boiling range distribution between 400c and 700 ° C at 0.001 MPa; ( e) has a TAN; (f) 0.2-0.99 grams, 0.3_0_8 grams, or 0.4.07 grams of residue per gram of crude feed; (magic package 3 nickel, vanadium, iron or its A mixture; (h) containing sulfur; and / or rhenium nitrogen-containing hydrocarbons. In some specific examples, the present invention also provides a hydrogen source containing molecular atmosphere in combination with one or more of the methods or compositions according to the method of the present invention. Comprises light hydrocarbons; (d) comprises methane, ethane, propane or mixtures thereof; (e) comprises water; and / or (f) mixtures thereof. In certain embodiments, the invention also provides and according to the invention A formula =: and a product—or a combination of multiple methods, which includes adjusting the titanium-free secondary media, wherein adjusting the inorganic catalyst includes: (i) adding an inorganic salt catalyst to a temperature of I π // 00 π ; And / or (b) the inorganic salt catalyst is heated to a temperature of; and the inorganic salt catalyst is cooled to a temperature of at most 500 = in some specific examples, the invention also provides a method according to the invention or, and, and A method of combining one or more raw materials into a product, which includes bringing crude oil into the door and controlling the contact conditions every time: ^ ^ Crude oil feed is at most. · 2 grams, at most. .15 Grams, up to. 0.05 grams on two or until the evening at 25 ° C 〇〇οοΜ # Cheng, such as quality β ϋ /, · pa 蚪 不The condensed hydrocarbons are 2 ^ wk; (b) the production temperature = internal or between -c; the pressure is within the range of 0 and 巳, and (d) the gaseous hydrogen needle meter is used to feed crude oil. The ratio is that during the production contact per cubic meter of crude oil feed, coke is contained in the complete product or in the product, so that the crude oil product is 0.05 g, at most 0.03 g per gram of crude product. , At most _ grams or at most 3 grams of annoyance; (h) making at least _ eight brothers to be semi-liquid or liquid; so that two = salt catalyst in this type of material TA ... the product has at most The crude oil feed (J) makes the crude oil product have

Material state / V / Fe content up to 90%, up to 50% or up to 5% total state / V / Fe content; (k) make the crude oil product have up to 90% sulfur content for the crude oil feed, Sulfur content of up to 60% or up to 30%; ⑴ makes the crude oil product have a nitrogen content of up to 90%, up to 70%, up to 50% or up to 10% of the nitrogen content of the crude feed; (m) makes crude oil The product has a residue content of at most 30%, at most 10%, or at most 5% of the crude feed feed residue content, (n) causes the ammonia system to co-produce with the crude product; (0) causes the crude product to contain A ' And the method further comprises: recovering methanol from the crude product; combining the recovered methanol with additional raw materials to form an additional crude feed / methanol mixture; and heating the additional crude feed / methanol mixture such that The TAN of the additional crude feed is reduced below; (P) causes one or more properties of the crude product to be changed by up to 90% compared to the individual or multiple properties of the crude feed; The amount of catalyst ranges from 100 grams of crude oil feed " 0 grams of total catalyst; And / or plutonium such that the hydrogen source is added to the crude feed before or during the contact.

2. In some specific examples, the present invention also provides contact conditions with one or more combinations of the method or composition according to the present invention, which includes: ⑷ mixing inorganic salt catalyst with crude oil feed at the following temperature , The straight salt catalyst is substantially insoluble in the crude oil feed; (b) search in the crude oil feed; inorganic catalyst; and / or make the crude oil feed with inorganic salt catalyst in water and " strip steam Contacting in the presence 'to make the complete product comprising an emu oil product which is a liquid mixture in STP. ^ K 矜 A method that does not invent a method or a combination of one or more of the methods' which includes bringing crude oil into the market 28 200535232…: Meng catalyst contact and it further includes: ⑷ before or during the contact ^: ..., Steam is provided to the contact zone; (b) the emulsion of the crude oil feed and water is formed when the crude oil feed is brought into contact with the inorganic salt catalyst and the hydrogen source; the contact zone is formed; and / or (d) the steam and inorganic The salt catalyst is contacted to at least partially remove coke from the surface of the inorganic salt catalyst. 2. 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 contacting a crude oil feed with an inorganic salt catalyst to make 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 at 25 people 0.11 Mpa to form the crude product, and the contact conditions are controlled such that (a) The crude product further comprises a component having a selected boiling range distribution; and / or (b) the crude product comprises a component having a selected ΔPI specific gravity. In some specific examples, the present invention also provides a method in combination with one or more of the party composition according to the present invention, which comprises contacting a crude oil feed with one or more catalysts and the one or more catalysts It is non-acidic. In some specific examples, the invention also provides a K3Fei () Si4 catalyst or a transition metal sulfide catalyst in combination with one or more of the methods or compositions according to the invention, which: (a) per gram of the K3Fei 〇SM catalyst or transition metal sulfide catalyst contains a total of at least 0.4 grams, at least 0.6 grams or at least 0.8 grams of at least one transition metal sulfide, (b) K3Fe1GSM catalyst or transition metal sulfide The atomic ratio of the transition metal to sulfur in the catalyst is in the range of 0.2 to 20, (c) further contains one or more metal detectors, one or more metal detectors or compounds or mixtures thereof, (d ) Further comprising one or more soil test 29 200535232 =, one or more soil test metals-or more compounds or mixtures thereof; (e) each step of one or more metal tests, one or more metal tests-or more compounds or In the mixture, the Chinese name "Xin Ai Cheng Cheng", "the atomic ratio of the transition metal to sulfur in the 3 A catalyst or the transition metal sulfur catalyst is in the range of 0.5 to 25, and the alkali metal to the transition metal atom; Step-up contains-or more soil testing metals, one ==: genus : A variety of compounds or their mixtures, in this team. The atomic ratio of the transition metal to sulfur in the s14 catalyst or the stone claw catalyst is within the range of 0.5 to 2.5. The atomic ratio is in the range of above q to '1 ^; (g) the step further includes zinc; (h) the step further includes lamps; the step includes KFeSr and / or scandium is non-acidic. In some specific examples 'The present invention also provides a combination of the square-shaped composition according to the present invention—or a combination thereof', wherein the media is on the spot in some specific examples, and the present invention also provides the same as the formula according to the present invention. A combination of one or more transition metal sulfides, or two or more transition metal sulfides, containing two or more transition metals selected from the 6 to 10 of the periodic table: genus, or one or more transition metal selected from the Or more compounds or compounds thereof; ⑻ contains-or more iron sulfides; ⑷ contains = containing tons; ⑷ contains a mixture of iron sulfides, wherein the iron is sulphurized ... Formula (w) S represents, where it is done at 0 Above the range of 0.17; ⑺, after contacting with the crude oil feed, further contains less than 10 m '(g) 6 Hai or Among transition metals of a variety of transition metal sulfides, iron is; and / or (h) is deposited on a carrier, and the transition metal 30 200535232 sulfide catalyst contains up to gram of catalyst. 25 grams of total carrier. In some specific examples, the present invention also provides contact with one or more of the methods or compositions according to the present invention.

:, And a method for forming a substance, the method comprising: transition metal oxide and metal salt 'to form a transition metal oxide / metal salt mixture; reacting the transition gold emulsion 7 metal salt mixture with hydrogen to form an intermediate; And reacting the intermediate with sulfur in the presence of one or more hydrocarbons to produce a transition metal sulfide catalyst: ⑷ the metal salt comprises a metal carbonate; ⑻ it further comprises dispersing the intermediate in one or more In liquid hydrocarbons, ㈣ react with sulfur; ⑷ where one or more of the hydrocarbons have a boiling point of at least 100,000%: ⑷ where one or more of the hydrocarbons are vg0, xylene, or a mixture thereof '( e) wherein the transition metal oxide and the metal salt are mixed includes: mixing the perylene metal oxide and the metal salt in the presence of deionized water to form a thirst ^ making the wet paste at a temperature ranging from 150.25 · (%) Under drying; and in the range from 300-600. . Calcining the dried paste at a temperature of 550 ° C .; wherein reacting the intermediate with sulfur includes adding the interstitial material to a temperature ranging from 240-350 ° C. in the presence of at least one of the hydrocarbons; 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, comprising: (a) one or more alkali metal carbonates, one or more alkaline earth Metal carbonates or mixtures thereof '(b) —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 a mixture thereof; (d) —one or more of one or more alkali metals 31 200535232

Sulfides, one or more sulfides of one or more earth test metals, or mixtures thereof; (e) —one or more amidines of one or more alkali metals, one or more amines of one or more alkaline earth metals, or mixtures thereof, ( f) one or more metals selected from columns 6-10 of the periodic table, one or more compounds or mixtures thereof selected from metals 6-10 of the periodic table, (g)-or more inorganic metal salts, And wherein at least one of the inorganic metal salts generates a hydride during the use of the catalyst; (h) sodium, potassium, tear, cesium or a mixture thereof; (i) calcium and / or magnesium; osmium sodium and potassium salts Mixture, and the potassium salt comprises potassium carbonate, bell hydroxide, potassium chloride, or a mixture thereof, and the sodium salt comprises sodium carbonate, steel hydroxide, sodium hydride, or a mixture thereof; and / or (k) a mixture thereof. In some specific examples, the present invention also provides an inorganic salt catalyst comprising an alkali metal in combination with one or more of the methods or compositions according to the present invention, wherein (a) an alkali metal pair atom having an atomic number of at least 11 The atomic ratio of an alkali metal having an order greater than u is in the range of 0.1 to 4; (b) at least two of the alkali metals are sodium and potassium, and the atomic ratio of sodium to potassium is in the range of 0.1 to 4 Within range; (c) $ / 卜 一 4 ^ in 5 metal inspection metals.

The main / both are sodium, potassium, and thallium, and sodium to potassium, sodium to thorium, and thorium and thorium are in the range of 0.1 to 5; (d) Among the alkali metals, sodium and potassium And the atomic ratios of sodium to potassium, sodium to potassium, and potassium to aluminum are in the range of A 1 · to 5; (e) at least three of the metals tested are potassium, thorium, and potassium. The atomic ratios of potassium to rhenium and planer to rhenium are each in the range of ο · 1 to 5. In some cases, > 1 ~ /, the present invention also provides a medium that is compatible with the compound or composition according to the invention, and the combination of one or more inorganic salts containing a carrier material. The carrier materials include hafnium oxide, calcium oxide, magnesium oxide, oxygen 32 200535232 titanium oxide, hydrotalcite, oxide oxide, germanium oxide, iron oxide, nickel oxide, zinc oxide, oxide oxide, antimony oxide, or mixtures thereof; and / or Incorporating into the carrier material are:-or more metals selected from the group of the Periodic Table, one of the metals selected from the Group of the Periodic Table of the Periodic Table-or more compounds. Metal carbonates, one or more Test metal hydroxides, one or more dimetal hydrides, one or more alkaline earth metal carbonates, one or more earth tests: belong to hydroxides,-or more alkaline earth metal hydrides and / or mixtures thereof.

In some specific examples, the present invention also provides a method in combination with-or more of the method or composition according to the present invention, which comprises contacting crude oil into a branch with an inorganic pigment medium, the towel of which: The catalyst activity is substantially unchanged in the presence of &a; and / or (b) 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: ⑷ a turning point of the exhaust gas in a temperature range of two P, and the Exhaust gas contains hydrogas and / or carbon dioxide; (b) at 2000-500CC.匚 or thermal transition in the temperature range between 3 00 400 c, as measured by differential scanning calorimetry at a heating rate of 10 C per knife; (c) between 200-500 ° C or 2,450; C DSC temperature in the range; ⑷ is at least 100. The X-ray diffraction pattern of the inorganic salt catalyst below 100 ° C at a degree of 〇 is greater than that of the X-ray diffraction pattern below 100 ° C, and / or ⑷ after adjustment, 3⑼. The ion conductivity is lower than the ion conductivity of the inorganic salt catalyst before adjustment. In some specific examples, the present invention also provides an inorganic salt catalyst in combination with one or more of the formula 33 200535232 or according to the present invention, which exhibits a turning point of discharge within a temperature range, please catty The tester and the contact conditions are such that the contact temperature is: (&) above T], where Ti is 30 ℃, 20 cC, or 10 ℃ below the TAP temperature of the inorganic salt catalyst Above, and / or (c) at least the D 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 is or among them. "" At least when the TAP temperature of the inorganic salt catalyst is It is liquid or semi-liquid, and the inorganic salt catalyst is substantially insoluble in the crude oil at least at the g TAP temperature: It is expected that the remaining TAP temperature is the minimum temperature at which the inorganic salt catalyst exhibits the turning point of the exhaust gas; ⑻ is in the range A mixture of a liquid phase and a solid phase at a temperature from 50.00 to 50000c; and / or (c) at least one of the two inorganic salts has a DSC temperature above 500 ° C. 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.

In the particle form test of a 1000 micron filter, when heated to a temperature of at least ° ^, it will self-shape under gravity and / or under a pressure of at least 7 so that the inorganic salt catalyst will change from the first form to the first. Two forms, and the second form is cooling the inorganic salt catalyst to 20 ° C. (: Can not be changed back to this first form. Also 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, per gram of the inorganic salt The catalyst contains ... (a) up to 0.01 g of lithium or a lithium compound, which is calculated based on the weight of Qu 34 200535232; (b) at most 1 g of i compound, the weight of this fine halogen is very different; δ; And 7 or ⑷ up to 0.001 grams of a glassy oxide compound. In certain embodiments, the present invention also provides for implantation with one or more of the methods or compositions according to the present invention-meaning I, and oral Where the whole product contains at least 0.8 grams of crude oil product per gram of complete product. In some specific examples, the present invention also provides one or more combinations with the method or composition according to the present invention, The crude oil product, which contains at most 3 grams, at most gram, at most gram, at most gram, at most 0 gram, gram ... 0.03 grams of fate; ⑻ per gram of crude oil product contains from 0 grams to 0.05 grams, please outline Gram or G Wei_G G1 1 coke; ⑷ has an olefin content of at least 10% greater than the olefin content of the crude oil feed; ⑷ per gram of crude oil product contains greater than 0 grams but less than 0.01 grams of total inorganic salt catalyst, such as The mass balance determiner '(e) contains at least 0 μg,' 0.00001-0.99 g, οι " grams, 0-6 〇8 grams of vg per gram of crude oil product; ⑴ includes VG and the paste per gram Contains at least 0.3 grams of aromatic compounds; ω contains 0.0000 grams or (M-0.5 grams of effluent; ⑻ up to 14 atomic H / C '⑴ has the crude oil feed H / c of 9 (μιη% of atomic haze; ⑴ monocyclic ring aromatic compound content having at least 10% greater than the monocyclic ring aromatic compound content of the crude oil feed; (k) containing xylenes, ethylbenzene or Monocyclic ring aromatic compounds of ethylbenzene compounds; ⑴ per gram of crude oil product contains at most (M grams of benzene, 0.05-5.15 grams of toluene, 0 009 grams of m-xylene, 0.5-0.15 Gram of o-xylene and 〇2_〇6 grams of para-xylene; ㈣ contains at least 0.0001 grams or 0.015 grams of diesel; ⑷ contains diesel, 35 200535232 2: Department Master gram diesel contains at least 0.3 grams of aromatic compounds,

f 2.0.1 grams of kerosene from 0 to 0.7 grams or grams; ⑻ contains kerosene, and the kerosene system contains at least 0.02 grams or at least 0.5 grams of a square group compound per gram of kerosene 'and / Or freezing point at a temperature of at most -30 ° C, at most _40 ° c or at most -50 ° C; ⑷ contains at least} grams or at least 〇5, light: ⑴ contains light oil, and the light oil is per gram The light oil contains at most _, at most 0.05 g or at most 002 g of benzene, at least 70, at least or at least 90 octane, and / or isoparaffin and n-paraffin, wherein The weight ratio of paraffin to normal paraffin is at most 1.4; and / or (s) has a volume of at least 10% greater than the original, from the feed volume. 〆

In some specific examples, the present invention also provides a method in combination with-or more, comprising contacting crude oil with a medium to form a complete product comprising a crude oil product. The progress of the method includes: The same as or different from the crude feed: 'combined to form a blend suitable for transportation; (b) combining crude products with a crude oil different from the crude feed to form a suitable processing facility (1) The crude oil product in the branch; (2) The crude oil product is divided into two formulas: two kinds of 1-field knife's are made from at least one of the distillates to produce transportation fuel; and / , Processing the transition gold sulfide catalyst to recover metal from the transition metal sulfide catalyst. In some specific shots, the present invention also provides a crude oil product that is equal to or greater than or equal to, which has at least 0.001 g of VG per gram of crude oil, and the vg 〇 series contains 5 small η 7 • 3 grams of aromatic compounds; (b) at least 0.001 grams of diesel, 36 200535232 and the diesel series contains at least 0.3 grams per gram of diesel, less 0.001 grams Light oil, and compounds; (c) to benzene containing light oil, mother gram light oil contains benzene, a minimum of 70, and / or hetero-chain hydrocarbons and normal chain ^ • 苴The weight ratio of the positive-bonded hydrocarbons is at most 2. The distribution of Yi Kefu Teng range is at most 2.4. ... ⑼ ... of = 5, and the mixture contains at most 3 g of olefins, (e) the atomic hydrogen in the composition is at most 1.75 or at most 1.8; (f ) At least 001

Bagu ... J grams of kerosene, and this kerosene ... per gram of kerosene

3 have up to ^ 0.5 grams of aromatic compounds and / or have at most ... c freezing point of temperature; tritium atomic hydrogen per gram of composition; (= ^ gas and light oil, when combined, there is at most 0.15 g per gram of combined non-condensable hydrocarbon gas and light oil β Alkenes; ⑴ non-condensable hydrocarbon gas and light oil, when combined, contain hetero-chain and normal-chain hydrocarbons, where the weight ratio of 1-chain hydrocarbons to normal-chain hydrocarbons in the combined light oil and non-condensable milk It is Zhixiang 14; hydrocarbons with up to 3 carbons, which include ... dilute hydrocarbons and paraffins with carbon numbers 2 (C2) and μ), and the combined C2 and q olefins to the combined dagger and q paraffin Weight ratio of up to 0.3; carbon number 2 (CD olefins and paraffins, where C2: »: Greek hydrocarbon to q-paraffin weight ratio is up to 0.2; and / or carbon number 3 (C3) Alkenes and paraffins, where the weight ratio of C3 olefins to C3 paraffins is at most 0.3; (k) has a butadiene content of at least 0.005 g; ⑴ has an API specific gravity in the range of 15 to 30 at 15.5 ° C; (It is called to have a total Ni / V / Fe of up to 0.00001 grams per gram of composition, and (η) has a boiling range distribution of at most 204. The paraffin content of the hydrocarbons is within the range of 0.7 g. ; (〇) boiling Hydrocarbons with a range of up to 204, with a boiling range of 37 200535232, with a distribution of up to 204. The broad u + octabutane group contains 0.001 to 0.5 g of olefins (p) including boiling of each olefin. The range distribution is at most 204 (including at least 0 hydrocarbons per gram of olefin, and the olefin series is distributed at most terminal dilute hydrocarbons to intramolecular olefins: and green has a gate of at least 0.4 and-, 'And / or ⑴ hydrocarbons within a range of 20% hydrocarbons per gram from 0 .. 01 _ .. 5 grams of 埽 = In some specific examples, the present invention also provides the same as the two according to the present invention: A combination of one or more crude oil products, which contains the package ,,, or less, wherein: (a) the alkali metal is up to ^, one is potassium, bismuth, or planer or a mixture thereof; and / _ 口Initially, and / or (b) y in the catalyst further comprises a transition metal, iron-potassium ore .... It is a sulfide and / or lignin. In further specific examples, specific examples from the present invention can be obtained. Merged with features from other specific examples of the invention. Examples u Features from a specific example may be combined with other specific examples The features of any one of them are combined. The crude oil product is obtained through any of the methods and systems described in this article that can be added to the specific embodiments described in this article to add additional features to the examples in the further embodiments. Mode] The invention is described in more detail here. A certain example of the present invention is also described in detail. It is an example of a dandelion. The name used in this article 38 200535232 is defined as "alkali metal," which refers to one or More than one compound selected from the periodic table. One or more compounds selected from the metal in column 1 of the periodic table, one or more compounds of the metal, or a mixture thereof. A metal, or a compound selected from the group consisting of metals in column 2 of the periodic table, or a plurality of compounds or mixtures thereof. "AMU" means the atomic mass unit. "ASTM" means American Standard Tests and Materials (a

Testing and Materials). "C5 asphaltene" refers to the pyrocyanine that is insoluble in scorch. Lithocyanin content is as measured by ASTM method D2007. Crude oil products, light oil, kerosene, diesel, and the fractional and atomic carbon percentages are API specific gravity as measured by the Hiran method called 91 "means the specific gravity of 15.5 ℃ Ding J. The API ratio is compared with Cao Sunshi by ASTM method D6822 Measured by: Shishi asphalt "refers to a type of Yanwa #Douyou. 1 Raw materials manufactured and / or obtained from the bottle factory are not listed unless otherwise mentioned; 5, upper, * R v Boiling of oil feed and / or complete product. Kiss the tester. Hydrocarbons are fortified alkanes, isoparaffins, alkenes such as alkanes & alkanes and aromatic compounds. The content of the compound is as measured by ASTM method D673. ^ The content of light oil diesel and VGO is as follows w TD * compounds are determined as described by IP method 368/90. Aromatic 39 200535232. The content of the substance in kerosene is determined by ASTM method D5 1 86. "Buxin", "Br011 sted-Lowry acid" refers to a molecular body that has the ability to donate protons to another molecular body. "Brunister-Rory base" refers to the ability to accept The molecular body of the shellfish of another molecular body. Examples of Bronister-Rore base include hydroxide ⑺Η), water (H2〇), metaborate (RC02-1), halide (Br—, C1 F, 1) , Hydrogen sulfate (HS04-) and sulfate (S〇42-). The stone inverse number refers to the total number of carbon atoms in the molecule. "Coke annoyance" means the mouth containing carbonaceous solids that will not vaporize under the conditions of the method. The version of the coke anion contains 5 lines as measured by mass balance. Coke weight is the total weight of solids minus the total weight of the input catalyst. This is the weight in the substrate (such as crude feed, complete product, or crude product), and is expressed as a weight fraction or weight percentage of the total weight of the substrate. "Wtppm" means parts per million expressed in terms of weight. "Diesel oil" means that the boiling range is distributed at 26 ° at 0.101 MPa. Smoke between radon and 343 C (500-650 ° F). The diesel content is as measured by astm method D2887. "Distillate" refers to hydrocarbons with a boiling range distribution between 纟 2 0c and 3340C (400-650 叩) at 0.1 (Π MPa). The content of the distillate is, for example, ASTM D28 87 Measured. Gu effluent may include kerosene and diesel. DSC refers to differential scanning calorimetry. Freezing point and 'freezing point' refers to the temperature at which crystalline particles form in the liquid. Freezing point is as measured by ASTM 〇2386 40 200535232 GC / MS refers to gas chromatography combined with mass spectrometry. Hard ^ refers to anions as described by Pearson in J⑽gang / 〇 / 山 —π 85, p. 3533. Quantity ratio. H / C refers to the "H / C" as measured by weight percentage, which refers to the atomic hydrogen to atomic carbon weight ASTM method D5291 weight percentage and carbon value. "Heteroatom" refers to a molecule in a hydrocarbon The structure contains oxygen 'nitrogen and / or sulfur. Heteroatom content is determined by AS ™ method E385 for oxygen, D5762 for nitrogen and D4294 for sulfur. Hydrogen source ”means hydrogen and / or Compounds and / or compound groups that react in the presence of the feedstock and catalyst to provide hydrogen to one or more compounds in the crude feed. Sources can include, but are not limited to: hydrocarbons (e.g., to & hydrocarbons, such as methylbenzene, ethylbenzene, propylene, dioxin, pentyl, light oil), water or mixtures thereof. Mass balance is used to Assess the net amount of hydrogen provided to one or more compounds in the crude oil feed. Inorganic salt "means a compound consisting of metal cations and anions." PP "means the Institute of Petroleum, now London, UK The Energy Institute (London, United Kingdom) o Heterobond burning "means branched saturated tobacco.

“Kerosene” means smoke with a boiling range between 204 ° C and 260 C (400-5 00 ° F) at 0.101 MPa. The kerosene content is determined by asTM method D28 87. 41 200535232 " "Lewis acid" refers to a compound or substance that has the ability to accept one or more electrons from another compound. "Lewis base" refers to a compound that has the ability to donate one or more electrons to another compound. And / or substances. "Light hydrocarbons" means hydrocarbons having a carbon number in the range of 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 a composition containing 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. The "micro carbon residue" ("MCR") # 扣 尤 从 和 # 々V j 系 # means the amount of carbon residue left after the material is evaporated and pyrolyzed. The MCR content is as bad as the 你 S such as the ASTM method Tested by D4530.

Teng range is distributed at 38. (: And 1 fe oil content is as measured by ASTM light oil means hydrocarbon component boiling at 204 ° C (100-400 ° F) at 0 · 101 MPa. Method D2887.

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

"_Fe content refers to the content of Nl / V / Fe in the matrix-Fe content is determined as as ™ * d5863." Nm3 / m3 "refers to the standard of" ㈣H 万 木 原 / 由 进 枓 "per cubic meter. Cubic meters of gas < ^ Jiu 丨 Health is deduction of Lewis base and / or cloth tolerance "丁 ％ # 秘" 丨 ~ Bute 'Luo Rui alkaline. The non-delay system refers to A # _ · 1〇1 MPa “positive bond component and / or component mixture at standard temperature and pressure (hereinafter referred to as“ STP ”). Straight-chain) saturated hydrocarbons. “Burning value” refers to the value of 42 200535232 of an internal combustion engine K ^ reference fuel. The anti-knock properties are numerically expressed. The calculated octane number of light oil is determined by ASTM method D6730. '' Means a compound with a non-aromatic carbon-carbon double bond. The species of olefins include but are not limited to: cis, trans, terminal, intramolecular, branched and linear. The Periodic Table "means purely international The periodic table stipulated by the Union of Applied Chemistry (IUPAC) in November 2003. "Polyaromatic compounds refer to compounds containing two or more aromatic rings. Examples of polyaromatic compounds include, but are not limited to: indene, naphthalene, anthracene, phenanthrene, benzothiophene, and dibenzothiophene. ' 'Residue' means a component with a boiling range above 538 ° C (1000 ° F) at 0.101 Mpa, as measured by ASTM method D5307. "Semi-liquid" refers to a material phase that has the properties of the 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 bran, pudding or toothpaste. "SCFB" refers to standard cubic feet 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" refers to Refers to the total number of KOH in milligrams ("mg,") per gram ("g") of the sample. TAN is as measured by ASTM method D664. "TAP" means transient analysis of the product. "TMS" means transition metal sulfide.

"VGO" refers to a composition with a boiling range between 343 ° C and 53.8 ° C (65 0-1000 ° F) at O.ioi MPa. The VGO content is as measured by ASTM 43 200535232 method D2887. In the context of this application, it is understood that if the values obtained for the properties of the composition under test fall outside the limits of the test method, the test method can be recalibrated to test the property. It should be understood that Bu can use other standardized test methods that are tolerated as equivalent to household cats, nicknames, U-sides, and test methods. The product is made and / or obtained, and then stabilized. Crude oil is suspended as solid, semi-solid and / or liquid. Crude oil may contain crude oil. The stabilization effect may include, but is not limited to, the removal of non-condensable gases, water, salts, 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. Stable crude oils have not generally been distilled and / or fractionated in processing facilities to produce multiple components with a specific boiling range distribution (eg, light oil, distillate VGO, and / or lubricating oil). Distillation includes, but is not limited to, the atmospheric distillation crane method and / or the vacuum distillation German method. The undistilled and / or unfractionated stable raw material contains components having a carbon number of 4 or more in an amount of at least 0.5 g of components per gram of crude oil. Examples of stable crude oil include whole crude oil, topped crude oil, desalted crude oil: ¾, desalted crude oil, or a combination thereof. "Extracted member" refers to a crude oil that has been processed so that at least some of its constituents with a boiling point below 35 ° C at 0.11 Mpa have been removed. Typically, topping crude oil is topping crude oil per gram. Contains such ingredients up to 0.1 g, up to 0.05 g, or up to 002 g. Some stabilized crude oils have a stable crude oil that can be transported to a traditional processing facility by a means of transport, such as an official road, truck, or vessel. Nature. The other 44 200535232 crude oils have one or more inappropriate properties that make them inferior. Inferior crudes may be unacceptable for transportation tools and / or processing facilities, thus giving 4 low-grade crudes a very low economy. Value. Economic value may lie in a reservoir that holds inferior crude oil that is tolerated as too expensive in terms of manufacturing, transportation, and / or processing. Inferior crude oil properties may include, but are not limited to: a) a TAN of at least 0.5 b) a viscosity of at least 0.2 Pa.s; c) a specific gravity of at most 19; a total Ni / V / Fe content of at least 0.0001 g Ni / V / Fe per gram of crude oil; e) per gram Crude oil with a total of at least 0.05 mg of heteroatoms Atomic content; f) residue content of at least 0.01 grams per gram of crude oil; g) asphaltene content of at least 004 grams per gram of crude oil; h) MCR of at least 0.02 grams of MCR per gram of crude oil Or a combination of them. In some specific examples, inferior crude oil 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 per gram of inferior crude oil. 9 grams of residue. 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 some specific examples, In an example, inferior crude oil may have a sulfur content of at least 0.0001 grams, at least 0.0005 grams, at least 0.01 grams, or at least 0.02 grams per gram of inferior crude oil. Inferior crude oil may include having a range A mixture of boiling point hydrocarbons. Inferior crude oil may include: at least 0.001 g, at least 0.05 g, or at least 0.01 g. The boiling range is distributed between 200 ° C and 300 ° C at 0.101 MPa. : Hydrocarbons in between; at least 0.001 g, at least 0.05 g, or at least 0.01 g boiling at 0.101 MPa Hydrocarbons distributed between 300 ° C and 400; and at least 0.001 g, at least 0.005 g, or at least 0.0005 200535232 g with a boiling range of 0.10 MPa and 400 ° C. Hydrocarbons or their combinations. In some specific examples, in addition to the higher Forte constituents, inferior crude oil can also include: at least 克, at least 0.005 gram per gram of inferior crude, or To) G.01 grams have a boiling range distribution of at most 0.1 MPa at 0.1 Mpa. Typical hydrocarbon grades are 5, and this inferior crude oil has at most 0.2 g or at most 0.1 per gram of inferior crude oil. Grams of such hydrocarbons. In some specific examples, the low grade crude oil may contain up to 0.9 grams per gram of low grade crude oil or a boiling range distribution of at least 300. "Chemical #. In some specific examples, low-grade crude oil, per gram of low-grade crude oil can also be Z to 0.001 grams of hydrocarbons with a boiling range distribution of at least 6500c. In some specific examples Medium and low grade crude oil can contain up to 19 grams per gram of low grade crude oil or up to 0.99 grams of hydrocarbons with a boiling range between 300 ° C and 丨 〇⑻.c. It can be processed using the methods described herein. Examples of inferior crude oil include, but are not limited to, crude oil obtained from the following countries and regions: Canadian Alberta, Venezuelan Orinoco, Venezuela, Southern California and Alaska North Slope . s〇uthern

Californian and north slope Alaska), Mexico Bay of Campeche, Argentina San Jorge basin, Brazilian Santos and Campos basins, China Netli Bay (China

Bohai Gulf) ’China Karamay, Iraq Zagros, Kazakhstan 46 200535232

Caspian) 'Nlgeria 〇ffsh〇re, Umted Kmgdom North Sea, Northwest Madagascar (thwest), Oman (0man) and Hungarian Baker (Schoonebek) ° Inferior crude oil Processing can enhance the nature of the crude oil, making 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 crude feed can be topping out as described herein. Using the methods described herein, crude oil products obtained from crude feed processing are suitable for transportation and / or refining. The properties of the crude oil product are more than that of the crude oil feed, and the correspondence between West Texas Intermediate (West Texas Int_diate) raw materials and oil: or closer to the Brent crude oil than the crude oil feed. Compared with the economic value of the crude oil feed, the economic value is improved. This type of crude oil product can be refined with little or no pre-treatment, thus improving the efficiency of refining. The previous step may be "+ 1 month" treatment, which may include desulfurization, demetallization, and / or atmospheric distillation to remove impurities from the crude oil product. The method of contacting the crude oil feed according to the present invention is explained here. Specific examples of products of concentrated light oil, coal & diesel and / or VG0: products, which usually cannot be made in the traditional type: raw materials can be sourced with hydrogen in the contact zone and / or in the presence of one or more catalysts Contact in a combination of one or more contact zones. Production can be generated on the spot. On-site production of gas source 200-500 Y / material and inorganic salt catalyst react at a temperature ranging from ^ 00-400. The formation of hydrogen and or light 47 200535232 quality hydrocarbons. 4 The on-site production may include at least a part of the reaction containing inorganic salt catalysts such as metal formate. The complete product usually contains the gas and vapor generated during the contact. , Liquid or a mixture thereof. The complete product comprises a crude product that is a liquid mixture at 纟 sTp, and in some specific examples, and includes non-condensable hydrocarbons at 纟 STP. In some specific examples, the complete product and / or Crude oil products may include solids (e.g., inorganic solids and / or coke). In some embodiments, the 'solids may be entrained in the resulting liquid and / or steam during contact

Out of breath. The W contact zone usually includes multiple parts of a reactor or multiple reactors. Examples of reactors that are contacted in the presence of catalysts are bed reactors, continuous stirred tank reactors, base flow reactors, and liquid / liquid contactor bed reactors and ebullated bed reactors. The reactor, part of the reactor, reacts to feed crude oil with a chlorine source. Includes: stacked bed reactor, stationary (CSTR), spray reactor, live CSTR examples include fluidization

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. Contact temperature range is 200-800 ° C, 300-700. (: Or 400-600 C. In the specific example where the hydrogen source is supplied as a gas (such as hydrogen, methyl or ethyl), the ratio of gas to crude oil feed is usually in the range of 16,100 NmVm3, 2-8000 Nm3 / m3, 3_4_ Nm3 / m3 or 5-3⑻ 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 of them The specific example of adding steam 48 200535232 The ratio of radon steam to crude oil feed is within the range of 0.08 kg per kg of crude oil: 0.03 · 2 · 5 kg 5 goo · 1.1 kg of steam. The flow rate of the crude oil feed may be sufficient to maintain the crude oil feed volume in the contact zone to at least 10%, at least 50%, or at least 90% of the contact volume. Typically, the crude feed volume in the contact zone is 40% of the total volume of the contact zone, 〇 / each " / 〇 〇 02. In one or two specific examples, the contacting may be performed in the presence of an additional gas such as argon, nitrogen, oxane diethane, propane, butane, propylene, butene, or a combination thereof.

雕 —Figure 1 疋 A schematic diagram of an example of a contact system i㈧ used to make a complete product of vapor. The crude feed leaves the crude feed supply source and passes through: V officer 104 enters contact ㊄102. The amount of catalyst used in the contact zone can be 60 grams for each gram of crude oil feed in the contact zone. In some specific examples, a diluent may be added to crude oil processing to reduce the crude oil feed. In some specific examples,

St passes through, _ goes into contact ... at the bottom. At some = before and / or during the delivery of crude oil feed to 1G2; original: the feed is heated to a temperature of at least "or at least ... temperature. Extraordinary. 'The crude oil feed can be heated to ⑽ ·% or 2 The temperature in the dry zone. In some specific examples, the catalyst is combined with the crude oil feed, and then touched: The contact area is 102 towels. The crude oil feed / catalyst mixture can be sent at the same time. Inlet = before heating to a temperature of… or at least 3. ^. To heat the original / from the feed to 200-500 V or 300_400 ℃ / dish. In some specific examples, crude oil feed / Catalyst mixture 49 200535232 is a slurry. Before this θ will be equal to the actual wealth, can be purchased 0 ... = reduced. For example, .... "or can be in the crude oil feed two: degrees When the crude oil feed / catalyst mixture is heated, the formation of alkali metals that form a sulfuric component can remove this acidity from the crude oil feed :: TAN for some metal salts. One _ 丨 generates a knife to reduce crude oil feed. In Jiewangguang 1Λ & Delayed transportation, Bedi added to the contact ... _Zone 102 mixing can be sufficient to suppress the catalyst and crude oil feed / catalyst mixture. Remove at least a part of the catalyst from the contact area worker 02, and in some specific examples, this type of catalyst is regenerated and reused. In this specific example, fresh catalysts can be added to the contact area 102 during the reaction procedure. In some embodiments, the crude oil feed and / or a mixture of the crude oil feed and the inorganic salt catalyst is fed into the contact zone as an emulsion. The emulsion can be obtained 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 remain stable for at least 2 days, at least 4 days, or at least 7 days. Typically, the ' emulsion is stable for 30, 10, 5 or 3 days. Surfactants include, but are not limited to: organic polycarboxylic acids (Tenax 2010;

MeadWestvaco Specialty Product Group; Charleston, South Carolina, U.S.A.), C21 dicarboxylic fatty acid (DIACID 1 550;

MeadWestvaco Specialty Product Group), petroleum lutein (Hostapur SAS 30; Clarient Corporation, Charlotte, North Carolina, U.S.A.), Tergital NP-40 surfactant (Union 50 200535232

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 · τ Baker; Phillipsburg, New Jersey, U.S.A.).

The circulation catheter 106 can connect the catheter 108 and the catheter 104. In some specific examples, the circulation catheter 106 may directly enter and / or exit the contact area ιo2. The tube 10 'may include a flow control valve 1 1 0. The flow control valve 1 1 〇 allows at least a part of the material from the duct! 08 is circulated into the catheter 104 and / or the contact area 102. In some specific examples, a condensation unit may be placed in the conduit 108 to allow at least a portion of the material to be condensed and recycled to the contact zone 102. In some specific examples, the circulation conduit 106 may be a gas circulation line. The flow control valves 11 and 110 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 specific examples', a liquid in a selected volume range over solid f can be maintained in the contact region 1G2. The feed volume in the contact zone 102 can be monitored using standard instruments. The gas injection 0 1 12 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 steam inlet 114 may be used to add steam to the contact zone 102. In some specific examples, the water vapor reaches the contact area 10 02 via the grave gas " Tian Yanfei entrance 1 14. In some specific examples, the complete product of at least _plus \ ^ V is generated as a vapor contact zone 102. In a certain example of 4b, the complete product is steamed and / or milk containing u 馐 containing small amounts of liquids and solids from the top of the contact area 102 and the production area 116. Can be changed. The steam is transported through the conduit 108 to the sub-51, the contact area of 20052005232] 02 hydrogen source for crude oil feed II [and / or the willingness in the contact area to control the scoop from the top of the contact area 102. W Radon and / or liquid phase. In one or two specific examples, the tomb generated from the top of the contact area] 0 W Original: The feed contains at least. +5 grams, at least. .8 grams, at least • 7 grams of crude product. In some specific examples, the vapor generated from contacting m 4 is a gram of crude oil product per gram of crude oil. +. ".8- " 9 grams or .. " .98 catalysts and / or solids of the materials can be left in the contact area 102 as a by-product of the contact process. The solid other / {田 、 风 川 ό and / Or used catalyst may contain residual crude oil feed

And / or coke. T eight on the knife / 116 days away, using standard separation techniques to cool the steam and separate it into crude oil products and gases. The crude product leaves the separation unit 116, and then enters the crude product receiver 119 via the conduit 118. The resulting crude oil product: suitable for transportation and / or processing. The crude product receiver m may include: or a plurality of pipelines, one or more storage units, one or more transport containers, or a combination of knives. Name: _ ij: ka / ^ In the case of Erbalian K, the separated gas (for example ^ anaerobic carbon monoxide, hydrogen sulfide or methane) is transported to other W-(for example, for use in fuel cells or sulfur recovery equipment ) And / or the guide Lv 12〇cyclic & to the contact area 102. In some embodiments, standard physical separation methods (such as filtration, centrifugation, or membrane separation) can be used to remove solids and / or liquids entrained in the crude product. Figure 2 depicts a contact system 122 for processing crude oil feeds 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. The crude oil feed can enter the contact zone via the conduit 104! 02 52 200535232 In some specific examples, the crude oil feed is received from a crude feed supply source, 'taste 104, which may include a gas inlet 1 12. In some specific examples, the air limb inlet 11 12 can directly enter the contact area 102. In some embodiments, the steam inlet 114 can be used to add steam to the contact zone 102. The crude feed can be contacted with the catalyst in the contact zone 102 to produce the complete product. In some specific examples, the 'duct 106' allows at least a portion of the complete product to be recycled to the contact zone 102. "The mixture comprising the complete product and / or solid and / or unreacted crude feed leaves contact g 102 and enters the separation via conduit 108," 24. *-In some specific examples, a "condensing unit" (for example, placed in s 06) so that at least-part of the mixture in the guide can be condensed and recycled to the contact zone 1 () 2 for incoming-step defense . In some embodiments, the loop duct 106 may be a gas circulation line. In some specific examples, lead 108 may include a filter to remove particles from the complete product. 124 towels in the separation zone. At least a portion of the crude oil production I can be separated from the complete production and / or catalyst. Specific examples of including solids in complete products "Separate solids from complete products using standard solids separation techniques (such as centrifugation, filtration, decantation, tree separation). For example, solid catalysts, used catalysts And / or a combination of coke. In some of them, a part of the gas system is separated from the complete product. In some == j, at least part of the complete product and / or solid can be introduced into the HM, and / or in— In some specific examples, it is through the contact area 1.2. For example, the cyclic part can be in contact with the original: to the back ... for advanced processing. Crude oil production leaves the separation area 124 by the pipe 128. The bismuth is edged Guided by some specific real money, crude oil products 53 200535232 can be transported to the crude oil product receivers. In some specific realities, & one less than one of the eight kings or crude oil products can be included to σ knife, catalyst . Entrainment in the complete product and / or use of standard gas / liquid product gas for separation.-'Special membrane knife and pressure reduction, ... In some specific examples, the separated gas is transported. Dry other processing units or ~ 6 "People, ',,, shaking cell, a sulfur recovery device, & dagger's Group 5) and / or recycled to contacting zone. Some specific examples, at least one

Separation of the crude oil feed in the original, and whoever ancestor 4 was carried out before the plant entered the contact zone. Figure 3 The combination of β-eight μ I-t systems and Hu Fen 仞 _ 立 w α 3 疋 刀 离 区 and contact system h, Yue Xuan see examples are not intended. Contact 糸 n! Contact 糸, first 1 30 may be contact system 100 and / or contact system 122 (shown in the picture! And 2 of them). Crude oil feed enters separation zone 132 via ¥ 104. Separation technology separates at least-part ㈣ £ £ 132 + crude oil feed using a standard centrifugal knife to make separated crude oil

Two hydrocarbons. The separated crude oil feed, in some specific examples, has a distribution of at least ⑽. C. Mixing of at least 12 () γ components. Or in some specific examples, the system contains a typical Ford range distribution of at least C, and the separated crude oil feed contains a boiling range distribution at 10 (M000 ° C, 120-900 ° C < 200-800 ° The warp series separated by the component mixture from the crude oil feed leaves the separation zone through the conduit m and is transported to other processing units, processing facilities, storage facilities, or a combination thereof. At least a part of the separated crude oil feed leaves the separation. Zone 1 enters the contact system 30 through the channel 1 36 to be further processed to form a crude oil product, which leaves the contact system 13 () via the conduit 138. 54 200535232

: In one or two specific examples, by any of the methods described herein from crude oil into the clothing: The crude oil product 'is the same as or different from a crude oil feed: Crude oil: Participate. For example, "the crude oil product may be different from crude oil having different viscosities:" to produce a blended product having a viscosity between the viscosity of the crude oil product and the viscosity of the crude oil. The resulting push product may be suitable for transportation and / or handling. Fig. 4 shows specific examples of the combination of the transfer zone 140 and the coupling system 13Q M. In some specific examples, at least part of the crude oil product leaves the contact system 13 through the guide 8 and enters the blending zone 14. In the blending zone: :: a small portion of the crude product is combined with one or more processing units (such as hydrocarbon streams or light oils made from " or multiple crude feeds), crude oil, raw materials: Manufacture blended products. Processing stream, crude oil = 'crude oil or its mixture is sent directly to the blending zone or upstream of the blending zone via: 142. The mixing system can be located near the blending zone. Blended products can meet specific product specifications. Specific product specifications: Not limited to:-Range or limit of ApI specific gravity, TAN, viscosity or

combination. The seeded product leaves the change-over area 140 via the guide # 144 and is broken and / or processed. The specific example of the production of 'methanol is that the catalyst is used during the contact process. For example, hydrogen and carbon monoxide can react to form methanol. The recovered methanol ° contains dissolved salts such as potassium hydroxide. The methanol at this time can be combined with an additional crude oil feed to form a crude oil feed / methanol mixture. The methanol is plated with alcohol 0 to 5 and the viscosity of the crude oil feed is easily reduced. Feed crude oil / A. Heating of up to 500 ° C can reduce the TAN of the crude feed to less than one. -55 200535232 Figure 5 is a schematic illustration of a specific example of a combination of a separation zone, a contact system, and a blending zone. The crude oil feed enters the separation zone 132 via a conduit 104. The raw materials and feedstocks are separated as described above to form separate crude oil feeds. The separate scoop of crude oil feed enters the contact system 30 via conduit 1 36. The crude product exits the actinide system, first 1 30 and enters the blending zone 140 via the conduit 1 38. In blending, other processing streams and / or crude oil fed through conduit 142 are combined with the crude product to form a blended product. The blended product leaves the breeding zone mo via the conduit 144.

θ 6 is a schematic diagram of the heavy contact system 46. The contact system 1 00 (= U can be placed before the contact system 148. In the alternative embodiment, the position preceded by ° m is interchanged. The contact system 1 00 includes an inorganic salt catalyst. The contact system 148 may include-or multiple catalyst The medium in the contact system 148 may be an additional inorganic salt catalyst, a transition metal sulfide catalyst, a commercially available medium, or a mixture thereof. The crude oil feed is introduced into the contact system 100 through a conduit 104, and then the Contact in the presence of an inorganic salt catalyst to produce a complete product. The complete product contains hydrogen, in a

Your specific implementation example also contains the original; product. The complete product can be obtained by m7 Λ.仏 J ,,, and E e 108 leave the contact system 100. The contact between the inorganic salt catalyst and the crude oil feed AA #, and the lice produced by the contact can be used as the source of the contact system 1 4 8. At least one of the lice produced by at least one octahedron was transferred from the contact system 100 to the contact system 148 via the catheter 150. In an alternative specific example, Jiang Shi θ ^ you have separated and / or processed the hydrogen produced by Shifang, and then transmitted it through the conduit 50 to contact the system 148. In some cases, the contact system ^ 48 may be a part of the contact system, the contact system, and the charge 100, so that the generated hydrogen can be obtained directly from the contact system 10 / the contact system 148. In some specific examples, the steam stream made from the ytterbium and 100 which is connected to the contact system 148 is directly mixed with the crude oil feed. The second crude oil feed was ordered by the contact system i48, and Xidun 152 entered the contact system 1 仏. The contact with the catalyst yields the hydrogen produced by a futai t ^ trowel and a niche block. The product is here a full product. The product was completed via · = —common order .. H. Guide 154 left the contact system 148. T A system including a contact system, a contact zone, a sub-shaft & and / or a blending zone. As shown in Figure U, it can be located near or in the vicinity of Zhizhu's manufacturing of crude oil feed. Germany, π the place of transformation. After processing through the catalyst system, the crude oil feed may be considered suitable for transportation and / or use in a refining process. In some specific examples, refining and / or processing products of transportation and / or conversion products, crude oil products and / or blended products can be processed. Product listings such as transportation fuels, heating fuels, lubricants Or chemical processing may include steaming and / or fractionating crude oil products and / or blended products to make one or more German deities. —, Lanthanum knife In some specific examples, the crude oil product, the blended product and / or one or more cranes can be added with nitrogen. In some specific examples, the complete product is at least 0.05 g, at most 0.03 g, or at most 0.01 g of coke per gram of the complete product. In some cases, the products of King 70 are consistently free of coke (ie, coke is undetectable). In some specific examples, the crude oil product may include at most 0.05 grams, at most 0.03 grams, at most 0.01 grams, at most 005 grams, or at most 0.003 grams of coke per gram of crude oil product. In some specific examples, the crude oil product has a range from above 0 to 5,000, 00001-003 grams, 0.0001-0.01 grams, or 0.001-0.005 grams per gram of crude oil products. The coke content, or 57 200535232 is undetectable. In certain specific examples, the crude oil product has a mcr content of up to 90%, up to 80%, up to 50%, up to 30%, or up to a runoff content of the crude feed mcr content. In some specific examples, the crude product has a negligible MCCR content. In the case of * —this presentation / § # ^ 1 »-Octahedral households, for example, crude oil products contain at most 0.05 grams, at most 0.003 grams, at most 0.01 grams, or at most 0.00 grams per gram of crude oil products. body. Typically, the ' crude oil product contains MCR from 0 g to 0.04 g, 0.0001 to 003 g, or 100,000 g per gram of crude oil product. In some specific examples, the complete product contains a non-condensable gas. Non-condensable gases usually include, but are not limited to, carbon dioxide, ammonia, hydrogen sulfide, hydrogen, oxygen oxides, methyl alcohol, and other non-condensable hydrocarbons or their mixtures. In certain embodiments, hydrogen, carbon dioxide, carbon monoxide, or a combination thereof 'may be formed on the spot via contact of steam and light hydrocarbons with an inorganic salt catalyst. Typically, 'the molar ratio of carbon monoxide to carbon dioxide is 0.07 under thermodynamic conditions. In some specific examples, the molar ratio of carbon monoxide produced to carbon dioxide produced is at least, 0.3, at least, 0.05, or = 0.7. In some specific examples, the molar ratio of the carbon monoxide produced to the carbon dioxide produced is 0.M.O. Or within the range of 〇5 〇8. The ability to generate CO2 over CO2 on-site 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 200535232 In some specific examples, such as Tai-the complete product produced can be mixed with a compound with a boiling range between -10 ° C and 53 π w τ package c. The mixture can contain carbon number 1 To 4 rw. Thing. ^ + Hydrocarbons in dry enclosure. The mixture # per gram of this mixture may contain 0 Λ system · υ〇Κ〇 · 8 grams, 〇〇〇 03_〇 〇005. 0-0. 1 g of C4 hydrocarbons. The Br4 group or the group is 0.001-0.8 g per gram of c4 hydrocarbons, 0.003-0.1 g or 0 Λ, and each-. 〇5-0. 01 g of butadiene. In some specific examples, isoparaffin is at most

Up to township U, at most 0.8, at most 03, or at most 1% of the denier ratio is obtained. In some specific examples, the hetero-chain burned hydrocarbons are relative to (... Weight in the range of 0.001_〇1: obtained. Paraffin may include isoparaffin and / or normal chain hydrocarbon.

In some embodiments, the complete product and / or crude product may contain olefins and / or paraffins in proportions or amounts not normally found in crude oils produced and / or retorted from the product. This olefin contains a mixture of olefin thin smoke with terminal double bonds ") and olefins with intramolecular double bonds. In some specific examples, the 'lean hydrocarbon content of the crude oil product is greater than the olefin content of the crude oil feed2, Factors of 10, 50, 100, or at least 200. In some specific examples, the dilute hydrocarbon content of the crude product is a factor that is greater than the olefin content of the crude feed by up to 1,000, up to 500, up to 300, or up to 250. In some specific examples, the furnace with a boiling range in the range of 20-400 # 1 has hydrocarbons in the boiling range of 20-400 ° C per gram in the range of 0.0000K 0.1 g, 0.0001-0.05 g, or 0.004 g In some specific examples, at least 0 001 grams, at least 0.005 grams, or at least 0.01 grams of alpha olefins can be produced per gram of crude oil product. In some specific examples 59 200535232 cases, the crude oil product is per gram. The crude product contains 0.5 g, 0.5 g, 0.001-0.2 g, or 0.01-0.1 g of hydrocarbons. In some specific examples, the boiling range is between 20-400. (: Hydrocarbons between Hydrocarbons distributed between 20-400 ° C per gram of boiling range Α-olefin content in the range of 0.001-0.08 grams, 0.001-0.05 grams, or 0.01-0. 04 grams. In some specific examples, the boiling range is distributed between 20-40. The hydrocarbons have a weight ratio of alpha olefins to intramolecular double-bonded olefins of at least 0.7, at least 0.8, at least 009, at least 10, at least 1.4, or at least 1.5. In some specific examples, the boiling range is distributed at 20%. Hydrocarbons between _2〇4 have a weight ratio of alpha olefins to intramolecular double-bonded olefins in the range of 0.7-10, 0.8-5, 0.9-3, or 1-2. Crude oil and commercially available products The weight ratio of intramolecular double bond dilute hydrocarbons is usually $ Λ Λ. Lt is suspended for two to five days. 5. To manufacture a thin-leaf furnace that increases the amount of fine smoke with intramolecular double bonds—p »Ping ^ This force can help convert crude oil products into commercially available products. In some specific examples, contacting the crude oil feed with a chlorine source in the presence of an inorganic salt catalyst can produce a boiling range distribution that includes linear olefins. Hydrocarbons between 20-4. The linear olefin has cis and trans double bonds. The linear olefins with trans double bonds have cis double bonds The weight ratio of linear olefins with octadecane bonds is at most 0.4, at most 1.0, or at most 14. Production of alpha α • In some specific examples, linear olefins with trans double bonds versus cis filaments + The weight ratio of the linear olefins of 〆, Λ and 键 is in the range of 0.001-1.4, 0.01-1.0, or 01_0 4. In some specific examples, the boiling range is distributed in the range of 20-204. (: Between the range The hydrocarbons have at least 0.1 g, at least 0 g per gram of boiling hydrocarbons distributed in the range of 20-400 with Bafan Qiu Tenggan around, and a main ^ 0.15 g, at least 0.2 0 grams or at least 60 200535232 0.30 grams of normal paraffin content. The normal paraffin content of such hydrocarbons may be in the range of 0. 0 (Η-0.9 grams, grams, or 0.2-0.5 grams per gram of hydrocarbons. In some specific examples, such hydrocarbons With a weight ratio of isoparaffins to normal paraffins of at most 15, at most 14, at most 0.8, at most 0.8 or at most 0.3. From the content of normal paraffins in such hydrocarbons, the normal paraffin content of crude oil products can be estimated Is in the range of 0.001-0.9 grams, 0.001-0.8 grams, or 0.001-0.5 grams per gram of crude product. In some specific examples, the crude product has a Ni / v / Fe feed for the crude oil. The total content of Nl / V / Fe is at most 5G%, at most 5%, at most 5%, or at most. In some specific examples, the crude oil product contains at most 0.0001 g, at most i χ per gram of crude oil product. 5 g or up to 1 X Η) -6 g of Nl / V / Fe. In certain specific examples, the crude oil product has between 1 X 10-7 grams to 5 X 10.5 grams, 3 x 10-7 grams to 10 grams, or 1 X 10 grams to 1 xi per gram of crude product. Total content in the range of 0-5 grams.

In some specific examples, the crude oil product has a TAN that is a crude oil feed; at most 90%, at most 50%, or at most 10%. In certain specific examples, the crude product may have a TAN of at most i, at most G5, at most qi, or at most 0.05. In some specific examples, the tan of the crude product may range from 0.001 to 0.5, 0.01 to 0.2, or 0.05 to 0.001. In some specific examples, the Aρ specific gravity of crude oil products is at least 10%, at least 50%, or at least 90% higher than the nanospecific gravity of crude oil soil. In some specific examples, the Aρ specific gravity of crude oil products is between , 15_3, or 16-20. 61 200535232 In some specific examples, the content of the child is at most 70% and at most. In some specific examples, at least 10% of the sub-content, at least the amount of crude oil product has a total heteroatom of 50% or up to 30% of the total heteroatom of the crude oil feed. 40% or at least 60% of the total heteroatom-containing crude oil products may have up to 90%, up to 70%, or up to 60% of the sulfur content of the crude feed feed. The sulfur content of crude oil products is G.G2 grams per gram of ancient U.sub.4, at most G._ grams, at most 0.005 grams, at most 0.004 years old, and empty Λ ΛΛ. Taxi 1 to 3.03 g or up to 0.001 g. In a specific example, the crude oil product has a sulfur content in the range of 0.000 to 0.02 g or 0.005-0. (H g. Θ) In some specific examples, the crude product may have a crude oil content. The feed nitrogen content is at most 90% or at most 80% s Yichuan / lice contains $. The nitrogen content of crude oil products, based on per gram of crude oil product, can be 吝 J to 0.004 grams at most, at most 0.003 grams or 0.001 grams to the night. In this case, the crude oil product has a value of 0.0001 grams per gram of crude oil product to 0.005 grams per gram of crude oil product. Nitrogen content in the range of 0.003 grams. 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 oil products. Is at most U, at most 1.7, at most 丨. 6, at most 丨 5 or at most 丨 4. In some specific examples, the H / C of the crude product is 80-12% or 90-m% of the crude feed H / C In other specific examples, the crude oil production ㈣h / c is 100-120% of the crude oil feed Η / C. The crude oil product H / C within the crude oil feed h / c _㈣ represents the hydrogen in the process. absorb 0 or 0 crude oil product with a minimum of 62 200535232 contains components with a range of boiling points. In some specific examples, the crude oil product contains: at least 0.001 grams or from 0.001 to 0.5 grams at a boiling range distribution of 0.101 MPa as Hydrocarbons up to 200 or up to 204 ° C; at least 0.001 g or from 0.001 to 0.5 g hydrocarbons with a boiling range between 200 ° C and 300 ° C at 0101 MPa; at least 0.001 g or From 0.001 to 0.5 g of hydrocarbons with a boiling range between 300 ° C and 400 OC at 0.101 MPa; and at least 0.001 g or from 0.0001 to 0.5 g Hydrocarbons with a boiling range of 0.100 MPa and 538 ℃ at 0.101 MPa. In some specific examples, the 'crude oil product has $ • 0001-0.2 g, 0.0001-0' g per gram of crude oil product. Or 0.00005 grams of light oil content. In some specific examples, the crude product contains 0.0001.02 grams or 001_00 grams of light oil. In some specific examples, the light oil contains per gram of light oil. Olefins of up to 3.05 g, up to .1 g, or up to 0.05 g. In some specific examples, the crude oil product is per gram of crude oil 00001_015 containing 0 g,

: · 0000 · 0.1 g or 0.001-0.05 g of a dilute hydrocarbon. In some specific examples, the 2 series has a benzene content of at most (UH grams, at most 5 grams, or 2 grams per gram of light oil. In some specific examples, the light oil has 5 or 1 × 10-7 grams to lxl0-2 g, 1x10.6 g to ΐχΐ0.5 g,

May be benzene content in the range of two grams to lxl0 · 4 grams. Compositions containing benzene do not require special treatment. ~ Lower sulfonium-containing W In certain embodiments, the 'light oil' may contain aromatic compounds. 63 200535232 Compounds may include monocyclic cyclic compounds and / or polycyclic cyclic compounds. Monocyclic% compounds may include, but are not limited to: benzene, toluene, o-xylene, m-dimethyl-p-methyl-benzyl, 1-ethyl-3-methylbenzene; 1-ethyl-2-methyl Benzene; 1,2,3-Trimethylbenzene; 丨, 3,5_Trimethylbenzene; 丨 methyl_3 • propylbenzene; 丨 methyl-2-propylbenzyl; ethyl " , 2-dimethylbenzene; 2-ethyl-2,4-difluorenylbenzene; 1,2,3,4-tetramethylbenzyl; ethyl, pentylmethylbenzene; 2,4,5,6_ methylbenzyl-diisopropyl-o-xylene; substituted homologues of benzene, toluene, o-xylene, m-benzyl, p-xylene or mixtures thereof. Monocyclic aromatic

Chemical compounds are used in a variety of commercially available products and / or sold as separate ingredients. Crude products produced as described herein generally have an increased monocyclic aromatic content. In some specific examples, the crude oil product has a toluene content of 0.001 0.2 g, 0.05-5 0 g, or 0.001 g per gram of crude product. The original product has 0.001 g per gram of crude oil product, and

The content of m-xylene of 0.05 g 0.08 g. Crude oil products are 0.00 g 0.2 g, 0.005-0 per gram of crude oil product; [g or 〇001_〇 05 grams of o-xylene I. The crude oil product has a p-xylene content of 0.0001-0.09 g or 0.0001-0.06 g per gram of crude product. Increasing the content of aromatic compounds in light oil tends to increase the statistical value of the light oil. Crude oil can be evaluated based on an estimate of the crude's gasoline potential. Steam: Can include but is not limited to the calculated scorch value for the light oil portion of crude oil. 0: often has a calculated scorch value within the 35-60 range chart. The completeness of gasoline: To reduce the scorch value of fuel oil, in the example, the crude oil product contains light oil with an octane number of at least 60, at least 70, at least: 64 200535232 or 90 .丄 In the 60-99, 7 (K98 $ μ QS) type, the octane number of light oil is in the range of 98 or 80-95. In some specific examples, the total aromatic content in the phase, the original, // /: The total light oil and kerosene and .c hydrocarbons in the crude oil feed are distributed at a boiling range of 204 ° c, ~ tanker oil and kerosene,) has a high ~ square compound content, and high ^. Main v 5%, at least 10%, at least 50 / or to 乂 99%. Typically, the total compound content of total light oil and kerosene in the crude oil product is higher than that of crude oil into the upper middle, middle, middle and upper reaches. Total Aromatization of Heart Oil and Kerosene

5 things ... 8%, 20%, 75% or 100%. In some specific examples, the kerosene bath, and the sclerophylla— > Benzobismuth-t oil may have a total kerosene η I oil in a mother gram of 5 g, 0.002 Total polyaromatics content in grams or 0.001-0.11 grams. The crude oil product has two grammes per gram of crude oil product, including 0.00000-0.09 grams, 0.5-grams, 0.1-0.3 grams, or 0.011.02 grams. -In some specific examples, the weight ratio of kerosene to diesel in the remaining effluent is

/ To 4: 1, 1: 3 to 3: 1, or 2: 5 to 5: 2. In some specific examples, the 'crude oil product' is a parent gram of crude oil product containing up to 1 g of coal, from 0 to 0.7 g, 0.001-0.5 g, or 0.1 g of kerosene. In certain embodiments, the 'crude oil product contains 0.001-0.5 g. 〇1-0.3 g of kerosene. In this specific example of the presenter, kerosene is per gram of coal: "0.2 grams, at least 0.3 grams, or at least 0.4 grams of aromatic compounds II: In some specific examples, 'kerosene It has an aromatic compound content per gram of kerosene in the range of 01_05 or 0.2-0.4 grams. In some specific examples, the freezing point of kerosene can be below -30. 匚, · 65 200535232 40 ° C. or ^ -50. Wide, below 50 ° C. The increase in the aromatic content of the kerosene portion of crude oil products tends to increase the density of the kerosene portion of the crude product and lower the freezing point. & ^ ^ j-seed kerosene D 卩 has a south density and low solidification point refined to manufacture and jealous ancient-life rt / 豕, from the fuel of the house machine. "... degree and low freezing point properties of aviation turbines in some specific In the example, the crude oil product refers to the diesel content per gram of crude oil or a range from one gram of crude oil. In the dibody example, the diesel system has an aromatic compound content of at least 0.01 g, at least 0, two, or at least ^ g per gram of diesel. In some specific examples, apple oil-based master diesel has an aromatic compound content of 0,5 g, 0,3 g, or 0,2. Brother-in-law In some specific examples, the crude oil product has a range of 0.0001-0 g " palladium · gram, 0 · 001_0 · 8 grams per gram of crude oil product or θ in the range of 0.1-0.3 grams per gram of crude oil product. . In some specific examples, the VGO content in the crude oil product ranges from 0.4 to 0.9 g or 0.6 to 0.8 g. In some specific examples, the ηα VGO system has an aromatic compound content per gram VG0 in the range of 0.001%, 0.8%, or 0.5 to 0.6 grams. In some specific examples, the crude oil product has a crude oil feed of up to 70% ^ ^, OO / s ^ Tti main eve, Cha Badan 50%, up to 30%, up to 10% or to the township. In some specific examples, the crude oil product is at most 0.1 grams, at most 0.05 grams, at most 03 grams, at most 0.001 gram, at most 0.005 grams, or at most 0.005 grams per gram of crude oil product. Residual content in grams. In the case of “one body”, the crude oil product is per gram of crude oil product and there are 0.00000 Π 1. Η ^ ^, • gram, 0.00001-0.05 gram, 0.0000-0.05 gram or 0.0005- 66 200535232 A content in the range of 0. 04 grams. In some specific examples, 'crude oil product medium. The isomorphic body f κ to 〆. The P knife touches ... In the' crude oil product, each gram of crude oil product contains More than 0 grams but less than 0.001 grams, 100,000 ounces of palladium. 勰 λ Gan_ υι gram or 0.0000 gram-0.0000 gram of catalyst. The catalyst can be used in transportation and / or stabilization of crude oil production. Touching π…-helps during the processing of… .., can inhibit rot #, inhibit friction, and / or increase the water separation ability of catty oil products. 可 # 白白It is said that the crude oil product containing at least a portion of the catalyst is further processed to produce lubricants and / or other commercially available products.

It is used to process crude oil in the presence of a hydrogen source. The catalyst can be a 7-inch Λ table ^ all the catalysts of all products. The catalyst used in this application may be a kind of catalyst that is converted into a catalyst in the contact area. The catalyst used to make crude oil feed blood ft '/ δ I' / 'λΙ- λ helps the crude oil feed molecular weight = contact to make the complete product can be reduced by shaking the knife. Without wishing to be bound by theory, catalysts and hydrogen

',' And cocoa, '. Workable ingredients (Louis base or Brewster's Rory base) and T-experimental ingredients in the catalyst to reduce the molecular weight of the components in the crude oil feed. May have a Lewis base and / or a Bronister-Rory 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 purpose, the weight of the transition metal sulfide in the TMs catalyst is determined by adding the total reset 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 0.2 to 20, 0.05 to 10, or 5. Examples of transition metal sulfides can be found in "Inorganic Sulfur 67 200535232" by G. Nickless; ("Inorganic Sulfur chemistry"; 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 grams, at least 0.5 grams, at least 0.8 grams, or at least 0.99 grams. In some specific examples, the TMS catalyst system has a total content of one or more transition metal sulfides per gram of catalyst ranging from 0.4 to 0.999 grams, 0.5 to 0.9 grams, or 0.6 to 0.8 grams.

TMS catalysts contain one or more transition metal sulfides. Examples of transition metal sulfides include: pyrite (Fe45Ni45S8), pyrite (Fe6.75Ni2.25Sn), galanthite, tetra = pyrite (Fe0.0575N1025S〇9), Yinlu Pyrite (AgFe6Ni2S8), Isometric Cuban Mine (CuFe2S3) 'Isometric chalcopyrite, brocade only (0.95 e0 05 S), limonite steel ore, pyrite tin ore (Cu6FeSn2s8)' Pyrite silver ore (), yellow steel ore ^), P member stone iron (F e S) 'pyrite (f gj)

,, magnetic iron ore (Fe (1.x) S (X = 〇 to 〇 · 17)), hethionite (Ni s, Qi Shiji 仏, Sichuan 382) or galena (NiS2) In some specific examples, the MS catalyst includes one or more transition metal stone knives L 4 daggers with a combination of alkali metals, earth metals, zinc, zinc compounds, or their compounds. In the case of r-octagonal Λ, the TMS catalyst is based on the general chemical formula

Ac [MflS6] d, where A 矣 -Shangrenrenyang, Manchurian, Alkaline earth metal or zinc; M represents a transition metal selected from the same L ^ side 1 of the periodic table, and S is sulfur . The atomic ratio of α is in the range of 0 5 $ 9 ς, 2 ... to 2.5 or 1 to 2. The atomic ratio of d "is in the range of 0.0001 to i, 〇10.8, or 0.3 to 0.5. 68 200535232 In some specific examples, the transition metal is iron. In one example, the TMS catalyst may include Commonly known alkali gold or I pallidum / transition metal sulfides (such as limonite (K3F ^ S14), Pyrite (K3F ^ S14), Pyrite (KF), aFei9Cu4NiS26Cl), Chlorothiopite Ore (6 "e24CnG 2s26 lC1.7) and / or ferrierite (Nπ ~ 85 · (Η2〇) 2). In an example of the S body, the ™ S angle media contains limonite potassium ore prepared on the spot The limonite potassium ore produced by the livestock farm can be called artificial limonite potassium ore. Natural and / or artificial limonite bell ore can be used as a medium in the method described herein. In two specific examples, TMS catalysts can be used for every 100 grams of TMS catalysts: carrier materials up to 25 grams, up to 15 grams, or up to 1 gram. Dianli. TMS catalysts contain 0 to 100 grams of TMs catalyst per 100 grams. 25 g, 0 · 00001 1 20 g, 0.0001 g to 10 g of carrier material. Examples of carrier materials that can be used with TMS catalysts include refractory oxides, porous carbon

Material 'Fir stone or its conjugate. In some specific examples, the TMS catalyst is consistently free or free of carrier material. The sintering medium of metal, alkaline earth metal, zinc, zinc compounds or mixtures thereof may have one or more transition metal sulfides, bimetal alkali metal transition metals, high-valent transition metal sulfides, transition metal oxides, or Mixtures, such as those measured by Ai and X-ray diffraction. Part of the TMS contact metal test, trowel test metal test, zinc test, and / or transition metal test & chemical test In the example, it exists as an amorphous composition that cannot be estimated by the X-ray diffraction technique. 69 200535232 In some specific examples, the crystal grains of the TMS catalyst and / or the mixture of the crystal grains of the TMS catalyst have at most 10%. 8 A, up to 103 A, up to 100 A, or up to 40 A. In general practice, the particle size of TMS catalyst grains is usually at least 1 ο A. Including metal test, earth test metal, zinc, A TMS catalyst of a compound or a mixture 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 column 1-2 metal carbonate, and column 1-2 metal oxalate , Brother 1-2 put metal vinegar Salt, zinc carbonate, acetic acid, zinc oxalate, or a mixture thereof to prepare a wet paste. The wet paste can be dried at a temperature of 150-250 ° C or 150-250 ° C to form a transition Metal oxide / salt mixture. The transition metal oxide / salt mixture can be calcined at a temperature ranging from 0 ° C, 500-800, or 600-700 to form a transition metal oxide metal salt mixture. The transition metal The oxide metal salt mixture can react with hydrogen to form a reduced intermediate solid. The addition of hydrogen can be carried out at a flow rate sufficient to provide excess hydrogen to the transition metal oxide metal salt mixture. It can be performed over a period of 10-50 hours or 20-40 hours Hydrogen is added to the transition metal oxide metal salt mixture to produce a reduced, 50-400 ° C or 100-

J. The force passed through the 40-mesh screen. The original intermediate was solid. Hydrogen can be added at 3 5-5 0 0. C, 300 ° C temperature and 10_15 MPa, ιΐ-14 200535232 The reduced intermediate solid can be added to the heat (eg, ^ λα ^ 100c) diluent / elemental sulfur and / t :: in a mixture of one or more compounds. The diluent may include any suitable diluent that provides a gamma domain approach. Dilution shots include a boiling range distribution of at least, at least 15 and less than _. ^ At least. c solvent. Usually the diluent has 100-500c, i50_ willow. C or 200-then the boiling range distribution between V. In some specific examples, the diluent is VGO and / or dimethylbenzyl. Sulfur compounds include, but are not limited to, sulfur lice and / or thiols. The amount of sulfur and / or sulfur compounds is based on the molar number of the Wth metal or zinc in all salts or zinc salts in column B2, and the range can be from i-HH) mol%, 2-80mol Ear%, 5-50 mole%, 10-30 mole%. After the reduced intermediate solids are added to the diluent / elemental sulfur mixture, the resulting mixture can be heated incrementally to 2000-500%, 250,000-45%, or 300, (). 〇: The final temperature, and maintained at least at this final temperature! " inch to eve 2 small inches or at least 10 hours. Typically, the final temperature is maintained for 5 hours, 1 G hours, 5 hours, or 15 hours. After heating to the elevated vulcanization reaction temperature, the diluent / catalyst mixture can be cooled to 0-100 C, 30-90. (: Or a temperature in the range of 50-80 ° c to help recover the catalyst from the mixture. Using standard techniques, the sulfurized catalyst can be isolated from the diluent in an oxygen-free atmosphere, and then at least _ part of a low boiling point solvent (Such as pentane, heptane, or hexane) to produce butane Ms catalysts. Standard TMS catalysts can be pulverized using standard techniques. In some specific examples, the catalysts are inorganic salt catalysts. Inorganic salt catalysts IW ions of the media include inorganic compounds, organic compounds, or mixtures thereof. Inorganic 200535232 Salt catalysts include metal carbonate, metal hydroxide, metal hydride, metal amine, metal sulfide, and metal acetate. , Test metal oxalate, test metal osmate, test metal pyruvate, test metal carbonate, test metal hydroxide, test metal hydride, test metal amine, test metal sulfide, Test metal acetate, test metal oxalate, test metal formate, alkaline earth metal pyruvate or mixtures thereof. Inorganic salt catalysts include, but are not limited to, mixtures of the following: NaOH / RbOH / CsOH; KOH / RbOH / C sOH; NaOH / KOH / RbOH; NaOH / KOH / CsOH; K2C03 / Rb2C03 / Cs2C03; Na20 / K20 / K2C03; NaHC03 / KHC03 / Rb2C03; LiHC03 / KHC03 / Rb2C03; a mixture with K2C03 / Rb2C03 / C / CsOH; K2C03 / CaC03; K2C03 / MgC03; Cs2C03 / CaC03; Cs2C03 / Ca0; Na2C03 / Ca (0H) 2; KH / CsC03; KOCHO / CaO; Cs0CH0 / CaC03; CsOCHO / Ca (OCHOK2) / Rb20; K2C03 / CaC03 / Rb2C03; K2C03 / CaC03 / Cs2C03; K2C03 / MgC03 / Rb2C03; K2C03 / MgC03 / Cs2C03; or some specific examples of Ca (OH) mixed with K2C03 / Rb2C03 / Cs2C0 ^. Inorganic salt catalysts contain up to 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 are per gram of inorganic salt catalyst. The medium contains lithium from 0 g but less than 0.01 g, 0.00000-001 g, or 0.00001-0.0001 g, based on the weight of lithium. In some specific examples, the inorganic salt catalyst includes a Or more alkali metal salts containing at least 11 of the original 200535232 subsequence. In some specific examples, when the inorganic salt catalyst contains two or more alkali metals, the atomic ratio of the alkali metal having an atomic order of at least 1 j to the alkali metal having an atomic order greater than 11 is in the range of 0.1 to 10. · In the range of 2 to 6 or 0.3 to 4. For example, inorganic salt catalysts can include sodium, potassium, and osmium salts, where the ratio of sodium to potassium is in the range of 0.16; the ratio of sodium to sodium is in the range of 0.1_6; The ratio of Gamma is in the range of 0.1 to 1-6. In another embodiment, 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 0.01 to 4. In some specific examples, the inorganic salt catalyst also includes a metal selected from columns 8-10 of the periodic table, a compound selected from metals from 8-10 of the periodic table, a metal selected from column 6 of the periodic table, and selected from the periodic table. Table 6 shows the compounds or mixtures of metals. Metals selected from columns 8-10 include, but are not limited to, iron, ruthenium, iron or copper. The metal selected from the 6th block includes, but is not limited to, complex and tungsten. In some specific examples, the inorganic salt contacts 婵 # | $ 5 Contains 啁 嫘 series mother gram inorganic salt catalyst package. .5 grams or 〇-2-〇 4 grams of Raney. In some specific examples, the inorganic salt catalyst also includes metal oxides in columns and / or thirteenth. From the thirteenth stage ... including but not limited to: boron or aluminum. Metal oxides * Metal oxidation ... ⑹, Potassium oxide (non-limiting examples of Λ include Hua Ming⑷203). In some specific Lewis acid columns such as BCl3, A1Cl3, and 糸, catalysts such as B2 (O) and ytterbium (C) or oxidized oxide (C) are not or are not substantially contained (for example, H3cr, H2s〇4 'HC1 and HN〇3, Brewster Rory acid such as borate and silicic acid) and π compounds / rolling composition (examples) and compounds. Inorganic salts per gram of inorganic salt catalyst 73 200535232 can Contains: from 0 g to (M g, 〇〇υϋ〇〇〇〇1- 〇1 gram or 0.00001-0.005 gram: coffee dagger; b) the formation of gas at a temperature of at least 350 oc or at most looooc Composition; c) Louis or e) mixtures thereof. Yi Shifang, d) Brewster-Rorylic acid; Inorganic salt catalysts can be mixed with the required amount of catalyst using standard mixing techniques (such as grinding and sterilization). In other specific examples, the inorganic composition is dissolved in a solvent such as water or a suitable organic solvent) to form an inorganic composition / solvent mixture. Solvents can be removed using standard separation techniques to produce inorganic salt catalysts. In some embodiments, the inorganic salt catalyst Γ can be formed as an inorganic salt catalyst on a carrier. Examples of the carrier include, but are not: 'Hua er, palpitations, oxidized towns, titanium oxide, hydrotalcite, oxidized sulphur, oxidized :, iron reduction, oxidation records, oxidation records, oxidation records, oxidation records, and pots Thing. In some specific examples, an inorganic salt, a "-genus and / or a metal compound of columns 6-10 can be impregnated in the carrier. Or, it can be: then imposed on the metal carrier or metal oxide loaded moon beans And / or on top of it to form an inorganic salt catalyst on the carrier. The structure of the skin inorganic salt catalyst occurs at a preset temperature or in the catalyst structure, and within the temperature range of the disorder, it usually becomes uneven; migration Inorganic salt catalyst = and / or Ke Er ,,, w, there is a consistent dagger (for example, no decomposition of salt). Without wishing to be bound by theory,… 丄 catalyst ions in the grid As the distance between them increases, A becomes / migrate). When the ion distance increases, crude oil feed and / or hydrogen source can penetrate the silk catalyst's surface, rather than across the surface of the inorganic salt catalyst. Crude oil; ^ 74 200535232 material and Permeation of a hydrogen source through an inorganic salt often results in an increase in the contact area between the inorganic salt catalyst and the crude oil feed and / or hydrogen source. An increase in the contact area and / or the active area of the inorganic salt catalyst usually increases crude oil. Product yield, restricted residues and / or coke production and / or promotion Changes in properties of crude oil products compared to the same properties of crude oil feed. The disorder of inorganic salt catalysts (such as heterogeneity, permeability and / or migration) can be measured using Dsc method, ion conductivity measurement method, TAP. , Visual inspection, X-ray diffraction, or a combination thereof.

The method of using TAP to determine catalyst properties is described in the following United States cases: 4,626,412 to Ebner et al .; 5,039,489 to%; and 5 264 183 to Ebner et al. TAPA is available from MithraTechnogies (Foley, Missouri, us a). TAP analysis can be performed at 25-85G%, 5 (in the temperature range of M⑽.c or ⑼ ·%) 3, with a heating rate of 1CM0 ° C or 2 (MoccC range and the name

Performed under vacuum in the range of 1 ^ 10 M to 1 X 10-8 Torr. Temperature can be maintained = text and / or increase as a function of time. When the temperature of the inorganic salt catalyst increases, it is measured that the gas discharged from the inorganic salt catalyst. Examples of the gas discharged from the inorganic salt catalyst include an emulsified carbon, carbon dioxide, A, water, or a mixture thereof. A turning point (a sharp increase) in the release of the inorganic salt catalyst gas is detected. # The temperature is considered to be the temperature at which the inorganic salt catalyst becomes disordered. In some specific examples, the turning point of the exhaust gas from the inorganic salt catalyst can be moved within 1 degree as measured using TAP. This temperature or phase range is called the "TAP temperature." The starting temperature of the temperature range where TAp is used is called the "minimum TAPH temperature." 75 200535232 Emissions exhibited by inorganic salt catalysts suitable for contact with crude oil feed Gas · 1 00.600 0 C. 2 0 0 0 5 0 0 0 0 c ^ 3 0 4 0 0 0 0 c ^ TAp temperature range M. Typically, the TAP temperature is in the range of V in the above specific examples, suitable inorganic Different compositions of salt catalysts also show gas turning points, but at different TAP temperatures. "The size of the ionization turning points related to the exhaust gas can be an indicator of the order of the substructures in the crystal structure. In a highly ordered crystal structure, ionic particles are usually tightly associated, so the release of ions, molecules, gases, or a combination thereof requires more energy (that is, more heat). In the disordered crystal structure, the ions are not as strong as each other, as in the highly ordered crystal structure. Due to this lower ion association, the release of filaments, molecules, and / or gases from the disordered crystal structure usually requires less energy. Therefore, the ion and / Or the k hang of the gas is greater than k N degrees of ordered crystal structure release of ions and / or gas

When using differential scanning calorimetry at 100 ° C

In some embodiments, the heating rate or cooling rate may be 50 ° C. . Extremely. c Scope Observe the heat of dissociation to the inorganic salt catalyst. In the 纟 Dsc method, the sample can be heated to the-temperature ', cooled to room temperature, and then heated again. The transitions observed during the first heating usually represent entrained water and / or solvents, and may not represent heat of dissociation. For example, a moist mouth that is easy to observe is usually hot and dry in the mouth. Below c, typically at 100-150 〇p + pq 4- χλ 1 °, the transition observed during the crotch cycle and the second heating corresponds to the heat of dissociation of the sample. 76 200535232 “Thermal transition” refers to the process that occurs when a 3 atom becomes disordered when the ordered molecules and / forms / fields in the composite structure increase in the south during the DSC analysis. "A to Ai refers to the process that occurs when the ordered molecules and / or atomic iron corpse of the day τ are low in DSC, such as in a structure r instance + blood society ', and the text is more uniform. -In the case of Diyuedandan, the inorganic salt catalyst appears in the range of the temperature. In the _Ath turn, the inorganic salt catalyst appears during the heating cycle of the w 埶 person, which is transformed by using the dsc. l, the escaped / dish degree or temperature range is called "the most temperature range during the coffee heat cycle. In the second addition of mm mm " Sc ^ degrees is called "minimum Dsc warming without picking salt catalyst can target between 巧 50-450 ° c or between 300-400 ° c In the range, the thermal transition is exhibited. Among inorganic salts containing organic salt particles that are fairly uniformly mixed with 8% m λ η mouth, Γ: In the medium containing :: large: ㈣, the inorganic salt with the inorganic salt particles of the mixture is in contact. When broad. I = 7: The peak of the heat absorbed during ΓΓ may be within the range of 1 °. The absence of Taifeng indicates that the salt does not absorb or release heat within the scanned temperature and dry range. Without heat transfer «No Changes during heating. Spear sample. Mouth, ..D during the structure to maintain the uniformity of particles in the Γ u increase, the mixture's ability to heat uniformity τ :, / or semi-liquid decreased. For cations with a small ionic radius, the cations are closed. As for the cations that have a greater percentage of force than those of the counter ion and share the corresponding anions, the acidity of the corresponding anions increases. For ions that read like charges, such as ^ ㈣ ion 疋 a hard base, then the smaller + diameter leads to High ion-attractive 77 200535232 gravitational ions, F f 1 3 3 丨 γ s / temperature and / or more salts in the salt have a higher thermal transition to increase the area under the C curve). Package: two = Sharp plum mixture tends to have a larger ionic radius, Yang Erzifeng: The acidity of the cation inorganic salt mixture decreases with the cation radius: 驮 & 'So, crude oil feed and hydrogen source are included; add. For example. The contact in the presence of an inorganic mixture of ΛΑ ^% ions, compared to the contact between the crude oil feed and a hydrogen source in the presence of an inorganic salt catalyst containing a cation with a larger ion radius, tends to produce an increased amount of gas and / Or coke. The ability to inhibit gas and / or coke production increases the total liquid product yield of the process. In some specific examples, the inorganic salt catalyst may include two or more inorganic salts. Each of the inorganic salts may be determined The minimum DSC temperature of the engine. The minimum DSC temperature of the 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 carbonate shavings. carbon Potassium and carbonic acid planers exhibit dsc / dish greater than 500. K2C03 / Rb2C03 / Cs2C03 catalysts exhibit DSC temperatures in the range of 290-300 ° C. · In some specific examples, the TAP temperature may be in the inorganic salt range. The DSC temperature of at least one of them and the DSC temperature of the inorganic salt catalyst. For example, the TAP temperature of the inorganic salt catalyst can be in the range of 350-500 ° C. The DSC temperature of the same inorganic salt catalyst can be In the range of 200-300 ° C, and the DSC temperature of individual salts may be at least 500. (: or at most 10000c. In many specific examples, it has a temperature of 150-500 ° C, 200-450 ℃ and TAP and / or DSC temperatures between 3 00-400 ° C and do not decompose at these 78 200535232 temperatures i High viscosity groups ... The medium can be used to catalyze high molecular weight and / or ^ such as crude oil feed )) The effect of conversion into a liquid product. In some specific examples, during the heating of inorganic salt catalysts in the range of 〇350-450 ° c ^ ^ ^ m L or 'Li & the inorganic salt catalysts can be displayed compared to individual helmets "^ ^-ϋ. ^ ,,,, and-are for increased conductivity. The increased conductivity of inorganic salt catalysts is affected by 3 逋 * 疋 because the particles in the inorganic salt catalysts have shifted. Some benefits, The temperature at which the ionic conductivity of the catalyst I changes 俜 is lower than the temperature at which the ionic conductivity of the inorganic salt catalyst changes again. The temperature at which the ionic conductivity of a component in the middle and early morning changes is lower. The ionic conductivity of the inorganic θ salt Ohm's law can be used to determine: η, & & 7 疋 current 'and a is resistance. To measure the ion conductivity, ..., organic salt catalyst is placed on two separate from each other but immersed in the beneficial organic salt contact In the quartz container of metal wire (such as copper wire or inscription wire) in the medium Γ Figure 7 is a schematic diagram of a system that can be used to measure the conductivity of I ions. Samples can be included. The quartz container 156 with a port 158 is placed in a heating device and is incremented. The ground is heated to the desired temperature. A voltage from the power source 16 is applied to the gold during heating. Belongs to line 162. The resulting current passes through the metal line "2 # 164 and is measured at meter 166. The meter 166 may be, but is not limited to, a multimeter or a Wheatstone bndge. As the sample becomes more non-uniform (more mobile) without decomposition, the resistance of the sample should decrease and the current observed in meter 166 should increase. In some specific examples', at a desired temperature, the inorganic salt catalyst may have different ionic conductivity after heating, cold drawing, and then heating. The difference in ionic conductivity can indicate that the crystal structure of the inorganic salt catalyst has been heated during the heating period. 2005200535232: The original shape (the first form) is changed to a different shape (after the second form is heated, if the inorganic salt catalyst form is heated If there is no change during this period, the ionic conductivity is expected to be similar or the same. In some specific examples, the inorganic salt catalyst has a particle size in the range of 1CM 000 μm, 20-50 μm g 5 (M00 μm, If the inorganic salt catalyst is measured through a net or a sieve. The inorganic salt catalyst may be softened at a temperature of 50 ° C or higher and less than 500 oc /%. When the inorganic salt catalyst is softened, the liquid It can coexist with the catalyst particles in the inorganic salt catalyst matrix. In some specific examples, the catalyst particles are heated to at least 300 ° C or up to 800. (: at a temperature of gravity, or at least 0.007 Self-deformation can transform the inorganic salt catalyst from the first form to the second form under a pressure of MPa or at most 010 Mpa. When the inorganic salt catalyst is cooled to 20, the second form of the inorganic salt catalyst cannot be returned. Inorganic salt catalyst The first form. The temperature at which the inorganic salt changes from the first form to the second form 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 When heated to the lower side; at any deformation temperature below the deformation temperature of any of the individual inorganic metal salts, _ will self-deform under gravity or pressure. In some specific examples, the inorganic salt catalyst contains one or more different deformations Temperature inorganic salt. In some specific examples, the deformation temperature of the inorganic salt catalyst is different from the deformation temperature of individual inorganic metal salts. In some specific examples, the inorganic salt catalyst is at TAP and / or DSC temperature or above Liquid and / or semi-liquid. In some specific examples, the inorganic salt catalyst is liquid or semi-liquid at the minimum TAP and / or DSC temperature. At 80 200535232 the minimum TAP and / or DSC,, prison, shirt, or above In some specific examples, the mixed liquid of the crude oil feed agrees with φ times + the liquid inorganic salt catalyst will form a phase separated from the feed of the tray. , At the minimum TAP temperature, the semi-liquid inorganic salt catalyst has low solubility in the crude oil feed (for example, the mother gram crude oil feed ranges from 0 g to 0.5 g, 0.0000 g to 0.2 g Or 〇〇〇〇〇〇〇- 1 · 1 g of inorganic salt catalyst) Η τ oil feed from 0 g to 0; gram 5 two crude oil feed (such as per gram of the original salt of inorganic catalyst) · Gram. ⑽ coffee cents or G buy 1 side inorganic ==: Department uses powder "ray diffraction method to shape her ... ... = = = ray =, the ^ pair of _ human order of the peak. X_ ray diffraction in the Dust peaks represent different species of inorganic salt catalysts, and can't be gated at 1 D. In powder X-ray diffraction, J °. With one peak, the interval between atoms can be estimated. The shape of the D_ peak in humans is very narrow in the contact with inorganic salts containing high-yield inorganic salt atoms. In: Co; Rb inorganic salt catalyst inorganic salt atom (such as K2C03 / Rb2C03 / Cs2C0, M M rb broad skin, or ', medium, the shape of the D〇〇 peak may be quite " or D⑽】 the peak may not Existence. Whether to change during heating, the disordered in-ray diffraction pattern of the inorganic salt atom can be taken. Panli Yaozhuan compares the inorganic salt catalyst before heating. Χ-ray obtained after 50〇Γ ... In the diffraction pattern obtained by the diffraction pattern at the upper temperature, the X-ray diffraction pattern of the upper, lower, and lower luo salt atoms may not exist, or the X-ray refraction at ~ 500 kg will be taken. Don't be inorganic in the radiograph spectrum ...- ray diffraction patterns can be the same: two-wide :. : Outside, the D00I peak. Φ exhibits a relatively narrow size under phase gates / plates 81 200535232 In addition to limiting and / or inhibiting the generation of by-products # ^ ^ ^ ^, in addition to the war, the contact conditions can be controlled to make the Fuwu product composition (that is, make ^ ^ ^, Feast / by-product) can be changed for a given crude oil feed. Complete product composition You are not limited to paraffins, olefins, proprietary compounds or mixtures thereof. These 4-compounds constitute a composition of crude oil products and non-condensable hydrocarbon gases. The combination of controlled contact conditions with the catalysts described herein can produce complete products with lower coke content than expected. Comparing the courtesy content of various crude oils allows crude oils to be graded according to their tendency to form coke. For example, a shield crude oil with an MCR content of 0.1 g MCR per gram of crude oil is expected to form more coke than a crude oil with a 0.001 g MCU MCR content in the parent gram of crude oil. Inferior crude oil typically has an MCR content of at least 0.05 g mcr per gram of inferior crude oil. In some specific examples, the residue content and / or coke content deposited on the catalyst during the reaction may be at most 0.1 g, at most 0.05 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 0.01-0.03 g. In some specific examples, the used catalyst is substantially free of residue and / or coke. In certain embodiments, the contact conditions are controlled such that coke formation is at most 5 grams, at most 0.01 grams, at most 0.005 grams, or at most 0.003 grams per gram of crude product. Contacting the crude oil feed with the catalyst under controlled conditions, as opposed to heating raw materials, coke produced from the feed, and / or residual products by using the same contact conditions in the presence of the refining catalyst or in the absence of the catalyst. 1 'produces a reduced amount of coke and / or residue. 82 200535232 In some specific examples, the contact conditions can be controlled so that at least G.5 grams, at least Q 7 grams, at least 0.8 grams, or at least " grams of crude oil feed is converted into crude oil products per gram of crude oil. . Typically, at Menton = °: 5- ° · 99 grams. Gram lifetime converts crude feed to crude product with minimal residue and / or coke production (if any) in the crude product such that the crude product = is converted to commercial product with minimal pretreatment at the refinery And in the Λ example, crude oil feeds of at most 0.02 grams, at most 0.01 grams, 0.3 grams, or 3.0 grams per gram of crude oil feed were converted into non-classes per gram of crude oil feed. In some specific examples, there is 0 to M ^ Γ'01'0 · 1 ^ 0 · 001 · 0 · 05 ^ 10 · 01-0 · 03 ^ per gram of crude oil feed. Flow rate, finish :: The flow rate and / or amount of the feed, or a combination thereof, can be carried out at :: the desired reaction temperature. In some specific examples, the temperature in the contact zone can be performed by changing the amount of gaseous chlorine source and / or inert gas to dilute the amount of hydrogen through the contact zone 1 and / or remove excess heat from the contact zone. In some specific examples, the temperature in the contact area can be controlled so that the temperature in the contact area is the desired temperature "T, or above or below some specific shots, the contact temperature is such that ^ TAP temperature and / or The minimum job temperature is too small

In the minimum temperature and / or minimum ^ / house example, A. . Or below. For example, in the case of 222, 720 ^ A ^ U, when the minimum temperature and / or the minimum DSC temperature are complete. At C, the contact temperature can be controlled to 370 ° C, 380 during the reaction period. (: Or 390 Qc. In other specific examples, the contact temperature is controlled such that the temperature is at or above the contact TAP temperature and / or the catalyst DSC temperature. For example, each minimum TAP temperature and / or minimum DSC temperature is 450 b + + inch, the contact temperature can be 450 V, 500 ° C, or 55 ° c during the reaction. The contact temperature is controlled according to the catalyst TAAρ temperature and / or the catalyst DSC temperature. Product properties. For example, this control can reduce bleaching / treatment, anaerobic formation, reduced non-condensable gas generation, or a combination thereof. In some specific examples, the organic salt catalyst can be adjusted before adding crude oil feed In some specific examples, the adjustment may be performed in the presence of a crude oil feed. Adjusting the inorganic salt catalyst may include heating the inorganic salt catalyst to at least 100 ° C, at least 300 ° C, at least 400 ° C Or at least the first temperature, and then the inorganic salt catalyst is cooled to a maximum temperature of 2500c, a maximum of 2 ° C. Or a second temperature of 100 ° c. In the specific example of the 駚 xingshe community, The inorganic salt catalyst is heated to W50-700 ° C and 600 ° C. Or the temperature within the range of 〇〇〇〇〇〇〇〇〇。 'and then cooled to 25-240 oc, 30_200 m0_90. ^ Within the second temperature. Adjusting the temperature can be buried / again Ji Tian 冽 疋 at different temperatures Ionic conductivity measurement. In this specific example, the adjustment temperature can be determined from the DSC temperature of the thermal / cold transition obtained by heating and cooling the inorganic salt catalyst multiple times in DSC. Inorganic contact The extraction of Xia catalyst can allow the contact of crude oil feed at a lower reaction temperature than that of conventional hydrotreating catalysts. In some specific examples, The content of the effluent, vg0 or its mixture in the complete product can be changed by changing the speed at which the complete product is removed from the contact zone 84 200535232. For example, reducing * 8 is more than increasing the crude oil feed catalyst The product removal rate tends to the contact time of the first media. Or the pressure of the initial force can increase the connection :: Compared to the crude oil feed with a predetermined mass flow rate from the beginning ... 2: The production of oil products, the blending of crude oil products, UP. Can increase hydrogen from gas into J ~ 口 'or you can change the contact time of these additives with the catalyst, 、,' 口. Crude oil feed: two V VG. In terms of the amount, can increase the amount of 2 kerosene 3 light oil and reduce the amount of VG〇. Increasing the contact time in the wood can also change the time of the 70 King products in the contact zone can be compared: the average number of dishes: weight: 100 products. Increase,

Specific Gravity) Lower carbon number with a weight I percentage (hence a higher API

"In some specific examples, the contact conditions may change over time. For example, two: increase the contact force and / or contact temperature to increase the absorption of crude oil feed:" the amount of hydrogen in the crude product. Changing the amount of hydrogen absorption of the crude oil feed, while improving the ability of the crude oil feed to other properties, and increasing the types of crude oil products that can be produced from a single U. The ability to make multiple raw and produced products from a single crude feed may allow different shipping and / or processing specifications to be met. Hydrogen uptake can be evaluated by comparing the H / c of the crude feed to the muscle of the crude product. The increase in crude product H / c relative to the crude feed H / c indicates that hydrogen was incorporated into the crude product from a hydrogen source. The rather low increase in H / c in crude oil products (20% when compared to crude oil feeds) indicates during processing: rather low hydrogen consumption. Crude product properties obtained with minimal hydrogen consumption = significant improvement over crude oil feedstock is ideal. ^ It is also possible to change the ratio of hydrogen source to crude oil feed to change the properties of crude oil products. 85 200535232 ’Increasing the ratio of hydrogen source to crude oil feed can result in crude oil products with increased VGO content per gram of crude oil product. J. gram of raw materials and / or steam :::: contact: feed and inorganic salt catalyst in contact with light hydrocarbons in the presence of chlorine and steam: :: crude oil feed and inorganic salt Less specific materials that are contacted in the presence of more liquid media in the spoon may contain components that are at least part of the crude oil product. Atomic carbon and hydrogen in the molecular structure of the component (from the specific example of f), the volume of the crude oil product obtained from an inorganic source with a hydrogen source is at least at least the volume A of the oil product from the thermal coating under stp. Less ISO / bucket, 10% of r 4/0, or up to ^ ㈣ crude oil ㈣ contact with inorganic salt catalyst "the total volume of the raw material can be at least 110 volumes of the volume under the crude oil feed coffee %. The increase in volume ^, caused by the lower density is usually at least partly due to the degree of reduction. &Quot; F knife system due to the hydrogenation of crude oil feed in some specific examples, per gram of crude oil The feed contains a medium containing at least gram, gram, or at least M grams of sulfur and / or at least ^ grams of N ore e = contact with a chlorine source in the presence of an inorganic salt catalyst without detracting from the contact-some specific examples In the inorganic salt catalyst, at least part of it can be regenerated by removing one or more of the following components: pollutants include without limitation; metals, sulfides, nitrogen, coke or mixtures thereof. Sulfide pollutants 86 200535232 Hydrogen sulfide can be produced by contacting steam and carbon dioxide with used catalysts. Removal from used inorganic salt catalyst. Contaminants can be removed by contacting the used inorganic salt catalyst with hot steam to produce ammonia. Coke pollutants can be contacted with steam and / or toluene through the used inorganic salt catalyst. Hydrogen and carbon oxides are generated and removed from used inorganic salts. 纟 —In some specific examples, one or more gas systems are generated from a mixture of inorganic salt catalyst and residual crude oil feed.

In some specific examples, used inorganic rhenium (such as K2C〇3 / Rb2C03 / Cs2C03; K0H / A1203; Cs2C03 / CaC03; or NaOH / KOH / LlOH / Zr〇2), unreacted crude oil Feed and / or residue and

Or ..., the mouthpiece is heated to a temperature in the range of 70 (M_ "800,00 ..." in the presence of strips, hydrogen, carbon dioxide and / or light hydrocarbons, until the gas and / or The production of liquids is minimized to produce a liquid phase and " Ge gas. The gas may include hydrogen and / or carbon dioxide in an increased amount relative to the reaction gas. For example, 'gas may include Q l_99 mole or mole per mole of reactive gas Lice and / or carbon dioxide. The gas may contain a relatively low amount of light hydrocarbons and / or carbon oxides. For example, light hydrocarbons less than 0.05 g per gram of gas and less than 0.01 g of carbon monoxide per gram of gas. The liquid phase may contain water, for example, a mother gram of liquid greater than 0.5-0.99 grams or greater than 0.9-0.9 grams of water. In some specific examples, used catalysts and / or solids in the contact zone may be treated so as to be used therefrom. Catalysts and / or solid recovery metals (such as vanadium and / or nickel). Used catalysts and / or solids can usually be treated using known metal separation techniques such as heating, chemical treatment and / or gasification. Catalyst preparation, catalyst test and those with controlled contact conditions 87 200535232 non-limiting examples of the system are described below. Preparation of dagger catalyst. A K-Fe sulfide catalyst system is prepared as follows: grams of iron oxide (Fe2Q3) and 58 grams of carbon-poor potassium 14 41 2 grams of deionized water were combined to form a wet paste. The wet paste was dried at 200 to form an iron oxide / potassium carbonate mixture. The iron oxide / potassium invertate mixture was calcined at 500 to form an iron oxide / potassium carbonate mixture. The rhenium iron oxide / potassium rhenate mixture was reacted with hydrogen to form a solid intermediate intermediate containing iron metal. The addition of hydrogen was performed at 450 ° C and 11.5-12.2 MPa (765 psi) for 48 hours. The intermediate solid was passed through a 40-mesh screen with minimal force. The & exothermic rate was added incrementally to the intermediate solids to produce a gas at 100 to the v-xylene / elemental mixture. After the addition of 1 solid, the resulting mixture was gradually heated to · V and allowed to stand for 1 hour at 300 ° C. The solvent / catalyst mixture is cooled to 100 ° C, and the lower sublayer separates the sulfurized catalyst from the mixture. The vulcanization catalyst was passed through silk analysis in a dry box under an argon atmosphere, and then washed with xylene off to obtain 54.7 g of a K-Fe sulfide catalyst. The K-Fe sulfide catalyst was pulverized by passing it through a 40-mesh screen. The X-ray diffraction technique was used to analyze the obtained sulfide catalyst. "Analysis of the line diffraction pattern, it was determined that the catalyst contains sulfite, K Fe litholithate (KFes 2), pyrrhotite, and iron oxides (eg, iron ore 'Fe 3 04). No χ-ray diffraction pattern was observed for iron disulfide (eg, yellow iron, tons).

The contact of light sulphide chess in the name I 88 200535232. The coffee liter $ liter, _ mixing tank reactor (composed of 3 16 stainless steel) is equipped with a bottom inlet inlet, a single steam outlet, three A thunderbolt inside the reactor… a galvanic couple and a shaft-driven L25-inch diameter six-blade Rushton turbine. The reactor was charged with a K-Fe sulfide catalyst (1 ⑺ g) prepared as described in Example 1 to the reactor. Hydrogen was metered to the reactor at 8, 000 NmVm3 (50,000 SCFB). Internally mixed with bitumen (Lloydmlnster reglon, Canada). Asphalt enters the reactor through the bottom inlet feed to form a hydrogen / crude oil feed mixture. During the 185-hour reaction operation, the hydrogen Feed the crude oil into the reactor continuously, and continuously take out the product through the outflow port of the port reaction. The crude oil feed is fed in at a rate of 67.0 g / hour to maintain the crude oil feed level 60% in the reactor body. A 50 micro-Curie 137 ~ γ-ray source and a sodium flash detector were used to measure the liquid level in the reactor. ^ Gas 7 crude oil feed system and catalyst at 43. The average internal reactor at 0C contacts twice. The contact of the hydrogen / crude oil feed with the catalyst produces a complete product in the form of a reactor effluent strip. The reactor effluent vapor leaves the valley via this single upper spring. The reaction is The top is heated to 4 3 0 C with electricity to avoid the reaction. The inside of the reactor is condensed. After leaving the reaction stage, the reactor effluent vapor is cooled and separated in a high-pressure gas / liquid separator and a low-pressure gas / liquid separator to obtain a liquid stream and a gas stream. A countercurrent alkaline scrubber was used to remove acid gases and then quantified using standard chromatographic techniques. The complete product is 0918 grams of crude product and 0.089 grams of non-condensable hydrocarbon gas per gram of complete product. In the reactor, 89 200535232 per gram Crude oil feed has 0.027 grams of solid residue. The properties and composition of the product and non-condensable hydrocarbon gas produced by this method are summarized in the figures: Table 2 of the crude oil and Table 3 of Figure 10. Meaning 1, Figure 9 This example demonstrates a method of contacting crude oil feed with hydrogen catalyst in the presence of minimal coke to a genus lycophytate. P. "" Eight + eight million wood products are produced to produce a complete product. Spoon method. Contains a liquid mixture under STP and contains up to 01 grams of non-condensable hydrocarbon gas per gram of complete product .... By comparing the MCR content of the crude feed in Table 1 (13 with the solids formed during the process (27 • Li / 〇) control conditions and catalysts Combined production ratio by the ASTM method II = low amount of coke. Anything more = classes include C2, W4 hydrocarbons. From the sum of the M ',: ratio listed in Table 2 (20.5 grams), Calculate 3 units of ethylene per gram of total C2 hydrocarbons. C2 hydrocarbons of hydrocarbon gas contain 73 grams of ethylene per gram of total C2 hydrocarbons. From the sum of the weight percentages of C3 hydrocarbons listed in Table 2 (2D grams), The propane content per gram of total C3 hydrocarbons can be calculated. The non-condensable hydrocarbon gas c warp series contains 0.21 grams of propylene per gram of total C3 hydrocarbons. The non-condensable hydrocarbon gas c: hydrocarbons have 0.2 isobutane The weight ratio to n-butane. This embodiment demonstrates a method for preparing a crude oil product containing the following: at least 0 · _g at a range of up to 204 at 0.1 () 1 MPa. Take 400. Hydrocarbons of 〇, at least 0.001 g of hydrocarbons with a range of 204 ° C and 3000c at a range of 20 ° C at 10,000 MPa, boiling range of at least 0.1 MPa At 30000c with Che. The smoke range between c and at least 0.001 g is boiling range at 0.101 MPa. c and 90 200535232 53PCF). The boiling range is distributed over 204. [= Hydrocarbons include smoke-aware and normal-bonded hydrocarbons, and the ratio of such hetero-chain normal paraffins is at most 1.4. The products of the Haihai crude oil include light oil, diesel oil, diesel oil, and VGO; tM @ original: = oil products contain at least _ grams of light oil, and the emu oil portion has a stun value of at least 7G. The crude oil The light oil portion of the product has at most "i gram of crude oil per gram of crude oil product. The light oil portion of the product contains 3 ... xuan crude oil per gram of light oil, 7 AA ± 1.5 grams. The light oil portion of this kilogram of oil product is an aromatic compound per gram of light oil. To ^ 0.1 g of the early ring type, the crude oil product contains at least 0.00% of the medium oil portion having less than -30 γ, Yancoal, the aromatics of the crude oil product from the 50 Hai crude oil, and the crude oil product The kerosene in the kerosene section has at least 03 grams of aromatic ... The kerosene portion of the product has no aromatic compounds per gram of square compound. The kerosene portion containing dendrite is a compound produced per gram of crude oil. The coal has at least G.2 grams of monocyclic ring aromatics. The crude oil product is now worth $. The remaining diesel oil contains aromatic Hi · 001 grams of diesel oil. The crude oil product has at least 0.4 / Λ per gram of diesel oil, and the diesel oil of the crude oil product is divided into aromatic compounds having a gram square compound. The osmium has a compound-free content per gram-to-square. The catalyst system is prepared as τ: 1000 g of iron oxide and 173 91 200535232 423 g of deionized water are combined to form a wet paste. As in the example! N = the wet paste is treated to form an intermediate solid. The intermediate solid was passed through a 40-mesh screen with minimal force. = Example 2 In contrast, the intermediate solid system was mixed with elemental sulfur in a hydrocarbon dilution ::. In a dry box using an argon atmosphere, the intermediate solid was mixed with c = elemental sulfur, placed in a sealed carbon steel cylinder, and heated to 4. . _ C for 1 hour. The vulcanization catalyst is solid from carbon steel. The material and pestle are used to pulverize the potassium-iron sulfide catalyst into powder, so that the catalyst powder obtained can pass through a 40-mesh sieve. The obtained potassium iron sulfide catalyst was analyzed using x-ray diffraction technology. From the analysis of the X-ray diffraction pattern, the catalyst was found to contain pyrite (FeS2), ^ (FeS), and pyrrhotite ds). Using x-ray diffraction techniques No mixed potassium-iron sulfide or iron oxide species were detected. The device, crude oil feed and reaction steps were the same as in Example 2, but the ratio of hydrogen to crude oil feed was

Nmw (_, _ SCFB). A K-Fe sulfide catalyst (硫化 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 vgo obtained in Example 4 is greater than the weight percentage of VG0 obtained in Example 2. The weight percentage of the effluent produced in Example 4 was less than the distillation percentage tb obtained in Example 2. D The specific gravity of the crude oil product produced in Example 4 was lower than that of the implementation. The API specific gravity of the crude product is obtained. A higher 92 200535232 API specific gravity means that hydrocarbons with higher carbon numbers are produced. 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 K3FeiQSi4 after being in the presence of crude oil feed and hydrogen. In all TAP experiments, a 300 mg sample was heated in a TAp system reactor from room temperature (270 ° C) to 500 ° C at a rate of 50 ° C per minute. (: The exhausted water vapor and carbon dioxide gas system was monitored using the system's mass spectrometer. The K2C03 / Rb2C03 / Cs2C03 catalyst supported on alumina showed contact with the inorganic salt at 36 ° C. The carbon dioxide discharged from the medium has a current turning point greater than 0.2 Volts and the discharged water has a current turning point of 001 Volts. The minimum temperature is 36 ° C as measured by the temperature of the ion current. Figure U is from K2CQ3 / Rb2CQ3 / CS2C03 The ionic current of the catalyst exhaust gas is called (1), (), which is a graph that plots the temperature ("τ"). Curves 168 and 170 are log values of the ion current of water and CO2 discharged from the inorganic salt catalyst. The sharp turning point of water and CO2 discharged from this inorganic salt catalyst appeared at 360 ° C. In contrast to the iCCVRb ^ CVChCO3 catalyst, carbonic acid and carbonic acid are at an undetectable current turning point for both discharged water and carbon dioxide. For K2C03 / Rb2C03 / Cs2C03 catalysts, the substantial increase in exhaust gas confirms that inorganic salt catalysts composed of two or more different inorganic salts can be more disordered than individual pure carbonates. 93 200535232 DSC test of broad inorganic salt catalyst and individual inorganic salts. In all DSC tests, 10 mg samples are taken at 10 per minute. (: The rate was heated to 520 ° C, at a rate of 10 per minute. (: The rate was cooled from 520 ° C to 〇〇〇〇 '' then using a differential scanning calorimeter (DSC) DSC-7 type (Perkm-Elmer (Manufactured by Norwalk, Connecticut, USA) was heated from 0 ° C to 600 ° c at a rate of 10.0 ° C per minute. K2C03 / Rb2C03 / Cs2C03 catalyst DSC analysis during the second heating of the sample showed that the salt The mixture exhibited a broad thermal transition between 2 ° C and 26.0 ° C. The midpoint of this temperature range was 25 °. ^. The area under the thermal transformation curve was calculated as _ 丨 .75 Joules / gram. The onset of crystal disorder was determined to start at a minimum DSC temperature of 219 0C. Contrary to these results, 'No clear thermal transfer was observed for cesium carbonate.

DSC analysis of 1 ^ / 〇3, 1 ^ 2 (: 〇3 and K2C〇3 during the second heating cycle showed that the Ll2C〇3 / Na2C〇3 / K2C〇3 mixture exhibited between 390 C and 400 Sharp thermal transition between ° C. The midpoint of this temperature range is 385 ° C. The area under the thermal transition curve is calculated to be _182 Joules / gram. The onset of mobility is determined at 39 ° < 3c The most + DSC temperature starts. The sharp thermal transition represents a substantially homogeneous salt mixture. Then n jyj-; from the foot heat machine strength relative to Κ2Γ guide I test ^^ the right 4 Gorge, 隹 a L —— — Wei Wei's test system is as follows: Put the inorganic salt contact welding type J 姝 or individual inorganic salts in a 3 * 8 cm inch inch into a muffle furnace (a furnace)! In a quartz container equipped with platinum-green wires separated from each other but immersed in the sample. This ancient AA AA soil-k two-metal wire was connected to a 9.55 volt 94 200535232. The muffle furnace was heated to 600 cells and one 220,000 Ohm current-limiting resistor ° C and measure current using a micro-ammeter. The acid unloading resistance ("] og (rK2C〇3),") is shown. Curves 172, 174, 176, Ca0 resistance, Figure 12 is a graph of the sample resistance vs. carbon vs. temperature ("Ding") iog Figures 178 and 180 are the k2C03 resistance, K2C03 / Rb2C03 / Cs2C03 catalyst resistance, Ll2C〇3 / K2C〇3 / Rb2C〇3 / Cs2c〇3 catalyst resistance, and

Mapping of Na2C03 / K2C03 / Rb2C03 / Cs2C03 catalyst resistance.

⑽ (Curve 174) exhibits a relatively large stable resistance relative to k2co3 (Curve 172) at a temperature in the range of 38-500 ° C. stable

Li2C03 / K2C03 / Rb2C03 / Cs2C03 catalyst (see curve 176, 疋 's book resistance table shows disordered structure and / or does not tend to separate and move ions during heating. K2C〇3 / Rb2C〇3 / Cs2C03 catalyst, catalyst and Na2C03 / K2C03 / 178 and 180) showed a sharp decrease in relative resistivity of K2C03 t at temperatures within the range of 350-500 丨 C :. The decrease in resistivity is usually expressed in the application of a voltage to an inorganic salt embedded in

A current was detected during the period of the metal wire in the catalyst. The data in Figure 12 confirm that inorganic salt catalysts are generally more mobile than pure inorganic salts at temperatures in the 6⑻C range. Figure U is a graphical representation of Na2C03 / K2C03 / Rb2C03 / CS2C03 catalyst resistance versus K2C03 resistance ("10g G K2C03)," vs. temperature ("T,"); iOg. Curve 182 is during the Na2c03 / K2C03 / Rb2c03 / Cs2c03 catalyst heating period. The Na2C03 / K2C (VRb2c03 / Cs2c03 catalyst resistance vs. K2C03 resistance (curve 172 ) Vs. temperature. After adding 95 200535232 heat, 'cool the Na2C03 / K2C03 / Rb2C03 / Cs2C03 catalyst to room temperature' and then heat it in a conductive device. The curve 84 is at 60 ° C. After the temperature reaches 25 ° C, during the Na2C03 / K2CG ^ / Rb2C〇3 / Cs2C03 catalyst heating, 'the inorganic salt catalyst resistance is plotted against the k2C03 resistance versus temperature 10 °. Reheating The ionic conductivity of the Na2C〇3 / K2C〇3 / Rb2C〇3 / Cs2c〇3 catalyst is increased compared to the ionic conductivity of the original Na2C〇3 / K2C03 / Rb2C03 / Cs2C03 catalyst. From this inorganic salt catalyst The difference between the ionic conductivity during the first heating and the second heating, it can be inferred that the inorganic salt catalyst forms a different shape (the second form) when cooling, which is different from the form before any heating (the first form) ） Different. Organic salt catalyst _ ^ _ ^ Reference property test · Place a layer of powdered K2CCVRb2C〇3 / Cs2C03 catalyst with a thickness of 1-2 km / knife on quartz The dish was placed in an oven and heated to 5000c for 1 hour. To measure the flow properties of the catalyst, the dish was manually tilted in an oven after heating. The K2C03 / Rb2CCVCS2C〇3 The catalyst does not flow. When pressed with a spatula, the catalyst has the consistency of toffee. | In contrast, individual carbonates are free-flowing powders under the same conditions. Under the same conditions The Na2C03 / K2C03 / Rb2C03 / Cs2C03 catalyst becomes liquid in the dish and is easy to flow (for example, similar to water). Ca n’t be used to store tF in Example 9-27 The equipment and general steps are listed, except for the case where the variables are stated. 96 200535232 # 4576 w. 250 ml HaStell〇y C Parr autoclave (Pair Model and 500 C rated at 35 MPa operating pressure (500 psi) ) ,: has a mechanical stirrer and an 800 watt Gaumer heater located on the EUrotherm controller that keeps the autoclave at ambient temperature, a gas inlet, a steam inlet, an outlet and a thermocouple to the internal temperature. Before heating, m is separated by glass cloth. Container: Adding container (250ml, 316 stainless steel hoke), equipped with fork-controlled heating system, appropriate gas control valve, pressure release device, thermocouple, pressure gauge and high temperature control Valve (sw —

Valve # SS-4UW), capable of regulating 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 the reactor exit and was introduced into a series of decreasing temperature cold traps (dipping tubes connected to a series of 150 ml, 3 16 stainless steel Hawker vessels). The liquid from this vapor condenses in the cold trap to form a gas stream and a liquid condensate stream. If necessary, use back pressure adjustment to adjust the flow rate of vapor from the reactor and through the cold trap. The flow rate and total gas volume of the airflow leaving the cold trap were measured using a wet test meter dttei * Model # TG 05 Wet Test Meter. After leaving the wet flowmeter, the gas stream was collected in an air bag (a Tedlar gas sample for analysis. GC / MS (Hewlett-Packard Model 5890, now Agilent Model 5890; Agilent Technologies, Zion 97 200535232)

(Manufactured by Illinois, 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 per gram of crude feed, a nitrogen content of 0.011 grams, and a total Ni / V content of 0.009 grams. 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 grams of K2co3, 19.44 grams of Rb2CO3 and 24.49 grams of Cs2C03 were combined. The K2C03 / Rb2C03 / Cs2C03 catalyst has a minimum TAP temperature of 360 0C. The K2C03 / Rb2C03 / Cs2C03 catalyst has a DSC temperature of 250 ° C. Individual salts (K2C03, Rb2C03 and Cs2C03) do not exhibit DSC temperatures in the range of 50-500 ° C. This 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 at a normal pressure flow of 250 cm V of methane. (:. After reaching the desired reaction temperature, steam was metered into the reactor at a rate of 0.4 milliliters per minute and pristane at a rate of 25.0 cm 3 per minute. After the crude oil feed was added to The steam and methylbenzene were continuously metered during the reactor for 2.6 hours. The crude oil feed was pressurized into the reactor using u Mpa (229 psi)% for 6 minutes. After the addition of the crude oil feed was completed, the residue The crude oil feed (0.56 g) remained in the addition vessel. A decrease in temperature to 370 ° C was observed during this crude oil feed addition. The catalyst / crude oil feed mixture was heated to a reaction temperature of 45% and 98% 200535232 was maintained at this temperature 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. From the initial catalyst weight to coke The difference in weight of catalyst / catalyst mixture shows that 0.046 grams of coke remained in the mother gram crude feed. The complete product contained 0.87 grams of crude product and gas with an average Aρ specific gravity of 13. The gas contained unreacted Cl and hydrogen , C2 and hydrocarbons and co2 (0.08 g of co2 per gram of gas).

" Hai Yuan 'from the product line contains 0.01 grams of sulfur and 0.000005 grams of total Qin and V per gram of crude oil product. The crude product was not analyzed further. In Example H), the reaction steps, conditions, crude oil feed and catalyst system are the same as in Example 9. The crude oil product of Example 10 was analyzed to determine the boiling range distribution of the crude oil product. The crude oil product is a gram of light oil per gram of crude oil product, 0.19 grams of distillate, 0.45 grams of VG0 and 0.00001 grams of residual content, and less than a small amount of coke. Examples 9 and 10 demonstrate crude oil feeds and gas sources per gram of crude oil.

= More than 3 grams of contact in the presence of a catalyst to produce a complete product containing liquid, oily products under STP. The crude product has a residue content of up to 30% of the feed slag content. This is the sulfur content of the crude oil feed, and the content of m / v. v Sulfur content of 90% in each summer> Lu Hai crude oil product contains a distribution of at least 0.001 and at most 200. . … Boiling at 0 · 101 Mpa Fan Boiling Fan Shao please 1 gram Futten target range under G.1G1 coffee distributed at 200 · 300 oc <hydrocarbons, at least 0.001 g 99 200535232 Boiling at 0.101 MPa Hydrocarbons ranging from 400-538 ° C (1000F). 11 -12,:

£ · ^ £ Ώ ^ _. Catalysts and steaming Jj_Existence of two benefits · The reaction steps and conditions in Examples 11 and 2 and the K / CVRb / Os / Cs / O3 catalyst system are the same as in Example 9. However, 130 grams of crude oil feed (Cerro Negr0) and 60 grams of K2C03 / Rb2C03 / Cs2C03 catalyst were used. In Example jJ, methane was used as a hydrogen source. In Example 12, hydrogen was used as a hydrogen source. A graphical representation of the non-condensable gas, crude product, and coke content is depicted in FIG. 14. Strips 186 and represent the weight% of coke produced, strips 190 and 192 represent the weight% of produced liquid hydrocarbons, and strip 194 #port 196 represents the weight percent of produced gas, which is based on crude oil. Material weight is the basis. In Example 11, 93% by weight of crude oil product (strip 192), 3% by weight of gas (strip 196), and 4% by weight of coke (strip 188) were prepared, which was based on the weight of Cerro Negro as Benchmark. In Example 12, a 84% by weight crude oil product (long strip 900) was prepared,

7% by weight of gas (strip 194) and 9% by weight of coke (strip 186), based on the weight of Cerro Negro. The corpse example called mouth 12 provides a comparison of the use of methyl chloride as a source of chlorine and the use of chlorine gas as a source of hydrogen. Pinane is generally cheaper to manufacture and / or transport than hydrogen, so a method using methane is ideal. As demonstrated, when the crude feed is contacted in the presence of a money salt catalyst to produce a complete product, torrefaction is at least as effective as gas as a source of hydrogen. Specific gravity of crude oil. 100 200535232 The device, reaction steps, and inorganic salt catalyst system are the same as those described in Example 9, but the reactor pressure is changed. In Example 13, the reactor pressure during the contact was 0 "MPa (14 7 PS0.) A crude product having a API density of 25" was obtained at 15. "C. The whole product had a carbon number distribution in the range of 5 to 32. Hydrocarbons (see curve 198 of 5). In Shell 14, the reactor pressure during the contact was 4 3.4 MPa (514.7 psi). 15.5 was obtained. Crude oil product with a T API specific gravity of 51.6 The complete product has a carbon number distribution in the range of 5 to 15 as shown in the curve 200 of FIG. 15). These examples are exemplary; # &amp; Motor oil and lice in contact with inorganic salt catalysts under different pressures to Method for obtaining crude oil products with a selected API weight ratio of right,, and #. By changing the pressure, a crude oil product with a lower or lower API weight ratio is hunted by I and II. The "coating, crude oil feeding and reaction steps were the same as in Example 9 'but the crude oil was fed and touched. #Use / media (or carbonized stone) at the same time directly into the mouth of the reaction. Carbon dioxide (CO, Conda &amp; 2) was used as a carrier gas. In Example 15, the Cerro Negro plate 60 4 ancient τ / _ /, 0.4 g K2C03 / Rb2C03 / Cs2C03 catalyst (same as in Example 9 3 2 3 ^ right Γ Shu) δ and . In Example 16, 132 sees Cerro Negro and 83 η ancient

Matp. 1 · Silicone (40 mesh, Stanford

Materials; Alls Viej, human tM, +, M + I). It is believed that this silicon carbide has low catalyst properties under the method conditions described in this article. 101 200535232 In each sample, square ~? , Heat the mixture to 500 between taxi, /, inch / month. c reaction temperature. C0 was measured at a rate of 100 cm 3 / min to 彳 πη at 88 3 2 to the reactor using a back pressure of 3.2 MPa (47Q 7 ·, 7 · 7 ps〇. Decomposition and momentum φ ^ +, Mi A. The crude oil product from the cold trap was consolidated and analyzed. Dao Guang was in Example 15 from this crude oil feed with inorganic salt catalyst in a dioxin atmosphere. The contact chapter J / U Serv 36.82 1 (26.68% by weight, based on the weight of the raw material) is a colorless smoke liquid with a weight of 50.

In Example 16, a 1 5 7 8 coupon was prepared from the contact between the crude oil feed and silicon carbide in a carbon dioxide atmosphere. (Based on the weight of the material) A yellow hydrocarbon liquid with an API specific gravity of 12. Although the yield in Example 15 was low, the on-site generation of the gas source in the presence of the inorganic salt catalyst was greater than the on-site generation of hydrogen in the absence of the 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 hydrogen was generated during the contact of the crude oil feed in the presence of inorganic salts and the absence of a gaseous hydrogen source.

1 Shen J 17—_20 "__ Feeding and CO, / Random 遽, silicon oxide exists in the atmospheric pressure 倏 侔 coupling device, reaction steps, crude oil feed and inorganic salt catalyst system and in Example 9 It is the same, but Cerro Negro is added directly to the reactor instead of via an addition vessel, and hydrogen is used as the hydrogen source. The reactor pressure during the contact was 0.101 MPa (14_7 psi). The hydrogen flow rate was 35.0 cm / 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 200535232 In Examples 17 and 18, the K2C03 / Rb2C03 / Cs2C03 catalyst was used. In Example 17, the contact temperature was 375 dC. In Example} 8, the contact temperature is in a temperature range of 500-600 0C.

As shown in Table 4 (Fig. 16), for Examples 17 and 18, when the temperature was increased from 375 ° C to 500 QC, the gas production was increased from 0.02 g ^ to 0.5 g of gas per gram of complete product. However, coke production decreased at higher temperatures from 0.17 grams per gram of crude feed to 0.09 grams of coke. The stone claw S cap of the crude product also decreased from 0.001 g per gram of crude product to 0.008 g of sulfur at a lower temperature. Both crude oil products have an H / C of 1.8. In Example 19, the crude feed and caC03 were contacted under conditions similar to those described in Example 18. The 100-to-knife series table for crude oil products, gas and coke production is shown in Table 4 of FIG. The gas production was square in Example 9 and the gas production in yoke 18 was increased. The demelting effect of the crude oil feed is not as effective as that in the embodiment 8. Compared to the sulfur content of 0.8 g of crude oil product per gram of crude oil product produced in Example 18,

The crude product produced in Shell Example 19 contains 0.01 g of sulfur per gram of crude product. Bega example 20 is for the embodiment, ~ μ on ^ Ding only. The company 1 also loaded 8 3.13 grams of silicon carbide into the reactor instead of the inorganic salt catalyst. The gas production and coke production in Example 20 were increased relative to the volume and coke production of Example 18. Under these catalyst-free conditions, gram of crude oil produced 4-22 grams of coke, 0.25 grams of non-condensable gas, and grams of crude oil products. For example, as compared with the amount of sulfur per gram of original 0.01 g produced in Example 18, the crude oil product produced in Example 20 contains 0.0 3 6 g per 103 200535232 oil product. Lau. Further examples demonstrate that the catalysts used in Examples 7 and 8 provide improved results over catalyst-free conditions and conventional metal salts. At 500. The amount of coke and non-condensable gas at and a flow rate of 250 cm V of hydrogen is significantly lower than the amount of coke and non-condensable gas produced under catalyst-free conditions. In the examples using inorganic salt catalysts (see Examples 1 to 7 in Table 4 in Figure 丨 6), compared to those formed during control experiments (eg, Example 20 in Table 4 in Figure 丨 6) Gas: It is observed that the weight-to-blade ratio of the generated gas is reduced. From the amount of smoke in the generated gas, it is estimated that the cracking of the crude oil feed is at most 2G% by weight, at most 15% by weight, at most 1% by weight, and at most 5% by summer, or not, in contact with the hydrogen source The total amount of crude oil feed is ~ oil feed and gas bear cicadas — or jellyfish treatment in the presence of carbonized hair

The devices in Examples 21 and 22 were the same as in Example 9, but were used as the source of lice. In Example 21, 130.4 grams of Cerro Neg 舁 30.88 grams of K2C03 / Rb2C03 / Cs2C03 catalysts were combined to form the original; I In Example 22, 139.6 grams of Cerro Neg] "14 Grams of silicon carbide were combined to form a crude oil feed mixture. The crude oil feed mixture was charged directly into the reactor. The crude oil feed mixture was heated to 300 ° C and the reaction temperature was increased to 300 ° C while maintaining the temperature 400 ° C and maintained at 40 ° C. After the reaction temperature reached 4000c, water was sent into the reactor at a rate of 0.4 g 104 200535232 minutes to combine with hydrogen. Water and hydrogen were metered to the reaction To maintain heating and residence time. After maintaining the reaction mixture at 0 ° C ', increase the reaction temperature to U 500. (: and maintain at 500 γ 2 J t collect the vapour generated in the reaction state in the cold In the trap and air bag. The liquid product from the cold trap was consolidated and analyzed. In Example 21, the weight is based on (dark red gram). 86 · 17 grams (66 1% by weight, feeding brown hydrocarbon liquid (crude product) and water ( 97 5 K2C03 / Rb2C03 / Cs2C03 Catalyst in hydrogen atmosphere

In Example 22, from anti-kusam # is to generate water radon gas and a small amount of gas. Check the reactor, and take the frozen brown viscous hydrocarbon liquid from Kuanshan and Daijiujian. Feed from crude oil with silicon carbide in hydrogen brown viscous hydrocarbon liquid. Phase Yield A 25% increase in crude oil product yield was observed in Example 21.Sinking contact yielded a depth of less than 50% by weight compared to the crude product produced in Example 22.

Implementation: The improvement in the properties of crude oil products produced using the methods described herein relative to crude oil products produced using hot water. Specifically, the crude oil product in Example 2! Is lower in boiling than the crude oil product obtained from the implementation [22], as demonstrated in the crude oil product produced in Example 22+ cannot be produced as a base gas. Compared to the crude product produced in Example 22, the crude product produced in Example 21 has enhanced flow properties, as determined by visual inspection. The product configuration, 105 200535232 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 reactor and a hydrogen source is used. The crude oil feed (CerroNegro) had an Aρ specific gravity of 6. 7 and a density of 1.02 g / ml at ΐ5 · =. In Example 23, 102 g of a crude oil feed (100 ml of a crude oil feed) and 3 g of a K2CO3 / Rb2CO3 / Cs2CO3 catalyst were charged into a reaction:. A crude oil product (μαg) with a specific gravity of 50 / PI and a density of 15.5% was 0.7976 g / litre (112¾ liters). In Example 24, 102 t of crude oil feed (100 ml of crude oil feed) and 80 g of silicon carbide were charged into the reactor. A crude oil product (70 g) having a specific gravity of 12 and a density of 15.5 (Si 98986 g / ml⑺ml) was prepared. Under these conditions, the volume of the crude oil product obtained from Example 23 was large. The force is 10% into the volume of the crude oil feed. The volume of Example 24 is significantly smaller than (4 exposures) in Example 23 = the volume of the product. The significant increase in the volume of the product enhances the producer's production of crude oil per volume of input The capacity of more volume of crude oil products. The last device and reaction steps in the presence are the same as those described in Example 9, but the steam is metered into the reactor at 300 cm3 / min K2C03 / Rb2C03 / Cs2C03 The catalyst was prepared by combining 27.2 g of K2C03, 32 2 g of RbO3 and 40.6 g of Cs2C03. The crude oil feed (13.35 g) and the K2C03 / Rb2C03 / Cs2C03 catalyst ( 3 1.6 grams) was charged into the reactor. CerrO Negr 0 crude oil was 106 106 35 232 per gram of crude oil. The feed contained 0.04 grams of boiling range distributed between 149 and 260. (: (300-500 ° F) total Aromatic compound content, G · Ca 64 () g combined Luhe and Su, 0.042g of sulfur and 0.56g of funeral. The The Αρι specific gravity of the oil feed is 6.7. The contact between the crude oil feed and the K2C (VRb2C〇3 / Cs2C〇3 catalyst in the presence of K2C (VRb2C0 / Cs2C03) catalyst is called ^ ^ c \ brother crude oil feed Based on this, the system produced 0.995 grams of complete product and 0.041 grams of coke. The complete product system contained 0.91 grams of crude oil product and 28 grams of flue gas per gram of complete product. The total gas system collected contained per mole of gas. 0.16 moles of hydrogen, G.G45 moles of carbon dioxide, and G G25 moles of q and c_Q hydrocarbons, measured in gc / ms. The remainder of the gas is 2 methane, air, carbon dioxide, and trace amounts ( 0 · 004 mole) of evaporated crude oil products. Crude oil products are analyzed using a combination of gas chromatography and mass spectrometry. Crude oil products contain hydrocarbon mixtures with a boiling range of 538.538 Υ. Total liquid product mixture is per gram of mixture Contains 0 006 g of ethylbenzene (monocyclic ring compound with a stagnation point of 136.2 oc at 0 · 101 MPa). This product has not been measured in crude oil feeds. Used catalyst ("First used catalyst,") Remove from the reactor, weigh, and analyze. The first The weight of the used catalyst increased from 3 丨 · 6 grams to a total weight of 37.38 grams (based on the original K2C03 / Rb2C〇3 / Cs2c03 catalyst weight, an increase of 18% by weight). This first used Per gram of used catalyst contains 0.15g of extra coke, 0.00035g of sulfur, 〇__g Ni / V and 0.845g of K2C〇3 / Rb2C〇3 / Cs2C 〇3. The additional crude feed (152.71 grams) was contacted with the first used catalyst 107 200535232 (3 6.63 grams) to make 150 grams of recovered complete product after loss. The complete product was 0.92 grams of liquid crude product per gram of complete product, 0.058 grams of extra coke and 0.07 grams of gas. The gas system contains 0.18 moles of hydrogen, 0.07 grams of carbon dioxide and 0.035 moles of CfC6 hydrocarbons per mole of gas. The remainder of the gas is methane, nitrogen, some air, and traces of evaporated petroleum products (&lt; 1% mole). This crude product contains a hydrocarbon mixture with a boiling range of 100-538 ° C. Part of the mixture whose boiling range is below 149 ° C is 0.018 mol% ethylbenzene, 0.004 mol% methylbenzene, 0.03 mol% m-xylene and mol per mol of total liquid hydrocarbons. · 060 mole% of para-xylene (monocyclic ring compound with a boiling point below 149 at 0.101 MPa). These products were undetectable in the 50-Hai crude oil 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 3 6 · 63 to 45.44 g. Total weight (based on the original K2C03 / Rb2C03 / CS2C03 catalyst weight, an increase of 43% by weight). The second used catalyst system contains 0.32 grams per gram of the second used catalyst Of coke, 0.001 g of sulfur, and 0 φ g. An additional crude oil feed (104 g) was contacted with the second used catalyst (material.g) to obtain per gram of crude oil feed. 104 g of the complete product was collected and 0.04 g of coke was collected. Since 1 44.1 g of the 133 g of crude oil feed was a crude oil feed, a part of the coke was attributed to the Coke formation caused by overheating the addition of a container. The complete product is composed of 0.86 grams of crude oil products and 108 200535232 0.025 grams of hydrocarbon gas per gram of complete product. The total gas system contains 0.88 moles per mole of gas. Hydrogen, 0.052 moles of carbon dioxide, and 03 moles of CfC: 6 hydrocarbons. The rest of the gas is scorched, air, monoxide , Hydrogen sulfide, and a small amount of evaporated petroleum. The crude oil product contains hydrocarbons with a boiling range of 100-538 ° C. The mixture with a boiling range of less than 149 partially contains 0.021 grams of ethyl per gram of hydrocarbon mixture Base benzene, 027 g of toluene, 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,% weight, and then analyzed. The weight of the third used catalyst was increased from 44 84 g to 56.59 g Total weight (based on the weight of K2C03 / Rb2c03 / Cs2C0 ^ media, an increase of 79% by weight). Detailed elemental analysis of the third used catalyst. The third used catalyst The catalyst system contains Γ · Γg of carbon, ° · 28g of chlorine, 0. ° 025g of oxygen, 0deck of melons, 0.017g of nitrogen, and 0.0018g of vanadium per gram of extra substance.

Grams of iron and 0._25 grams of chloride ions such as chromium, titanium and knots. /, Yu h is other transition metal, π, factory / 1 is over shoulder, coke, sulfur and / or metal deposited in inorganic thorium does not affect the contact through the original: or in the presence of inorganic salt catalyst Produced: The feed and hydrogen source are at least in contact with the test. The crude oil product has a monocyclic aromatic compound content in the 14 ^ distribution with a boiling range that is twice the boiling range of the crude feed monocyclic ring M. The content of the compound is at least 109 200535232. The yield of the crude oil product (based on the amount of crumbs, wafers, and cymbals) is δ9. The weight of crude oil is 7.5% by weight. Weight basis), care standard: difference ^ 2.7% 'and the average weight yield of gaseous 1 detoxification is J% (based on the weight of the oil feed), and the standard deviation is 0 ·. : The larger standard deviation of both bulk and coke is due to the third test °:

&amp; caused by excessive heating of crude oil in the container. Even &amp;, even the large amount of coke tested here, has no significant significant adverse effect on catalyst system / tongue properties. The ratio of C2 olefins to total q is 019. The ratio of q olefins to total q is 0.4. The ratio of α-baked to intramolecular dilute hydrocarbons of type C4 fe is 0 6 1.匸 The cis / trans olefin ratio is 6.34. This ratio is considerably higher than the predicted 4 thermodynamic C4 cis / trans-olefin ratio of 068. The ratio of A hydrocarbons to olefins in the molecule is 0.92. This ratio is greater than the predicted ratio of thermodynamic α-olefins to olefins in I molecule. The C5 cis / trans olefin ratio was i · 25. This ratio is larger than the predicted thermodynamic c5 cis / anti-lean hydrocarbon ratio of 0-9.

___ ϋ—: Crude oil with a relatively high sulfur content is expected to be in contact with the Weng Ji A catalyst. The setting and reaction steps are the same as those described in Example 9. Feed into the reactor. The amount of feed in the reactor was monitored using changes in the weight of the reactor. Phenane gas was continuously metered into the reactor at 500 cm V. Steam was continuously metered into the reactor at 6 g / min. The inorganic salt catalyst was prepared by combining 27.2 grams of K2C03, 32.2 grams of Rb2C03, and 40.6 grams of Cs2C03. The K2C03 / 110 200535232

Rb2co3 / Cs2co3 catalyst (59.88 g) was charged into the reactor. Badan heated a crude oil feed with an API specific gravity of 9.4, a sulfur content of 0.02 g of sulfur, and a residue content of 0.40 g per gram of crude oil feed (asphalt, Romming, Canada, "Inch Area") in a heating vessel To 150. The hot bitumen was continuously metered from Tianli Gujie to the reactor at 10.5 g / min in an attempt to maintain the crude oil feed level at 50% of the reactor volume. However, This rate is not sufficient to maintain the liquid level. The methane / steam / crude oil feed is in contact with the catalyst at an average internal reactor temperature of 456. The contact between the formazan / steam / crude oil feed and the catalyst yields Lu 70 Product (in this example, in the form of reactor effluent vapors). A total of 640 grams of crude oil feed was processed during 6 hours. The difference between the initial catalyst reset and the weight of the residue / catalyst mixture is known Each gram of crude oil feed had 0.58 grams of coke burn left in the reactor. From the contact between the crude oil feed and methylbenzene in the presence of ICCVRlCCCCsfO3 catalyst, 0.93 grams of crude oil was produced per gram of crude oil feed. Complete product. The complete product contains 0.03 grams of gas per gram of complete product; fn 0.97 The crude oil product: ^ includes the amount of methane and water used to react in the spring. The gas system contains 0.014 grams of hydrogen per gram of gas, 0.018 grams of monoxide, 0.08 grams of carbon dioxide, 0.13 grams of sulfur Hydrogen and 0.68 grams of non-condensables. From the amount of hydrogen sulfide produced, it can be estimated that the sulfur content of the crude feed was reduced by 18% by weight. As shown in this example, there are hydrogen, carbon monoxide, and carbon dioxide Produced. The molar ratio of carbon monoxide to carbon dioxide is 0.4. C2 ~ C5 hydrocarbons contain 0.30 g of C2 compounds per gram of hydrocarbons. 111 200535232 g of C3 compounds and 0.26 g of C4 compounds And 010 grams of the q compound. The weight ratio of isopentane to n-pentane in non-condensable hydrocarbons was 0.3. The weight ratio of isobutane to n-butane in non-condensable hydrocarbons was 0 · 丨 89. This C4 compound has a butadiene content of gram per gram of compound I. The weight ratio of aC4 olefin to intramolecular C4 olefin was 0.75. The weight ratio of olefin to c5 olefin in the molecule was 1.08. The data in Example 25 confirm that continuous processing of a relatively high sulfur crude oil feed with the same catalyst in the presence of coke has not impaired the activity of the inorganic salt catalyst 'and produced a crude product suitable for transportation. ❿: Crude oil feed and hydrogen source are at / Cs? CO, and the contact and device and reaction steps are performed under the conditions described in Example 26. The K2C03 / Rb2C03 / CS2C ... catalyst (56 · 5 g) was filled into the responder. A total of 2 $ 500 grams of crude oil feed was processed over a 6 hour period. From the difference between the weight of the starting catalyst and the weight of the residue / catalyst mixture, it is known that based on the weight of the crude oil feed, 4 g of coke per gram of crude oil feed remains in the reactor. Each gram of crude oil feed produced a total of 089 grams of complete product. This complete product is a product containing 0.001 grams of gas and 0.96 grams of crude oil per gram of complete product, excluding the amount of hexane and water used in the reaction. The gas system contains 0.021 grams of hydrogen, 0.018 grams of monoxide, 0.052 grams of carbon dioxide, 0.18 grams of hydrogen sulfide, and 0.65 grams of non-condensable hydrocarbons per gram of gas. From the amount of hydrogen sulfide produced, it can be estimated that the sulfur content of the crude oil feed was reduced by 14 weight s%, which is based on the weight of the crude oil feed. As shown in this embodiment, hydrogen, carbon monoxide, and carbon dioxide are generated. The molar ratio of carbon monoxide to carbon dioxide is 0.6. The C2-C6 fe class is a mother gram C2-C6 fe class including 0.44 g of a C 2 compound, 0.3 g of a C3 compound, 0.19 g of a C4 compound, and 0.068 g of a compound. The weight ratio of isopentane to n-pentane in non-condensable hydrocarbons was 0.25. The weight ratio of isobutane to n-butane in non-condensable hydrocarbons was 015. The C4 compound has a butadiene content of 0.0003 g per gram of the I 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 light of this description, modifications and substitutions of specific examples 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 scope of the following patent applications. [Brief description of the drawings] The advantages of the present invention will be more clearly understood by those with ordinary knowledge in the technical field to which the present invention pertains after the above detailed description and reference to the attached drawings. Figure: 113 200535232 Figure 1 is used for A schematic illustration of a specific example of a contact system for contacting a crude oil feed with a chlorine source in the presence of one or more catalysts to produce a complete product. Figure 2 疋 Schematic diagram of 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 0 Figure 3 is a combination of a contact system Fig. 4 is a schematic diagram of a specific example of a blending zone combined with a contact system. Fig. 5 is a schematic diagram of a specific example of a separation zone, a contact zone and a junction zone. Fig. 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. Fig. 8 is a list of crude oil feed properties and crude oil product properties obtained from a specific example of contacting a crude oil feed with a transition metal sulfide catalyst. Figure 9 is a list of crude feed composition and non-condensable hydrocarbon composition obtained from a practical example of contacting a crude feed with a transition metal sulfide catalyst. Figure 10 is a list of properties and composition of crude oil products obtained from a specific example of contacting a crude oil feed with a transition metal sulfide catalyst. Fig. 11 is a graph plotting log current of ion current versus temperature of inorganic salt catalyst exhaust gas as measured by TAP. Fig. 12 is a graph plotting log 10 of temperature versus temperature of an inorganic salt catalyst and an inorganic salt versus potassium carbonate resistance.

Figure 13 is a diagram of the Na2C (VK2e (^ / R 114 200535232) catalyst resistance versus temperature of 10g and 10 versus potassium carbonate resistance. Figure 14 is a graph of coke, liquid hydrocarbons, and gases versus The specific example of the hydrogen source produced by contacting the material with the inorganic salt catalyst is shown in Figure 7TΓ. Figure 15 is a specific example of the contact between the crude oil feed and the unshielded shield and the mountain ridge A A graphical representation of the weight percent of the crude oil product coated by the example versus the carbon number. Figure 16 is a list of ingredients made from a specific example of contacting a crude feed with an inorganic salt catalyst. Π or a siliconized silicon

Although the present invention is apt to have various modifications and specific examples shown in the drawings as examples, and ^, it will be specifically described. The drawings may not be drawn to scale. It should be understood that the detailed description herein is not intended to limit the present invention to the particular forms disclosed and their details The present invention is intended to cover equivalents and alternatives which fall within the spirit of the invention All changes of the door, M [Description of main component symbols] 100 Contact system 101 Crude oil feed supply 102 Contact zone 104 Conduit 106 Circulating conduit 108 Conduit 110 Flow control valve 110 'Flow control valve 112 Gas inlet π 115 200535232 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 conduit 152 Conduit 154 Conduit 156 Quartz Vessel 158 Sample

116 200535232 160 Power supply 162 Metal wire 164 Metal wire 166 Meter 168-170 Ion current vs. temperature 172-180 Resistance curve vs. temperature 182-184 Relative resistance curve vs. temperature 186-188 Weight% 190-192 Weight% of liquid hydrocarbons 194-196 Weight% of gas 198-200 Graph of carbon number distribution

117

Claims (1)

200535232 10. Scope of patent application: μ million method, which includes 1. a cracking source makes the crude oil feed and hydrogen source contact in the presence of M spoon ^ m…, desalting catalyst to make the complete product of 3 crude oil The product, 苴 MPa, is called Dingren /, and the crude product is at 25. (: Condensable with 0.10 MPa), the original Gullu, Xingzhan u Jinke has a residual content of at least 0.2 grams of residual product from the mother gram of crude oil feed, and the beneficial machine ',,, Desalting catalysts show turning points for stomata that drain stomata in the range between 50 ° C and 500 ° C, as determined by the product's Sunwatch Analysis (TAP); and ^ The contact conditions of the industrial system make the crude oil production site have a residue content of at most 30% of the crude oil feed owing residue and i, and the number of residues is expressed in grams of the crude oil product. As determined by astm method D5307. 2. A method of 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 comprising a crude product, wherein the crude product is liquid at 25 and palpitation MPa The crude oil feed has a residue content of at least 0-2 grams of residue per gram of crude feed, as determined by ASTM method D5307, and the inorganic salt catalyst exhibits a value of 50. Exhaust gas inflection point of exhaust gas in the temperature range between 〇 and 50000c, as determined by product transient analysis (TAp); and the production of the crude oil product such that the crude oil is produced at a measurement volume of 25 and 0.101 MPa The volume of the product is at least 5% greater than the volume of the crude feed. _ 3. As for the method in the first or second scope of the patent application, the contact conditions are also controlled so that the contact temperature is above Tm, where Tm is below the temperature of the inorganic salt contact 118 200535232 medium TAP. And the temperature of the TAP is the temperature at which the exhaust gas is turned off. ^ "U« Show the lower temperature of the U. The method of any one of the items in the scope of patent application 帛 η, wherein the discharged milk The body is water vapor and / or carbon dioxide. 5. A method for producing 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 of the crude oil product, wherein the crude oil The product is liquid at h and 010 MPa. In this case, the crude oil feed has at least 0.2 grams of residue per gram of crude oil feed, 杏 杏 1 2 3 ^^ contains $, and the inorganic salt catalyst has a value of 200 and Thermal transitions in the temperature range between 500 C, as measured by differential scanning calorimetry (Dsc) at a rate of 4 ° C per minute; and control of the contact conditions so that the crude oil product has at most the residue content of the crude feed. The residue content of 30% is expressed in grams of residue per gram of crude product, wherein the residue content is as determined by ASTM method D5307. 6. The method of applying patent scope 帛 5 X member, wherein the thermal transfer of the inorganic salt catalyst, the temperature range of 250-450 ° C or 300-400 ° C Internal 0 119 1. The method according to any one of claims 1 to 6, wherein the 2 inorganic salt catalyst comprises one or more alkali metal carbonates, one or more alkaline earth metal carbonates, one or more alkali gold Layer hydroxides, one or more alkaline earth metals3 hydroxides, one or more alkali metal hydrides, one or more alkaline earth metal hydrogen ^ or one or more sulfides of metals, one or more soil tests4 , Or sulfides, one or more metallurgical women or one or more ammonium amines of alkaline earth metals, or mixtures thereof. 200535232 The method according to item 7 of the scope of the patent application, wherein the one or more metals are sodium, unload, hammer, or a mixture thereof, and / or the one or more metals are # 5, thorium or a mixture thereof. 9. The method of any one of item (1) of the scope of claim 4, whose source includes hydrogen, light hydrocarbons, water, or a mixture thereof. / 、 To 10 · If the method is in any one of the scope of the patent application, a small part of the complete product is made by steam, and the method advances :: 25: and-condensed at least-heart ^ ... i: For example, the method of any one of items 1 to 10 in application f and the scope of interest, wherein the contact of the raw and feed lice sources in the presence of an inorganic salt catalyst is in the contact area in the contact area. -The method of supplying steam to the crude oil during the contact-or-period ::: special: dry-enclosing any one of items 1-11, in which it is impossible. The mother gram crude feed contains ㈣ · 2.0 · 99 g or. 3.8 grams 13. If the scope of the patent application is 任 any of the workers-the ^ empty contact conditions make: during this contact more and more. · 2 grams, at most ... grams, at most. · I grams or to and. Addition of non-condensable hydrocarbons ;: · 5 grams in the person.乂 As determined by mass balance, the method of any one of item H3 in the patent application range, wherein the crude oil feed also has a number or heteroatoms. ^ The parent sees the total expressed in grams of Nl / V / Fe grams of crude oil feed. / Fe content and total heteroatom content, 120 200535232 and also control the contact conditions so that the crude oil product also has a TAN of the crude oil feed, a total Nl / V / Fe content and / or a TAN of the total heteroatom content , Total Nl / V / Fe content and / or total heteroatom content. 〇15. According to the method of any one of the "4 workers" in the scope of patent application, the 6 Hai crude oil product also contains 0.0000 〇ιι_〇2 grams of _ per gram of crude oil product, from 0.0001_0 • 9 grams of distillate, 0 0001 second oil, mixture. i. The real gas oil of i or its 16. The method of any one of claims 15 to 15, wherein the method further comprises combining the crude oil product: raw materials from crude oils of the same or different feeds to form A blend. A 17 · crude oil product or blend, which can be obtained by the method of any one of the 16 patent claims. Have 1δ · — a crude oil product, wherein the crude oil product is 4 per gram of crude oil product Residues to f 0.05 gram, at least 1 gram of hydrocarbons at 0.1 () 1 MPaT boiling range @ ㈣ ° C (4007) as measured by the ASTM method; / at least 0.001 gram at 0.101 The boiling range is distributed at 204 at MPa. Hydrocarbons between 300 ° C and 300 ° C; boiling range of at least 0.001 g at 0.101 MPa is 300. And 400 Qc hydrocarbons; at least grams of boiling range at 0.11 MPa distributed in the weight. Hydrocarbons between 538 ℃ (〗, _ 〇F); and the smoke ratio in which the boiling range is distributed between 2G2G4 QC € 121 200535232 and the molar ratio of dilute hydrocarbons with internal double bonds is at least Among them, it has a terminal double bond of 0.4, as determined by ASTM D6730 with an olefinic olefin having a terminal double bond and an internal double bond. 2. The 18 crude oil products claiming that the patent is dry and solid, in which the Jiteng range is distributed at 20. (： 金 ο ”Hydrocarbons between 204 ° C are distributed between 200 ℃ and 204 〇 ** per gram of boiling range. Hydrocarbons contain 0.001 ~ 0.5 grams of olefins. Crude oil Product, each gram of crude product containing .05 grams of residuals, as determined by ASTM method D5307, and At least 0 · 0 0 1 square, so dizzy. Brother 0 / Futeng has a warp-type mixture distributed between 20 ° C and 538 ° C (1,000), as measured by the ASTM D5 tear method, and the mixture contains per gram of the mixture: at least 0.001 grams of chain-burned hydrocarbons, as measured by ASTM method 0673, 0.001 grams of olefins, as measured by ASTM, / 丄 uo / JU f / r And / ene olefins contain at least 100,000 grams of terminal olefins as determined by ASTM method D6730; at least 0.001 grams of light oil; 0.001 grams of kerosene, which contains at least grams of aromatic compounds per gram of kerosene ^ As measured by ASTM method D5186; ^ J 〇.001 grams of diesel oil, which contains at least 0.3 grams of aromatic compounds per gram of diesel oil, such as those measured by Ip method 368/90 and vg 〇 to ^ 001 grams of vacuum gas oil (VGO), the VGO system has at least 0.3 grams of aromatic compounds per gram, such as the IP method 3 68/90 122 200535232 tester. The crude oil product such as the 20th in the scope of the patent application, which makes the hydrocarbon content of the hydrocarbon mixture in the range of 0.7 g to 98 g. 22. A crude oil composition containing at least 0.001 per gram of composition and a distribution of 'Futten range up to 204 0c (400) at 101 MPa. Hydrocarbons, at least 0.001 g of hydrocarbons with a boiling range distributed between 204 ^ and 300 ° C at 0.101 MPa, at least 0.001 g of boiling depleted at 300 ° C with a boiling range . (: Hydrocarbons between 400 ° C and at least 001. gram boiling range distributed at 400 at 0.101 MPa. (: Hydrocarbons between 538 γ (1,000), And the boiling range distribution is up to 204. The hydrocarbon content of 匸 contains isoparaffins and normal paraffins, where the weight-to-weight ratio of isoparaffins to normal paraffins is at most 1.4, as determined by ASTM method D673. 23 A crude oil product containing, per gram of crude oil product, a residue of up to 0.05 g, as determined by ASTM method D5307; and . At least 0,001 grams of hydrocarbons with a boiling range distribution of at most 204 C (400) at 0.101 MPa; at least o.ool grams of boiling ranges at about 40 c and about 300 at 0101 MPa. Hydrocarbons between π; at least 0.001 g of boiling range distributed at about 3 ⑽ at 0101 MPa. Hydrocarbons between C and about 400 ° C; and, at least 0.001 g has a boiling range distribution of about 4,000 c and about 538 at 0.101 MPa. (: Hydrocarbons between (!, 〇〇〇〇 叩), as measured by the AStm method MM ?; and 123 200535232 in the boiling range distribution of about] G ° c and about. The hydrocarbon b 3 compound with an inverse number of 4 (c4) is compounded into the compound 4 and the parent compound is C4. The compound 3 has at least 0.001 g of butadiene. 24. Such as the scope of the patent application, 23 crude oil products , Where the butadiene is at least 0.005 grams. 25. As the crude oil product of any one of the 17th item of the scope of the patent application, the weight of atomic hydrogen to atomic carbon of the emu oil product (MH / C) is to the eve 1 · 8 〇 26: For example, the crude oil product of any of claims 17-25 in the scope of the patent application, Cao, and the oil product has an API ratio Z and medium API specific gravity at 15.50 ° C in the range of 15 to 30 as determined by the astm method D6 milk By. 27. The crude oil product according to any of the claims in the scope of application for fπ%, the oil product contains 0.00001-0.03 grams or 0.0000 g-0.00 g of coke per gram of crude oil product. 〆 square, 8 · types of manufacturing transportation fuels, heating fuels, lubricants or chemicals \, Which includes processing of crude oil products or blends as described in any of claims 17-27 of the scope of the patent application. With 29. As claimed in the patent scope 请 28 method, wherein the processing includes winter ※ crude oil product or the blend is distilled into one or more fractions. 30. The method of claim 28 or 29, wherein the processing includes hydrotreating. XI. Schematic: as next page 124