TW200530389A - 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

200530389 IX. Description of the invention: [Technical field to which the invention belongs] This invention relates generally to systems and methods for processing crude oil feeds, and to compositions made using such systems and methods, for example. In more detail, the specific examples described herein are related to converting a crude oil feed with a crumb content of at least 0.2 grams per gram of crude oil per gram into a liquid mixture at 25 ^ and 0 ^ And (b) there are systems and methods for improving crude oil products with one or more properties f compared to the same properties of the crude feed. [Prior Art] Crude oils that have one or more inappropriate properties that do not allow crude oil to be economically transported or processed using traditional facilities, are commonly referred to as, "disadvantaged crudes". Famous crudes often contain high levels of residue. Class $ crudes 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. Alternatively, high-residue crude oils are typically treated with water at high temperatures to produce less viscous crude oils and / or crude oil mixtures. 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 oil may contain hydrogen deficient hydrcarbons. When processing depleted hydrocarbons, it is often necessary to add a consistent amount of hydrogen, especially if unsaturated fragments are produced due to the cracking process:. Hydrogenation during processing usually involves the use of active hydrogenation catalysts, and it may be necessary to suppress the formation of coke from unsaturated fragments. The production and / or transportation of hydrogen to a processing facility is expensive. 200530389 Coke can be formed and / or deposited quickly during the processing of inferior crude oil. To regenerate Beishan, _ "The catalytic activity of regenerating the catalyst that is burnt and mischievously dyed can be… The high temperature used during regeneration may also weaken the catalyst or degrade the catalyst. Prolonged crude oil may contain fuel to feed crude oil Total acid value ("D is said to be an acidic component. Secondary spinning with a fairly high TAN; § a bit +, /,, p_ A and other, and crude oil can lead to the formation of metal components during the transportation and / or processing of inferior crude oil. Knife corrosion. Removal of acidic components from inferior crude oil can include neutralizing acidic components with various bases to reduce the acid content. Alternatively, anti-corrosion can be used in transportation equipment and / or processing equipment. Money metal. The use of anti-corrosion genus usually involves the use of special metals. The use of metal in existing equipment may not be universally acceptable. Another method to suppress corrosion May involve the addition of corrosion inhibitors to inferior crude oil and / or “T 1,” or the reduction of force. The use of rot inhibitors can adversely affect the processing of crude oil. Equipment and / or products made from the crude oil Inferior crude oils may contain metal contaminants such as nickel, vanadium, and / or iron that are compatible with Gudan Xiangtianhari. During processing of such crude oils, compounds that are 3 dyes and / or 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 oil usually includes hetero-atoms (such as sulfur, oxygen and Nitrogen). Organically bound heterobromide Agan + also atoms may have adverse effects on catalysts in some cases. Alkali metal salts and / or alkaline earth metals II have been used in the process of desulfurization of residues. These procedures are prone to cause poor people ’s rate of stone removal, produce oil-insoluble sludge, poor metal removal efficiency, # + Kai Xicheng inseparable salt-oil mixture on bebe, use a large amount of Hydrogen / oxygen / fourteen meters fart rolling and / or equivalent hydrogen pressure. 200530389 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, Adding a diluent usually causes The cost of thinners and / or the cost of managing inferior crude oils increases, which increases the cost of processing inferior crude oils. Adding diluents to inferior crude oils may in some cases reduce the stability of such crude oils. The following US Patent number: 3,13ό 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 .; McCollum et al. 3,9605706; awarded to

3,960,708 by McCollum et al; 4,1 19,5 28 by Baird, Jr and others; 4,127,470 by Baird, Jr. and others; 4,224,140 by Fujimori et al; and 4,437 by Heredy and others , 98〇; awarded

4,591,426 by Krasuk et al; 4,665,261 to Mazurek; 5,064,523 to Kretschmar et al; 5,166,118 to Kretschmar et al; 5,288,681 to Gatsis; 6,547,957 to Sudhakar et al; and υ Δ • Public application publication number: 20030000867 issued to Yi and 2003i493i7 issued to Rendina, describing various methods and systems for processing crude oil. However, the methods, systems, and conflicts described in these patents have limited applicability due to the many technical issues mentioned above. In short, high residues, a tendency to measure hydrogen (such as inferior crude oils generally have unsatisfactory properties) (eg, a tendency to corrode equipment, and / or consume considerable amounts during processing). Other undesirable properties include Quite a high amount of unwanted: quite high TAN, organic-bonded heteroatoms and / or gold 200530389 (genus / 5 " ^)). This type of property creates problems in traditional transportation and / or handling facilities, including increased ammonia use during increased decay. = Reduced catalyst life and / or have more desirable properties in processing ... For improved systems, methods and / or catalysts used to convert inferior crude oil into products with /, 'products, there are obvious economic and technical demand. [Summary of the Invention] The invention described in this article is generally related to the use of one or more catalysts to contact crude oil feeds to produce encapsulation ^ 3 crude oil products and, in some specific examples, the completion of non-condensable gases + System and method of private products. The invention described herein also broadly relates to the composition of Langzhong and ancient ^ ^ with a combination of novel ingredients. Such compositions can be obtained by the systems and methods described herein. 2. Good crude oil provides a method for producing crude oil products, which includes contacting crude oil with a hydrogen source in the presence of-or a plurality of catalysts to produce crude oil products, wherein the catalyst-or more Catalyst. Tsukizuki also provides a method of making a crude oil product, comprising: contacting a crude oil feed with a hydrogen source in the presence of one or more catalysts to produce a complete product comprising the crude oil product, which brings the crude oil product at 25. . And 0. ΗΗ is a liquid mixture, at least one of the catalysts contains one or more transition ^ claw compounds, and the crude oil feed has a residual fish content of at least 0.2 grams of residual edge per gram of crude oil feed, such as ^ Measured by the top method; and controlling the contact conditions so that the crude oil product contains 0.05 mg per gram of crude oil product, and the crude oil product contains at least 0.001 g of car per gram of crude oil product. Stem oil 'while the light oil has an octane number of at least 70. The present invention also provides a method for preparing a crude oil product, comprising: contacting 200530389: an oil feed with a hydrogen source in the presence of-or a plurality of catalysts, a complete product of a crude oil product, wherein the crude oil product is at 25:

¥ is a liquid mixture, at least one of the catalysts contains multiple = metal sulfides, and the crude oil feed has a residual content of at least H residues per gram of crude oil feed, as described in ASTM method D; and ^ The contact conditions are such that the crude oil product of the Nigerian, Russian & Seventh Aberdeen crude oil contains kerosene, which is an aromatic compound of 3 ^ 0.2 g per gram of kerosene, as determined by ASTM method D5186. The freezing point of at most _3 (QC temperature), as determined by AS · D2386, and the crude oil product is at most 0.05 g of coke per gram of crude oil product. The 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 cc and MPa Is a liquid mixture, at least one of the catalysts contains one or more transition metal sulfides, and the crude feed has a residue content of at least 0.2 grams of residue per gram of crude feed; and controlling the contact conditions such that the crude product A gram of crude product contains at most 0.05 grams of coke, wherein the weight ratio of atomic hydrogen to atomic carbon in the crude product is at most h75, as determined by ASTM method 0673. 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 cC and 0 〇1 Mpa is a liquid mixture. At least one of the catalysts contains one or more transition monoxide & compounds, and the Haihai crude oil feed has a residue content of at least 0.2 grams of 200530389 residue per gram of crude oil feed, such as As determined by ASTM method 0507, and the weight ratio (H / c) of atomic hydrogen to atomic carbon in the crude oil feed is at least 15; and the contact conditions are controlled so that the crude oil product has the atomic H / The atomic H / c ratio of c ratio, the crude oil product has a residue content of at most 3G% of the crude oil feed residue content. As determined by ASTM, crude oil products contain at least grams of light per gram of crude oil product. Oil, and the light oil has an octane number of at least 70. The present invention also provides a method for manufacturing a crude oil product, comprising: contacting a crude oil feed with a hydrogen source in the presence of-or a plurality of catalysts; and secondly manufacturing a complete product comprising a crude oil product, wherein the crude oil product is at 25 γ and γ. .10 MPa is a liquid mixture, at least one of the catalysts: · one or more transition metal & compounds are included in the catalyst, and the crude oil feed has at least grams of residual residue content per gram of crude oil feed, such as Measured by ASTMD5307 household weight; and control the contact conditions so that the crude oil product contains at least ㈣i: light oil per gram of crude oil product, the light oil has a scorch value of at least 70; at least 0 001 grams of kerosene ', the kerosene contains Aromatic compounds, the kerosene system contains up to 〆 · 2 grams of aromatic compounds per gram of kerosene, as measured by ASTM method D5i86, and rust kerosene has a temperature of at most · 300 ° C.

J breaking point, such as measured by ASTM 2 2386 kg; at least 0.001 grams of vacuum gas oil (0), the VGO system contains at least 0.3 compound per gram of VG, such as IP method 368 / 90; and up to 005 rule 7. The present invention also provides a method for producing a crude oil product if the present invention is difficult, which comprises: contacting a crude oil feed with a hydrogen source in the presence of one or more catalysts containing a transition metal sulfide catalyst 200530389 to produce The complete product of a crude oil product, where the crude oil product is a liquid mixture at 25 ° C and 0.101 Mpa, the transition to the metal catalyst system contains at least 0.4 grams of a per gram of total transition metal sulfide catalyst or A variety of transition metal sulfides, the crude oil feed has a residual fish content of at least 0.2 grams of residue per gram of crude oil feed, such as the 卩 ASTM method

The tester and the contact conditions are controlled so that the crude oil product has at most G Q5 g of coke per gram of raw and product 3, and the crude oil product has a residue content of 30% of the crude oil feed residue content, such as Tested 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—or a plurality of horns containing a transition metal sulfide catalyst—to produce a complete product containing the crude oil product, wherein Crude products are at 25. (: With 0.11 Mpa is a liquid mixture, the

The metal sulfide catalyst system contains a total of at least 0.4 grams of transition metal sulfide per gram of total transition metal sulfide catalyst, and the crude oil feed has an atmosphere of ^ 1 000 nitrogen per ^ crude oil feed. Content, and the crude oil feed has: a gram crude oil feed of at least 0.2 "residue content of the residue; and controlled contact pieces, so that the crude oil product has at most 90% of the nitrogen content of the crude oil feed

The nitrogen product has a residue content of at most 30% of the content of the crude oil feed residue, where the nitrogen content is as measured by the astm method 'and the residual fish content is as measured by the ASTM method D53q7. 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 11 200530389

The 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 0.001 grams of residue per gram of crude oil feed. '· And controlling the contact conditions so that the crude oil product contains at most 0.05 g of coke per gram of crude oil product, and the crude oil product has a total Ni / V / Fe content of at most 90% of the crude feedstock / V / Fe content The crude oil product has a residue content of at most 30% of the content of the crude oil feed residue, and the content of v / Fe is as measured by the ASTM method, and the residue content is as measured by the ASTM method D5307. Measured by. The present invention also provides a method for manufacturing a crude oil product, which includes " contacting a crude oil feed with a hydrogen source in the presence of a horn containing a transition metal sulfide catalyst to produce a complete product including a crude oil product, which " Crude product at 25 .; . It is a liquid mixture with 0.11 Mpa. The metal sulfide catalyst contains a total of one gram of total transition metal sulfide catalyst per gram.

Less than 0.4 grams of one or more transition metal sulfides, the crude oil feed has at least 10,000 grams of crude oil feed, and the stone claws of Shikshiwa are contained, and the crude oil feed has a shoulder The mother gram crude oil is fed with at least 0_2 grams of residual fishery containing conditions, so that the crude oil product has a sulfur content of 70%, and a sulfur content of 70% of the sulfur content of the crude oil feedstock. It has a residual content of at most 30% of this, where the sulfur content is as measured by ASTM method D429 and the residual content is as measured by astem ^. The invention also provides a 12 200530389 method for manufacturing a transition metal sulfide catalyst composition, which comprises: mixing a transition metal oxide with a metal salt to form a transition metal oxide / metal salt mixture; and making the transition metal oxide The / metal salt mixture is reacted with hydrogen to form an intermediate; and the intermediate is reacted 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 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 0.101 Mpa. The transition metal sulfide catalyst contains transition metal sulfides. The crude oil feed has a residual content of at least 0.2 grams per gram of crude oil feed. Measured by astm method D5307; control the contact conditions so that the crude oil product has a residue content of at most 30% of the crude feed residue content; and wherein the transition metal sulfide catalyst system is obtained as follows: the transition metal oxide Mixed with a metal salt to form a transition metal oxide / metal salt mixture; reacting the transition metal oxide / metal salt mixture with hydrogen to form an intermediate; and interposing the 'intermediate with sulfur in the presence of one or more hydrocarbons Reaction to produce a transition metal sulfide catalyst. 'The present invention also provides a method for manufacturing a crude oil product, comprising: contacting a crude oil feed with a hydrogen source in the presence of-or a plurality of catalysts, to complete a complete product of the crude oil product by dreaming, wherein the crude oil is at 25 γ i Q1 ¥ is a liquid mixture, and the crude oil feed contains 0.2 grams of residue per gram of crude oil feed, as determined by the eight rules; the partial complete product is made into a vapor; at 25. 〇 和 〇ι〇ι coffee; 13 200530389 at least the steam; and the formation of a crude oil product, wherein the crude oil, the product is per gram of crude oil product contains: at least 100,000 grams of light oil, the light oil has An octane number of at least 70; at least 0 001 grams of VGO, which contains at least 0.3 grams of aromatic compounds per gram of VGO, as determined by the ιρ method 368/90, and at most 0.05 grams of residue , As measured by ASTM method D5307. The present invention also provides a method for manufacturing a crude oil product, comprising: contacting a crude oil feed with a hydrogen source in the presence of an inorganic salt catalyst to produce a complete product comprising a crude oil product, wherein the crude oil feed has a crude oil feed per gram of crude oil feed Residue content to 0.2 g of residue, as determined by astm method D5307. The crude oil product is a liquid mixture at 25 and 0.101 Mpa, and the crude oil product contains at least 0.001 g of light oil per gram of crude oil product, which contains at least 0.001 g of light oil per gram of light oil. The monocyclic ring aromatic compound is 'as measured by ASTM method D6730; at least 0.001 g of distillate' and up to 0.05 g of residue, as measured by ASTM method 05307. 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 crude product, wherein the crude oil feed has per gram Crude oil is fed to a residue content of 0.20 g. As determined by ASTM method D5307, the crude oil product is a liquid mixture at 25 and 001, and the crude oil product contains per gram of crude oil product. At least 0.001 grams of diesel, and the diesel series contains at least 0.3 grams of aromatic compounds per gram of diesel, as determined by IP 3 68/90; at least 0.001 grams of vG0, and the series 14 200530389 Each gram of paste contains at least 0.3 grams of aromatic compounds, such as in the ιρ method soot = :: and up to 5 grams of residues-one-the invention also provides a method for manufacturing crude oil products, which :: feed and hydrogen The source is contacted in the presence of an inorganic salt catalyst to produce a complete product containing the original product, where the crude product is at 25 ° C. . J is a liquid mixture. 'The crude oil feed has a residue content per gram of crude oil feed = 2 2 residues, as described by As ™ Law Secretary 7, and the "' from the feed has a maximum of 0 gram per gram of crude oil feed. Ii 4 The monophonic entry of the object into the early-spreading ring aromatic compound in the contact 2 ::: the content of the material and control the contact conditions, so that

Mpa 砗 and 7 people have a total of 0.2 g at 25 ° C and 〇01, so that ::: hydrocarbons are formed as determined by the mass balance, and the crude oil product has at least 5% greater than the crude oil feed Single compound content = 1 ... "composite content 'where the monocyclic ring aromatics 3 are as measured by ASTM method D6730. Method of making crude oil products from crude oil species' which includes: contacting the secondary product of the oil product Γ Contact in the presence of a medium to produce the whole product containing the original Mg, all liquids at 1 ° C and 25 ° C with (M (HMpa g of sacrifice of ❹) dan Λ per gram of crude oil after entering the department at least 0.2, For example, according to ASTM method D5307, then-soil w _ Crude oil feed has a weight per gram of jin / 疋, and the amount; olefins expressed in grams of dilute hydrocarbons contain crude oil contact conditions, making crude oil The product has to

The heart content of Fagar's 730 series' wherein the smoke content is as measured by ASTM. 15 200530389 The present invention also provides a potential > Li crude "crude oil product method, comprising: contacting a crude oil feed with a hydrogen source under an inorganic J card to produce a complete product comprising a crude oil product, where , Night carving, "into you", the product at 25 ° C and 〇1〇1 Mpa ^ 5 # 'The crude oil feed has a residue content of at least 02 per gram of crude oil feed, and the inorganic The salt catalyst exhibits 纟 50. [The turning point of the exhaust gas of the 齑 7 body in the temperature range between 500 and 500 c, as measured by the product transient analysis (Temporal Analysis of ρ, aiyS1S 〇f PrOduCtS, TAP)

And control the contact conditions so that the crude oil product has a residual content of at most 30% of the crude feed feed residue content, which is expressed in grams per gram of crude oil product, where the residue content is as astm & d53 Fixer. ,

The present invention also provides a method for manufacturing a crude oil product, comprising: contacting a crude oil feed with a hydrogen source in the presence of an inorganic salt catalyst to produce a whole product including a crude oil product, wherein the crude oil product is under Is a liquid mixture, the crude oil feed has a residue content of at least 0.2 grams of residue per gram of crude oil feed, the inorganic salt catalyst contains at least two inorganic metal salts, and the inorganic salt catalyst exhibits a temperature range The turning point of the exhaust gas in the exhaust gas, as measured by the instantaneous product of the product (τΑρ), wherein the temperature of the turning point of the exhaust gas is between the two inorganic metal salts and the DSC temperature of one of the (b) the The DSC temperature of the inorganic salt catalyst; and the control contact conditions, so that the crude oil product has a residue content of at most 30% of the crude feed residue content, which is expressed in grams of residue per gram of crude product, where The residue content is measured by ASTM method D5307. The present invention also provides a method for manufacturing a crude oil product, comprising: contacting a 2005 200530389 crude oil feed with a hydrogen source in the presence of a blood machine_catalyst catalyst to produce a complete product comprising a raw / tritium product, wherein the shoulder Ding Da, Yuan / Yang product is a liquid mixture at 25 ° C and 0.101 Mpa. The crude oil is fed with a residue content of at least 0.2 g of residue in the crude oil feed, as determined by ASTM method 仏 ^, 沄 D5307. In addition, the inorganic salt catalyst exhibits a turning point of the exhaust gas discharged from the milk in a temperature range between 50 ℃ and 500 〇Γ々ψ, ^ α, and 500 C. ) Measured and manufactured crude oil products' such that at 2 "c and 〇i〇iMpa measured volume%, the volume of the crude oil product produced is at least the expected volume. / 0 A million, crude oil, 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 containing a crude oil product, wherein the shoulder crude product is at 25 ° C and 0 · Liquid mixture at 101 Mpa, the crude feed There is a content of at least 0.2 H in the mother gram crude oil feed, and the inorganic salt catalyst exhibits a determination at 5 盘 mesh and 冲 analysis (TAP); the contact conditions are made in ^. &Amp; Each gram of crude oil feed has at most 0.2 grams of cyanine. Hour C and 0.101 Mpa are formed of non-condensable hydrocarbons, as determined by mass balance. The present invention also provides a method for manufacturing crude oil products, including: The raw material was contacted with a nitrogen source in the presence of an inorganic salt catalyst to produce a complete product containing raw material: wherein the crude oil product was at 25 ° C and 0.001 finely liquid mixture. The crude oil feed had per gram Crude oil feed has at least the residue content of the residue, and the helmet is in contact ... The solitary catalyst has a thermal transition in the temperature range between 200 ° C and 500 °, such as radon by differential scanning calorimetry 17 200530389 (Ca) measured at a rate of 10 per minute; and controlling the contact conditions so that the crude oil product has a residue content of at most %% of the crude feed residue content, which is based on the residue per gram of crude product The gram number indicates that the residue content is Measured by ASTM method D5307. 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 comprising a crude oil product, wherein the The crude oil product is a liquid mixture at 25.0 and 0,001. This crude oil feed has at least one gram of crude oil feed.

The residue content of grams of residues, and the ionic conductivity of the inorganic salt catalyst is at least one of the inorganic salts in the inorganic salt catalyst is in the range of 300c to 5⑻. The conductivity in the range of C and the control of the contact conditions make the crude oil product have a residue content of at most 30% of the crude feed residue content, which is expressed in grams of the residue of the crude oil product. , Where the content of residue is as determined by ASTM method D5 3 07. The 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

The complete product of oil products, 1 φ Xidian,

"Zhonghai Hai crude oil product is a liquid mixture at 25 0C and 0 · 101 M. The crude oil feed has a residual fish content of at least 02 grams of residual fish per gram of crude oil feed. The inorganic salt catalyst contains a metal test salt, where At least one of the metal test salts is considered to be a metal carbonate test, and the alkali metal is less than 1 1 in atomic order, and the alkali metal sequence of at least u to the alkali metal having an atomic order greater than II is at least- The kind of atomic ratio is in the range of 0j to 10: and the contact conditions are controlled. Your crude oil product has a residue of at most 30% of the residue content of the crude oil feed. The content is as determined by astm 18 200530389 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, wherein the crude oil The feed has a residue content of at least 0.2 grams of residue per gram of crude oil feed. The inorganic salt catalyst comprises an alkali metal salt, wherein at least one of the alkali metal salts is an alkali metal hydroxide, and the alkali metal has at least Atomic order of 11 'and the original At least one atomic ratio of an alkali metal of at least 11 to a test metal having an atomic number greater than η is in the range of 0.1 to 10; at least a part of the complete product is made into a vapor; at 25. (: and 0.101 Mpa, cold reduced to / Part of the vapor; and forming the crude oil product, wherein the crude oil product has a residue content of at most 30% of the residue content of the crude oil feed. Ben Maoming also provides a method of manufacturing a crude oil product, which includes ... The feed is contacted with a hydrogen source in the presence of an inorganic salt catalyst to produce a complete product: In the middle ° Hai crude oil feed, there are at least 0.2 grams of residues per gram of crude oil feed in Wenslag 3, the rhenium inorganic salt catalyst contains alkali A metal salt, wherein at least one of the alkali metal salts is an alkali metal hydride, and the alkali metal has at least π: an alkali metal having an atomic order of at least 11 and at least one atom of the base f having an atomic order greater than 11 The ratio is in the range of ο · 1 to; the complete product of at least-'knives is made into a vapor, · 纟 25 ... and at least a part of the radon gas% a + ... holes condensed with 0 · 〇 and the crude product is formed Of which crude oil production is at most The content of crude oil feed residue is 30. The present invention also provides a method for producing a raw material of less than 3 miles, which includes: making Beijing oil feed and hydrogen source in the helmet oil production private aa 隹 ... 钺 catalyst exists Contact to produce a complete product containing the original, where the r 豕 甴 / 甴 product is a liquid mixture at 25 ° C and 0.101 Mpa 19 200530389, the crude oil feed has τ I ^ 0.2 g residue per gram of crude oil feed Residue content, the inorganic salt catalyst comprises one or more ~ γ hard alkali metal salts, one or more alkaline earth metal salts, or a mixture thereof, wherein the alkali metal is an alkali metal carbonate, wherein the alkali metal has an atom of at least u And control the contact conditions so that the crude oil product has a residue content of at most 30% of the residue content of the crude oil feed, wherein the residue content is as determined by 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 comprising a crude oil product, wherein the crude oil product is at 25 ° C. (: It is a liquid mixture with 0.11 Mpa. 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 one or more alkali metal hydroxides, one or A plurality of alkaline earth metal salts or mixtures thereof, wherein the alkali gold II has an atomic order of at least 1 1; and controlling the contact conditions so that the crude oil product has a residue content of at most 30% of the residue content of the crude oil feed, wherein the content of the slag is As measured by ASTM method D5307. This month also provides a method for manufacturing crude oil products, which includes: contacting the source feed with a hydrogen source in the presence of an inorganic salt catalyst to make a human

Complete bucket for oil products S

Product 'wherein the crude product is a liquid at 25 ° C and 0.11 M, and the crude feed has at least 0.02 g of residues per gram of crude feed. Here, the Rong inorganic salt catalyst includes one or more alkali metal hydrogens having an atomic order of = or more alkaline earth metal salts or mixtures thereof, and wherein the alkali metal objects have an atomic order of / 1; and controlling the contact conditions such that crude oil produces, Till the evening is a residue content of 30% of the crude oil feed residue content, 20 200530389 is expressed in grams of residue per gram of crude oil product, and the residual content is as determined by ASTM method D5 3 07. The invention also provides a method for producing hydrogen, which includes: contacting a crude oil feed with one or more hydrocarbons in the presence of an inorganic salt, and water, the hydrocarbons having a carbon in the range of 1 to 6 The ^ ^, edge crude oil feed has a residue content of 0.2 g of residue per gram of crude oil feed, .CA and the 5 xan inorganic salt catalyst exhibits a temperature range between 50 and 500, ^ The turning point of the discharged gas between the discharged breasts, such as the product instantaneous analysis (TAp) ^, then the one; and the generation of hydrogen.

The present invention also provides a method for manufacturing a crude oil product, which comprises: contacting a crude oil feedstock with an inorganic salt catalyst, and contacting Feizi to produce a gas stream containing hydrogen, The first ^ ^ crude oil feed in beans has at least 0.2 grams of residual, stubborn, mixed glutinous glutinous cyanide, white glutamate, and white odor, 3 ounces per gram of the original raw material / from the feed, such as using the astm method 053. 7 The tester 'and the inorganic salt catalyst exhibited at 50 ° C and the other.c

The temperature of the exhaust gas in the temperature range 屮 B k ^ the exhaust gas "turning point, as measured by the product transient analysis (TAP); the first-Shidi crude oil feed and the second catalyst at least

A part of the generated gas stream is in contact to produce a π-king product containing a crude oil product, where the crude oil product is a liquid limb mixture at > 1 JL and 〇1 〇1 MPa; Compared with one or more properties of the second ... J crude oil product, the properties are changed by at least 10%.

The present invention also provides a method for producing ancient, + 4 A ^, 4, lice / melon, which includes: ... contacting crude oil with an inorganic salt catalyst at base steam Qi Qi Qi ... Wherein the crude oil is fed and at least 0.2 g of crude oil is fed,

Fanci! Residue content, as measured in accordance with ASTM 21 200530389 method 370; and generating a gas stream comprising hydrogen, slave oxide, and -carbon oxide 'and wherein the molar ratio of carbon dioxide to dioxide is at least 0.3. ~ The present invention also provides a method for manufacturing a crude oil product, comprising: adjusting a HH catalyst to 'contact a crude oil feed with a chlorine source under the adjusted inorganic salt catalyst M' to produce a complete product comprising a crude oil product, wherein The original product is a liquid mixture at 25 C and 0.001 Mpa, and the crude oil feed has a residual content of gram 0.20 grams of residue per gram of crude oil; and controlled and contacting conditions make the crude oil product have Up to 30% of the residual content of the crude oil feed residue, which is expressed in grams of residual product per gram of crude oil product, where the residue content is determined by the method of 8% by weight 1) 5307 By. Ben Maoming also provides a crude oil composition '纟 that contains a boiling range distributed at 30i and 53rc0. F) smoke between the hydrocarbons including hetero-chain and normal-chain hydrocarbons, wherein the weight ratio of hetero-bonds to normal-chain alkanes is at most h4, as determined by ASTM method D673. The present invention also provides a crude oil composition, each gram of which contains: 0.001 grams of hydrocarbons having a boiling range distribution of at most 204 (400 F) at 0.101 MPa, at least 0.001 grams in 0.001. The boiling range at i is 204. (: And hydrocarbons between 3,0 ..., at least 0.001 g of hydrocarbons with a boiling range distributed between 3 000c and 4 000 MPa at 0 MPa, and at least 0 ·· 001 grams of hydrocarbons with a boiling range distributed between 4000c and 8 ° C (1,000 ° F) at 0.1101 MPa, and where the boiling range is distributed up to 204 ° C The hydrocarbons include isoparaffin and normal paraffin, wherein the weight ratio of isoparaffin to normal paraffin is at most! · 4, as measured by ASTM method D6730. 22 200530389 The present invention also provides a crude oil composition The composition of gram contains at least 0., gram of light oil, which has at least 70% female avalanche. The light oil contains at most gram of dilute hydrocarbon per gram of light oil, as measured by astm? D6730 kg. ; At least °, grams of kerosene, the kerosene system has at least 0.2 grams of aromatic compounds per gram of kerosene 2, such as astmd5i8 = tester 'and the kerosene has a freezing point at a temperature of at most _30 ℃, aSTmD2386; and up to 0.05 g of residue, as measured by ASTM method D5 3 07.

The present invention also provides a crude oil composition, which per gram of composition contains: at most 0.15 grams of non-condensable hydrocarbon gas at 25 and (Moi Mpa), non-condensable flue gas system contains at most G.3 per gram of non-condensable hydrocarbon gas Grams of hydrocarbons with a carbon number from 43 ^ to C3); at least 0.001 grams of light oil, which has a Xinxin value of at least Sichuan; at least 0._ grams of kerosene, which has a freezing point at a temperature of at most As measured by ASTM & D2386, and the kerosene system contains at least 0,2 grams of aromatic compounds per gram of kerosene, as measured by the method 5 1 86, and up to 0.05 grams of residue, such as by the aStm method D5307 Measured by. The present invention also provides a crude oil composition containing per gram of composition: at most 0.05 g of residue, as measured by ASTM method D5307; at least 0.001 g of boiling range distribution at 0.11 MPa Hydrocarbons of up to 204 ° C (400 ° F); at least 0.001 grams of Fotan range at 0.001 at 0.11 MPa. 〇: and 300. 〇: hydrocarbons in between; at least 0.001 g of boiling range distributed at 300 under 001 1 ^ 1 ^. (: Hydrocarbons between and 400 oc; at least 0.001 g of hydrocarbons with a boiling range distributed between 4000 and 538 oc (1,000,200,2005,30,389,0F) at 0.101 MPa; and Among them, the hydrocarbons in the boiling range distribution between 20% and 20% (:) include olefins with terminal double bonds and women's tobacco with intramolecular double bonds: where olefins with terminal double bonds have intramolecular double bonds The mol ratio of olefins is at least 0.4, as measured by ASTM method D673. The present invention also provides a crude oil composition containing per gram of composition: up to 0.05 g of residue, such as by ASTM method D53 〇7 measured; and at least 0.001 grams of boiling range distributed between 20.0 and 538 〇c (1, delete. Hydrocarbon mixture 'as measured by AST ^ D53G7, and the hydrocarbon mixture per gram The hydrocarbon mixture contains: at least 0,001 grams of paraffinic hydrocarbons, as measured by the ASTM method plus 730,000; at least 0.001 grams of thin smoke, as measured by the ASTM method D673G, and the dilute hydrocarbons are Kerene smoke contains at least o.ool grams of terminal dilute hydrocarbons, as determined by ASTM ^ D673〇; at least, please 1 gram of light oil ' At least 1 gram of kerosene is required. The kerosene is 0.2 to 0.2 grams of aromatic compounds per gram, as measured by MTM method D5186. At least 0.001 grams of diesel, which contains up to > 0.3 g of aromatic compound 'as determined by IP method 368/90; and at least 1 g of vacuum gas oil The VG0 is per gram of paste: there is at least 0.3 g of aromatic compound, as deleted by the ιρ method .Measured by.

The present invention also provides a Ludian MS crude oil composition, which per gram of composition contains: at most 0. 05 Bai Baishun, Apricot, 丄 χ 彳-as measured by ASTM method D5307; to. The distribution of less_grams in the 1M_㈣ range is at most. At 400 ° F) hydrocarbons; at least 〇〇〇〇-c ^ 3〇ooc. PbU ^ ° · 101 spoon, at least 0.001 grams at 0101 MPa 24 200530389 boiling range distribution at 300 ° C and Hydrocarbons between 400; and at least two 0.001 grams of hydrocarbons with a boiling range distributed between 400 ° c and 538 (1,000 ° F) at 0.101 MPa, as determined by ASTM method D2887; boiling range distribution For up to 204. (: The hydrocarbons contain at least 0.01 g of dilute hydrocarbons per gram of boiling range of 204 C in the boiling range, as measured by astm method D6730; and at least 0.001 g of paraffin, the Paraffinic hydrocarbons include isoparaffins and normal paraffins, wherein the weight ratio of isoparaffins to normal paraffins is at most 1.4, as measured by ASTM method D6730. The present invention also provides a crude oil composition, each of which contains · _ Residues of up to 0.05 g, as measured by ASTM method D53〇7; and y 0.001 g of Fouteng range distribution of up to 204 0C (4000F) at 0.001 MPa Hydrocarbons; at least 0.001 g of hydrocarbons with a boiling range distributed between 204.0 and 300 γ at 0101 MPa; at least 0.001 g of boiling regions with a distribution range of 300 at 0.011 MPa Hydrocarbons between 40,000 and 400c; and at least 0.001 g of hydrocarbons with a boiling range distributed at 0.101 MPa. 匸 and 53.8 ° C (1,000.00.?), As determined by ASTM method d2887; and the hydrocarbons in which the boiling range is distributed between · 100c and 204 include compounds having a carbon number of 4 (C4) The q compound contains at least 0.001 g of butadiene per gram of C4 compound. The present invention also provides a crude oil composition containing per gram of composition: at most 0.05 g of residue; at least 0.001 Grams of hydrocarbons with a boiling range of 0,001 MpaT and a distribution range of up to 204 ° C (400 ° F), at least 0.001g, and a boiling range of 40,000 ° C and 300 ° F at 00 MPa Between at least 0.001 g of hydrocarbons with a boiling range of 0.30 MPa at 0.11 MPa and hydrocarbons between 0.000 and 4,000c 25 200530389 and at least please! 克 在 ㈣i Hydrocarbons with boiling ranges in the range of 400 ° C and 538 ° C under Mpa; and-or more catalysts-greater than 0 g but less than 0.01 g-where the catalyst contains at least one or more alkali metals. In some specific examples, the present invention also provides crude oil feeds in combination with one or more of the methods or compositions according to the present invention, which have not been processed, resid, and / or defensed in refining obstacles; ⑻ contains ingredients with a carbon number of 4 or more, and the crude oil feed contains at least 0.5 grams of such ingredients per gram of crude feed; (c) Hydrocarbons, some of which have a boiling range distribution below 〇i〇i MpaT of less than 100 ℃, a distribution of 'Futeng dry-circle distribution between /, 200 ℃ under 〇IO1 MPa, and oloi Mpa Distribution between 2000c humans: 300C :, Forten range distribution, boiling range distribution between 0.10M and 3.0 ° C M 4.0 ° C, and between 0.10 ° C The boiling range distribution under Μρ & between 400 and 7000cC; (10 per gram of crude oil feed contains… to 1.00 gram of hydrocarbons with a boiling range distribution below 0.101 MPa at 0.101 MPa , At least 0.001 grams of boiling range distribution between 1000c and 200 at 0101 MPa. (: Hydrocarbons between, at least 0.001 g boiling range at 200 MPa distributed at 200. (: and 300. (: hydrocarbons between, at least 0.00 00 g at _101 Hydrocarbons with a boiling range between 300 and 4000c at MPa, and at least 0.001 g of hydrocarbons with a boiling range between 400C and 700 ° C at 001 MPa; (E) having a tan; (f) containing 0.2-0.99 g, 0.3-0.8 g, or 0.4-0.7 g of residue per gram of crude oil feed; (g) containing iron, hunger, iron, or a mixture thereof; (H) contains sulfur; and / or 氮 nitrogen-containing hydrocarbons. In some specific examples, the present invention also provides a hydrogen source in combination with the party 26 200530389 = ::: Is gaseous; ⑻ includes a mixture of Γ: two Γ buried species, including…, Yixuan, or π, (e) contains water; and / or ⑺ mixtures thereof. = In some specific examples, the present invention also provides a method according to the law or A method of the composition of-or a combination of: organic salt catalyst, and ^ 田 # ”dagger as short, Hai Wu, /, 5 Zhou Lang The inorganic catalyst includes: 0) 11 11 ga gg # Λ hot to at least 300ΑΑ — 彳 liver… stick salt The temperature of the medium is reduced, and / or (b) the inorganic salt catalyst is heated to a temperature of about 50 ° C and the inorganic salt catalyst is cooled to a temperature of at most 500 ° C. Some specific properties, the present invention also provides The combination with one or more of the present method or composition includes the introduction of crude oil ^ "Control of contact conditions: ⑷ so that during the contact period = crude oil feed is at most 0.2 grams, at most. 15 grams , At most ;, 25 g at 25 ° C and 0.2-㈣ non-condensable hydrocarbon-shaped didicarbonate 1 balance measured; (b) the contact temperature M at ㈣: Wai: or between 26- ⑷ pressure is within ^ ^ ^ ^ ^ so that the ratio of gaseous chlorine source to crude oil feed is within the range of 1-16100 per cubic meter of raw / feed or quasi-cubic meters of hydrogen source) pieces ,, = 1) In order to inhibit the formation of coke in the complete product or containing ^ during the contact; ⑻ make the crude product is more white per gram of crude product ;: · 05 grams, at most 0.03 grams, at most _ grams or at most Gram] ..., tired, (h) makes at least _duba n > τ. ^ The knife's inorganic salt catalyst in contact with the material or liquid in this condition; ⑴ makes crude oil The product has a TAN of at most 90% of the crude oil; ⑴ makes the crude oil product have an ash / WFe content of at most 90%, at most 50% or at most _ indeed the N · content, of the crude oil. The crude oil product has a sulfur content of up to 90%, up to 60%, or up to 30% of the sulfur content of the crude oil feed; ⑴ making the crude oil product have up to 90%, up to 70% of the nitrogen content of the crude oil feed. , At most or at most the nitrogen content; (m) the crude oil product has a residual content of at most 30% of the crude oil feed, at most ⑽, or at most states; ⑷ makes ammonia and crude oil products co-produce ; (. ) Causing the crude product to contain methyl formaldehyde, and the method further comprising: recovering methanol from the crude product; combining the recovered methanol with an additional crude feed to form an additional crude feed / methanol mixture; and heating the The additional crude feed / methanol mixture reduces the TAN of the additional crude feed below "; (P) causes the-or multiple properties of the crude product to be changed compared to the individual or multiple properties of the crude feed g. The amount range is 16 grams per gram; the catalyst in the contact zone is fed to the crude catalyst with 60 grams of crude oil; and / or the hydrogen source is added to the crude oil feed before or during the contact. in. In some specific examples, the present invention also provides contact conditions with a combination of one or more of the methods or compositions according to the present invention, which include: ⑷ feeding the inorganic salt catalyst to crude oil at a temperature of _: Mixing, wherein the inorganic-Shu medium is insoluble in the crude oil feed; (b) agitating the catalyst in the crude oil feed; and / or mixing the crude oil feed with the inorganic salt catalyst in water and / Or = contact in the presence of vapor to make a complete product comprising a crude product that is a liquid mixture under STP. In some specific examples, the present invention also provides a method in combination with one or more of the party / or composition according to the present invention, which comprises contacting crude oil with an inorganic salt catalyst and further includes: (A) Before or during the contact, steam is known to be supplied to the contact area, (b) Before the crude oil feed is contacted with the inorganic salt catalyst and hydrogen source, an emulsion of the crude oil feed and water is formed. (C) spraying the crude feed into the contact zone; and / or (d) contacting the steam with the inorganic salt catalyst to at least partially remove coke from the surface of the inorganic salt catalyst. In certain embodiments, the present invention also provides a method in combination with one or more of the methods or compositions according to the present invention, comprising contacting a crude oil feed with an inorganic salt catalyst to make a complete product, wherein At least a portion of the complete product is made with vapor, and the method further includes condensing at least a portion of the vapor at 25 φ c and 0.11 Mpa to form the crude product. The contact conditions are controlled such that: (a) The crude product further comprises a component having a selected boiling range distribution; and / or (b) the crude product comprises a component having a selected API specific gravity. In some specific examples, the invention also provides a method in combination with one or more of the methods or compositions according to the invention, comprising 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 present invention also provides a K3FeiGSi4 catalyst or a transition metal sulfide catalyst in combination with one or more of the methods or compositions according to the present invention 'which: (a) per gram of the K3Fei ( ) Si4 catalyst or transition metal sulfide catalyst contains a total of at least 0.4 grams, at least Θ.6 grams, or at least 0.8 grams of ^ transition metal sulfides; (b) K3Fe1GS14 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 alkali metals, one or more alkali metal or evening compounds or a mixture thereof; (d) further Comprising one or more alkaline earth 29 200530389 metals, one or more compounds of alkaline earth metals or one or more compounds thereof; further comprising one or more metal detection metals, or one or more compounds or mixtures of alkali metals thereof, wherein The atomic ratio of transition metal to sulfur in a catalyst or transition metal sulfide catalyst is in the range of 0.5 to 25 and the range of 0 to 1 and the atomic ratio of alkali metal to transition metal is between

(F) further comprising one or more alkaline earth metals, one or more compounds of alkaline earth metals or a mixture thereof, the atomic ratio of transition metal to sulfur in the K3Fe 丄 catalyst or transition metal sulfide catalyst is In the range of 0.5-5_2, and the atomic ratio of the alkaline earth metal to the transition metal is in the range of 0 to ^ '(g) further includes zinc; (h) further includes KFe2S3; ⑴ further includes KFeS2; and / Or rhenium is non-acidic. In some specific embodiments, the present invention also provides a combination with one or more of the methods or compositions according to the present invention, in which the K3Fei0Si4 catalyst is formed on the spot. In certain embodiments, the present invention also provides one or more transition metal sulfides in combination with one or more of the methods or compositions according to the present invention, which or wherein: (a) comprises-or more selected from the periodic table Number 6] 〇Interval's transition _ metal, one or more compounds selected from transition metals No. 6_10, or a mixture thereof; (b) containing one or more iron sulfides; containing FeS; (d) containing FeS 〗 〖; (E) a mixture containing iron sulfide, wherein the iron sulfide is represented by a chemical formula, wherein 6 is in the range of 0 or more to 〇17; (f) further comprises K3Fei0S14 after contact with the crude oil feed; (g) at least one of the transition metals of the one or more transition metal sulfides is iron; and / or (h) is deposited on a support, and the transition metal 30 200530389 sulfide catalyst is per 100 grams of catalyst Contains up to 0.25 grams of total carrier. In certain embodiments, the present invention also provides a method for forming a transition metal sulfide catalyst composition in combination with one or more of the methods or compositions according to the present invention, the method comprising combining a transition metal oxide with a metal Mixing salts to form a transition 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 smokes to Generates transition metal sulfide catalysts: ⑷ the metal salt contains an alkali metal carbonate; ㈨ it further

Including dispersing the intermediate in-or more liquid hydrocarbons, ㈣ causing potfish sulfur reaction; ⑷ where-or more of the hydrocarbons have a boiling point of at least Η) 〇γ, ⑷ where the hydrocarbons-or more is VGQ: methylbenzyl or its mixture; ⑷ mixing transition metal oxides and metal salts includes: mixing transition = emulsion with metal deionized water to form a wet paste; Γ wet paste in the range from 15G-25G ° C for drying 1 and calcining the dried paste at a temperature in the range ::

Including heating the intermediate to 240-350 ° in the presence of at least one of the hydrocarbons, rubella, heart, and / or (g) it further includes the catalyst, and The product is contacted with a crude oil feed containing a source of sulfur and hydrogen. In some specific examples, the present invention also provides inorganic salt catalysts in combination with-or more of the party or composition according to the present invention. The pot contains:-a metal test carbonate, one or more metal test carbonates Salt or its mixture (:-or metal-oxide chloride, one or more metallurgical compounds or mixtures thereof; plutonium- or more metal-pigment gasifications ... more than earth metal hydrides or mixtures thereof; plutonium- or One or more of various metal test 31 200530389 Sulfides, one or more sulfides of one or more alkaline earth metals or mixtures thereof; (e) — one or more amidines of one or more alkali metals, one or more alkaline earth metals One or more amidines or mixtures thereof; (f) one or more metals selected from columns 6-10 of the periodic table, one or more compounds selected from columns 6-10 of the periodic table or a mixture thereof; ( g) one 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, osmium, planer or mixtures thereof; osmium calcium and / or magnesium;混合物 a mixture of sodium and potassium salts, and the potassium Comprises potassium carbonate, potassium hydroxide, potassium hydride or a mixture thereof, and the sodium salt comprises sodium carbonate, sodium hydroxide, sodium hydride or a mixture thereof; and / or (k) a mixture thereof. In certain embodiments, The present invention also provides an inorganic salt catalyst containing an alkali metal in combination with one or more of the formula = or the composition according to the present invention, wherein: ⑷ metal test atom having an atomic order of at least U to metal test atom having an atomic order greater than u The ratio is in the range of 0 "to 4; (b) at least two: sodium and potassium in the alkali metal, and the atomic ratio of sodium to potassium is in the range of 0.1 to 4; At least three of them are sodium, potassium, and thorium, and the atomic ratios of sodium to potassium, sodium to thorium, and to I are each in the range of ο · 1 to 5. The metal towels are sodium, potassium, and planer. And the ratios of sodium to potassium, sodium to cesium, and potassium to planers are each in the range of η 1 r potassium, ▲, .1 to 5; (e) at least three of the alkali metals are bismuth, and The atomic ratios of potassium versus planer, potassium versus scandium, and planer versus scandium are each in the range of • to 5. In a specific embodiment of the method, the present invention also provides a medium according to the present invention, and : / The combination of inorganic salts containing a carrier material (a) The carrier material contains hafnium oxide, calcium oxide, magnesium oxide, oxygen 32 200530389 Huaqin, hydrotalcite, oxide oxide, germanium oxide, zinc, cadmium oxide Nicotiana tabaci L., an emulsified compound; and ^ compounds; and 7 or ⑻ mixed with the carrier material 有.-Or more selected from the sixth table of the periodic table. "One or more compounds of metals; gold =: acid salts, one or more metal oxides,-or more bismuth earth metal carbonates, one or more alkaline earth metal hydroxides, one戍 Various kinds of 蛉 + person ^ 4 7 miles of alkaline earth metal hydride and / or mixtures thereof_ In some specific examples, the present invention also provides a sigma Godot information with the method or composition according to the present invention A method of combination of the company and the company, which includes contacting the crude oil feed with an inorganic salt: g-, catalyst contact, where: ⑷The catalyst activity of the inorganic salt catalyst is temporarily measured in the presence of sulfur. θ, 疋 No, cross; and / or (b) Add the inorganic salt catalyst to the crude oil feed . In some specific examples, the present invention also provides an inorganic salt catalyst combined with one or more of the method according to the present invention, and exhibits: 展现 Exhaust gas in the temperature range The turning point, and the exhaust gas contains water bars * 1 and / or carbon dioxide; ⑻ at 2000-500c, 2500 • ㈣. Thermal transitions in the temperature range between C or 3 0 1 400 c, as determined by differential scanning calorimetry at a heating rate of 10 ° C. per minute; (c) between 200-500 0 C or 25 0- DSC temperature in the range between 45 ° C; (d) at least 100. . At a temperature of j, an X-ray diffraction pattern that is wider than the x-ray diffraction pattern of the inorganic salt catalyst below 1000, and / or ⑷ after adjustment, 3 ⑽. The ionic conductivity of c 4 is smaller than the ionic conductivity of the inorganic salt catalyst before adjustment. In some specific examples, the present invention also provides an inflection point measurement / representation in the inorganic temperature range in combination with one or more of the methods or compositions according to the method 33 200530389 of the present invention. It also controls the wood so that the contact temperature is: ⑷] or more, and the inorganic salt of the bean contacts /, T 1 疋 is at 3 ° C, 20 at the TAP temperature. . Or 10. . ; ㈨ Temperature. ^ ^ 上 'and / or at least the TAP method or example of the inorganic media, the present invention also provides and according to the present invention ...

White, — or a combination of inorganic salt catalysts, or of which: (a to > TAP γ_ t / night body or semi-liquid in the inorganic salt catalyst, and the inorganic salt catalyst at least in the τΑΡ ^ translated π ^ Μ t insolubility is insoluble in the crude oil, and the two-hour TAP temperature is the minimum temperature of the inorganic salt catalyst display point, ranging from 50 to 50: body: folded And solid phase mixture; and the following is a liquid, and / or (C) at least one ^ 500 DSC $ ^ 〇 of the δH-a inorganic salt has

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. When tested in the form of particles that can pass through a micrometer filter, when When heated to at least 'C', it will self-deform under gravity and / or at least 0.007 MPa, so that the inorganic salt catalyst changes from the first form to the second form, and the second form is in Cooling the inorganic salt catalyst to 2000c cannot return to the first form. In some specific examples, the present invention also provides inorganic salt catalysts in combination with-or more of the method or composition according to the present invention, each of which has a maximum of 0.01 g per gram of inorganic salt catalyst. Lithium or lithium compounds, based on the weight of lithium 34 200530389, (b) up to 0 001 grams of free radicals, which is calculated based on the weight of dentin; and / or ⑷ up to 0.001 grams of glass Like oxide compound. In certain embodiments, the present invention also provides a complete product in combination with one or more of the methods or compositions according to the present invention, which contains at least 0.8 grams of crude oil product per gram of complete product. In certain specific aspects, the invention also provides crude oil products in combination with one or more of the methods or compositions according to the invention, which: at most 0.003 grams, at most 0.02 grams, at most gram crude oil products. 〇ι 克 at most 0.05 grams, the most? 0.001 g, 0.00000 g, 0.00 g, or 0.001 g-0.0 g of residue; (b) each gram of crude oil product contains from 0 g to 0.05 g, 0.01 g. 03 g or 10,000 g of coke; ⑷ has a dilute hydrocarbon content of at least 10% greater than the olefin content of the crude oil feed; ⑷ per gram of dead product contains greater than 0 g but less than 001 g of total inorganic salt contact Medium, as determined by mass balance; (e) each gram of crude oil product contains at least 0.01 g, 0.00-0 g (Π-0.99 g, 0.04-0.9 g, 〇6_〇8 g of v (k >; ⑴ contains VGO and the ⑽ system contains at least G3 grams of aromatic compounds per gram; ω contains 0 g or (mm g of 镏 effluent; ㈦ up to 14 atomic H / C; ⑴ has the crude oil feed H / c of 9 (M 10% atomic brain pupae having a monocyclic cycloaromatic compound content of at least 10% greater than the monocyclic cycloaromatic compound content of the crude oil feed; (k) containing xylenes, Ethylbenzene or a monocyclic aromatic compound of ethylbenzene compounds; ⑴ per gram of crude oil product contains 0.0! G of benzene, 0.05-0.51 g of toluene, and 3.09 g of m-dimethylene Ben, 〇 · 5-0.15 grams of o-dimethylbenzyl and 0_2_0.6 grams of para-xylene; (m) diesel oil containing at least 0.1 g or CUHW grams; (η) diesel oil, 35 200530389, and the diesel oil per coupon Disease, the mother of the mother sees that the wood oil contains at least 0.3 grams of aromatic compounds; (there is at least 〇〇〇〇ΐ 身, you π ,,,,, see more than 0 to 0.7 grams or 0.001-0.5 grams Kerosene; (P) "some / by" and the kerosene system contains at least 0_2 grams or at least 0.5 grams of aromatic compounds per gram of kerosene, and / or at most -30 V, at most wo γ or at most _5G ° Ca degree freezing point; ⑷ contains at least 0 side grams or at least 0.5 grams of light oil; ⑴ contains light oil, and the light oil system contains at most 0.001 ^ to Xi 05 grams per gram of light oil or Up to 0.002 grams of benzene, at least 70, at least 80, or up to ν 90 octane and / or isoparaffin and normal paraffin, wherein the weight ratio of isoparaffin to normal paraffin in the light oil is at most 1.4; and / Or ⑷ has a volume of at least 10% greater than the volume of the crude oil feed. In certain embodiments, the present invention also provides-or more groups, of the method or composition according to the present invention A combined method, which includes: connecting the crude oil feed with the catalyst, and forming a complete product of the crude oil product. The method includes: (a) the same or different crude oil product from one At the ', _' mouth of the crude oil feed to form a blend suitable for transportation; (b) combining the crude oil product with a crude oil of the same f which is different from the crude feed to form a suitable processing facility; (C) fractionating the crude oil product; (d) fractionating the crude oil product into / or: seed filling knives, and manufacturing transportation fuel from at least one of the fractions; and /) Tian catalyst is a transition metal sulfide catalyst When the catalyst is used, the transition metal catalyst is processed to recover the metal from the transition metal sulfide catalyst. In some specific examples, the present invention also provides a crude oil product combined with one or more of the formulae or 20% of the product according to the present invention, which has 3 per gram of crude oil. (A) at least 0.001 Grams of VG0, and the VG0 is at least 0.3 grams of aromatic compounds per gram of VG0a; ⑻ please at least gram of diesel, 36 200530389 == at least per gram of diesel. .3 grams of aromatic compound; ⑷ to. Gram of light oil, and the light oil: each gram of light oil contains up to 0.05 g = two t Μ of the calorific value, and / or heterogeneous and positive chain smoke, which ~ The weight ratio of the chain to the positive chain hospital cigarette is a mixture of up to 204 ° C (400 ° F) with a total distribution of up to ^ .001 grams of Foten = and the mixture is The gram mixture contains at most 0.15 grams of thin smoke; (e) the weight ratio of atomic hydrogen to atomic carbon in the composition is ≤ 3 to 0.5 gram of aromatic compound and / or has at most _3. % Freezing point of temperature; (g) atomic hydrogen from U9.M3 grams per gram of composition; ^ condensed hydrocarbon gas and light oil 'when combined, its combined non-condensable hydrocarbon gas and light oil contains at most 0.15 grams of Alkenes; non-condensable hydrocarbon gas and light oil, when combined, they contain isofluorinated hydrocarbons and normal-chain hydrocarbons, where the weight ratio of iso-paraffins to normal paraffins in the combined non-condensable light-gas is 14 at most ; ⑴ carbon number up to 3 hydrocarbons, including: carbon number 2 (C2) and 3 (C3): hydrocarbons and chain burning smoke, and the combined A and I olefins to the combined dagger and C3 chain burning hydrocarbons Weight ratio to 0.3; carbon number 2 (C2) olefins and paraffins, with a weight ratio of 2 olefins to c ′ hydrocarbons up to 0.2; and / or carbon number 3 (c3) olefins and chain hydrocarbons, which The weight ratio of the tobacco C3 diene to & chain-burning tobacco is at most 0.3; (k) has a succinic content of at least ο, g; ⑴ has 15.5. (: Aρι specific gravity in the range of 15 to 30; (m) total Nl / V / Fe per 2 composition up to 彡 00 · 1; paraffin content of hydrocarbons with a distribution range of up to 204 γ It is in the range of 〇7_〇 · 98 grams. ⑷ Boiling range distribution of hydrocarbons up to 204 ^, per gram stagnation range 37 200530389 smoke distribution of up to 204 〇C containing 胄 〇 · 〇〇1 · 〇5 grams of dilute hydrocarbons, including hydrocarbons with a boiling range distribution of up to 204 γ, and the olefins contain at least 0._ grams of terminal dilute hydrocarbons per gram of hydrocarbons; ⑷ contains olefins; Smoke up to 204 ° C, and the olefin has at least a molar ratio of terminal olefin to intramolecular smoke; and / or hydrocarbons distributed within a boiling range of between 20% and 204 ° C per gram from 〇〇〇ι_〇5 hydrocarbons. In some specific examples, the present invention also provides a crude oil produced in combination with one or more of the formula: or composition, which contains one or more bases At least one of the metal catalysts, Gan Zhankao, in which: (a) the alkali metal: at least one of which is potassium, a substance, or a compound thereof; and / or the catalyst At least one of them further comprises a transition metal, a transition metal sulfide, and / or a bartonite. In a further specific example, features from the present invention may be combined with features from other specific examples of the present invention. Examples + special features:-The characteristics of specific examples can be combined with the characteristics from other tests-crude oil products are obtained through any of the specific specific and further specific examples described in this article and in the system Additional features are added to the examples in further specific examples.

Detailed description of the invention: Here I will explain some examples of the present invention in more detail. The terms used in this article 38 200530389 are defined as follows. — Alkali metal ”means—or more than one metal selected from the first group of the periodic table, —or more than one metal selected from the first group of the periodic table—or more compounds or mixtures thereof. A variety of metals selected from column 2 of the periodic table, or compounds or mixtures thereof from column 2 of the periodic table. AMU means atomic mass unit. "ASTM" means American Standard Tests and Materials (American (Standard · Testing and Materials) 〇Asphaltene refers to asphaltenes that are insoluble in pentane. Q Asphaltene content is as measured by ASTM method D2007. Crude oil feed, crude oil products, light oil, kerosene, diesel, and VGO The atomic hydrogen percentage and atomic carbon percentage are as measured by ASTM method D529i. API specific gravity 'refers to the specific gravity of Aρm at 15.0 ° C. The specific gravity of API is as determined by ASTM method D6822. Lu “Asphalt” system Refers to a type of crude oil produced and / or retorted from a hydrocarbon product. 'Unless otherwise mentioned, the boiling range distribution of the crude feed and / or complete product is as determined by ASTM method D5307. Hydrocarbon composition, E.g The content of paraffins, isoparaffins, alkenes, naphthenes, and aromatic compounds in light oil is determined by ASTM method D6730. The content of aromatic compound Z in diesel and VGO is determined by the ip method 368 Measured by / 90—a 'Fangzu 39 200530389 The content of chemical compounds in coal / yield is determined by the method D5 丨%. Bronze 4 ^ f ^ ih / inch_dimensional (Br0nsted_L〇wry) Acid, refers to the molecular body that has the ability to give protons to the f 'two-molecule body. So, "Bu = sterolite," refers to the knife body that can accept shellfish from another molecular body. Examples of Nyster's Rory base include hydroxide (0H ^, water (H2O), carboxylate (RC02-), halide (Br-, C1, F, 1), hydrogen sulfate (HS 〇r) and sulfate (s (V-). Stone inverse number "refers to the total number of carbon atoms in the molecule.

'' It is deducted that there are carbonaceous solids that do not vaporize under the conditions of the method ..., and the three miles are determined by mass balance. Coke weight is the total weight of solids minus the total weight of the input catalyst. "Content" refers to the weight of a component in a substrate (such as crude feed, complete product, or crude product, expressed as a weight fraction or weight percentage of the total weight of the substrate. "Wtppm," refers to per hundred expressed by weight). Parts in 10,000 parts. "Diesel" refers to hydrocarbons whose boiling range is distributed between 26 ° and 343Y (500-650 500) at 0.101 MPa. The diesel content is as determined by the μ term D2887. The `` liquid discharge '' refers to the cigarettes with a discharge range of G.101 MPa between 2400c and 343 ° C (400-650 叩). The remaining liquid content is as determined by ASTM method D2887. The effluent may include kerosene and diesel. "DSC" refers to differential scanning calorimetry. "Freezing point" and "freezing point" refer to the temperature at which crystalline particles form in the liquid. The freezing point is as measured by ASTM D2386. Measurer. 40 200530389 GC / MS refers to gas chromatography combined with mass spectrometry. "Hard" refers to Pearson in 〇 / 如 — 心 de〇 ;, 1963, 85, ρ · 3 5 33 The stated anion. The weight ratio of H / C based atomic hydrogen to atomic carbon. H / c based on ASTM method D5291 "Heteroatom" refers to the oxygen, nitrogen, and / or sulfur contained in the molecular structure of a hydrocarbon. Heteroatom content is determined by ASTM method E385. Determined by oxygen, D5762 vs. nitrogen and D4294 vs. sulfur. "Hydrogen source" means hydrogen and / or a compound that reacts in the presence of a crude oil feed and a catalyst to provide hydrogen to one or more compounds in the crude oil feed. And / or compound groups. Hydrogen sources may include, but are not limited to: hydrocarbons (such as q to G hydrocarbons, such as formazan, B :): end, C;): end, butan, pentam, light oil, Water or a mixture thereof. Mass balance is used to evaluate the net amount of hydrogen supplied to one or more compounds in a crude oil feed. "Inorganic salt" means a compound composed of a metal cation and an anion. IP refers to the Petroleum Institute (the Institute of Petrole), and now the Energy Institute of London (United Kingdom) 〇 Heterogeneous burning ”refers to branched saturated hydrocarbons. Kerosene refers to The boiling range is distributed at 204 at 10 MPa.

Hydrocarbons between 2 60 C (400-5 00 ° F). Kerosene content is as determined by asTM method D2887. 41 200530389 "Lewis acid" means a compound or substance that has the ability to accept one or more electrons from another compound. "Lewis base" means a compound that has the ability to donate one or more electrons to another compound Chemical compounds and / or substances. "Light hydrocarbons" refer to hydrocarbons with carbon numbers in the range of 1 to 6. "Liquid mixtures" refer to compounds containing one or more at standard temperature and pressure (25 ° c ' 〇1〇1 MPa, hereinafter referred to as "STp") is a composition of a compound that is liquid, or refers to a combination of- Composition. "Micro Carbon Residue" ("MCR") refers to the amount of carbon residue that remains after the substance has evaporated and pyrolyzed. The MCR content is determined by ASTM & D45. "Light oil '" refers to a hydrocarbon component having a boiling range of 38 ° C and 2400 ° C (1 ° F) at 0.101 MPa. The content of light oil is as measured by ASTM method D2887.

"Nl / WFe" means nickel, vanadium, iron, or a combination thereof.

The combined amount of Ni / V / Fe refers to Ni / V / Fe in a basic test. HASTM Fana 3 ^ refers to the standard cubic meter of gas per cubic meter of crude oil feed. "The nature of Lewis test and / or Brewster test. 4 Chaotic and refer to components and / or mixtures of ingredients at standard temperature and pressure (hereinafter referred to as" STP, "M Mpa)) . "U" refers to normal (straight-chain) saturated hydrocarbons. The “octane number” refers to the ratio of U-fuel in the U.K. compared to the standard reference fuel. 42 200530389 Number of different anti-knock properties + +. The calculated octane number of the light oil is as measured by ASTM method D 6 7 30. Alkenes are compounds with non-aromatic carbon-carbon double bonds. The types of olefins include, but are not limited to, V · 丨 Fake bucket '—, · 丨 member, trans, terminal, intramolecular, branched, and linear 0 k. "The table refers to the International Union of Pure and Applied Chemistry (IUPAC) Periodic table stipulated in November 2003. A multi-family compound refers to a compound containing two or more aromatic rings. Examples of evening aromatic compounds include, but are not limited to, indene, naphthalene, anthracene, phenanthrene, benzothiophene and dibenzophenone. "Residual" refers to a component with a boiling range above 538 ° C (1000 ° F) at 0 · 101 Mpa, as measured by ASTM method D5307. "Semi-liquid" means a material phase that has The liquid and solid phases of this substance. Examples of semi-liquid inorganic salt catalysts include pulp and / or phases with consistency such as toffee, pudding, or toothpaste. "SCFB" refers to the standard of crude oil feed per barrel Cubic feet of gas. Superbase "refers to a substance that can deprotonate hydrocarbons such as chain-burned hydrocarbons and olefins under reaction conditions. "TAN" means the total number of acids in grams of KOH ("mg") per gram ("g") of the sample. TAN is as measured by ASTM method D664. "TAP" means transient analysis of the product. "TMS" means transition metal sulfide.

"VGO" refers to a component whose boiling range is distributed between 343 ° C and 53.8 ° C (65 (MO)) at o.ioi MPa. The VGO content is determined by ASTM D 200530389 method D2887 In the context of this application, it is to be understood that if the value of h for the test and the product (± 所) is outside the limit of the test method, the & Test method to test this property. It should be understood that other standardized test methods that are considered to be equivalent to 芬 @ 芬 号 ”于 所 k and martial arts testing methods can be used.

Crude oil can be obtained from 3 products and / or Zengwa Pavilion, and then reconciled '. Crude oil is usually tritium, semi-solid and / or liquid. Crude oil may contain tritium oil. Stabilization may include, but is not limited to, removing non-condensable table, water, salt, or a combination thereof from the crude oil to form a stable crude oil. This stabilizing intermediary action can take place at or near the manufacturing and / or distillation site.

Stable crude oils have generally not been distilled and / or branched off at processing facilities to produce multiple components with a specific boiling range distribution (eg, light oil, distillate, VGO, and / or lubricating oil). Steaming halls include, but are not limited to, atmospheric distillation and / or vacuum distillation. The undistilled and / or unfractionated stable crude oil may contain components having a carbon number of 纟 4 or more in an amount of at least Q 5 grams of components per gram of crude oil. Examples of stable crude oil include whole crude oil, topped crude oil, desalted crude oil, desalted crude oil, or a combination thereof. "Topping, refers to a type of H that has been processed so that at least some of the components with a boiling point of less than 35% at 0.101 MPa have been removed. Typically, topping crude oil contains up to 彡 (M g, Ingredients with a content of at most G.G 5 g or at most g. Some stabilizers; properties by which stable crude oil can be obtained and transported to traditional processing facilities by means of transportation, such as pipelines, trucks or ships. Others 44 200530389 Crude oil has one or more inappropriate properties that make them inferior. Inferior crude oil may be unacceptable to moxibustion transportation vehicles and / or processing facilities, so it has a low economic value. The economic value may lie in a receptacle that holds inferior crude oil that is considered too expensive to manufacture, transport and / or handle. The properties of inferior crude oil may include, but are not limited to: a) a TAN of at least 0.5;) to v 0.2 Pa.s viscosity; c) Specific gravity of at most 19; d) Total state weight of at least 0.00005 g or at least 0.001 g of Ni / V / Fe per gram of crude oil per gram of crude oil per gram of crude oil Total heteroatom content of at least 0.005 grams of heteroatoms; f) φ per G residue of at least 0.01 g of residue; g) asphaltene content of at least 0.004 grams of asphaltene per gram of crude oil; h) MCR content of at least 0.02 grams of MCR per gram of crude oil, or a combination thereof. In some specific examples, the low-grade crude oil may include at least 0.2 grams of residue, at least 0.3 grams of residue, at least 0.5 grams of residue, or at least 0.9 grams of residue per gram of low-grade crude oil. In some specific examples, the low-grade crude oil contains 彳 0.2-0.09 grams, 0.3.09 grams, or 0.4-0.7 grams of residue per gram of low-grade crude oil. In some specific examples, The grade crude oil may have a sulfur content of at least, 0.001 grams, to 10,000 grams, at least 0.01 grams, or at least 0.02 grams per gram of grade crude oil. The grade crude oil may contain hydrocarbons having a range of boiling points Low-grade crude oil can contain at least 0.001 grams, at least 0.05 grams, or at least 0.01 grams per gram of low-grade crude oil. The boiling range is distributed between 2000 and 300 at 0. 101 MPa. Hydrocarbons in between; at least 0.00 g, at least 0.05 g, or at least 0.001 g with a boiling range of 0.100 at 0.1011 ^ 3. Hydrocarbons between 4,000 and 400; and at least 0.001 g, at least 0.05 g, or at least 0.0005 gram, and 200530389 g. The boiling range at 0.101 MPa is distributed between 4000c and 700. In some specific examples, in addition to higher boiling components, inferior crude oil can also include: at least 0 001 grams, at least 0⑽5 per gram of inferior crude oil. Grams or at least 0.01 grams of hydrocarbons with a boiling range distribution of at most 2 ° C at 0.101 MPa. Typically, this inferior crude oil has at most 0.2 grams or at most 0.1 grams of such hydrocarbons per gram of inferior crude oil. content. In some specific examples, the low-grade crude oil may include up to 0.9 grams or up to 0-99 grams of furnace φ per gram boiling range distribution. In some specific examples, the low-grade crude oil may also contain at least 0.001 grams of hydrocarbons with a boiling range distribution of at least 650 ° C per gram of low-grade crude oil. In some specific examples, inferior crude oil can contain up to 19 grams or as high as 0.99 grams of hydrocarbons with boiling ranges in the range of 300 and 1,000 per gram. Examples of inferior crudes that can be processed using the methods described herein include, but are not limited to, crudes obtained from the following countries and regions: Canadian Alberta, Venezuelan φ Orinoco, Venezuela, South America California and Alaska North Slope (US

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

Bohai Gulf), China Karamay, Iraq Zagros, Kazakhstan 46 200530389

Caspian) ’Nigeria Offshore, United Kingdom North Sea, Madagascar northwest, Oman and Netherlands Schoonebek. The treatment of inferior crude oil can enhance the properties of inferior crude oil, making the crude oil acceptable for transportation and / or premises. The crude oil and / or inferior crude oil to be processed may be referred to as a "crude oil feed." This crude oil feed may be topped 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 closer to the corresponding properties of West Texas Intermediate (West Texas plus geocentric) crude oil than the crude oil feed, or closer to the counterpart properties of Brent crude oil than the crude oil feed. Compared with the original; the economic value increased by the economic value of the feed. Such crude oil products can be refined with little or no pre-treatment, which improves refining efficiency. The pretreatment may include desulfurization, demetallization, and / or removal of impurities from the crude product.

A method for contacting a crude oil feed according to the present invention is described here. In addition, specific examples of products with various concentrations of light oil, kerosene, diesel, and / or VG0 are manufactured. They usually cannot be produced in the traditional type of method: 'The feed can be derived from-or multiple contacts with hydrogen. Contact in the presence of a medium in a contact zone or a combination of one or more contact zones. The generation may include: Γ ::: 'hydrogen source is generated on the spot. On-the-spot hydrogen source of 20000 ^ — Part of the crude oil feed reacts with inorganic salt catalysts in the range of _ shoulder V degrees, "into ammonia and / or 47 200530389 quality hydrocarbons. On-site generation of hydrogen may include at least Part of the reaction contains an inorganic salt catalyst such as an alkali metal formate. The complete product usually contains the gas, vapor, liquid or mixture thereof produced during the contact. The complete product comprises a crude oil product which is a liquid mixture under STp, and, In some specific examples, and including hydrocarbons that are not condensable at sTp. In some specific examples, the complete product and / or crude product may include solids (such as inorganic solids and / or coke). In some specific examples The solid may be entrained in the liquid and / or vapor produced during the contact. Φ The contact zone usually includes a reactor, a part of the reactor, multiple parts of the reactor, or multiple reactors. It can be used to feed crude oil into Examples of reactors in which materials and hydrogen sources come into contact in the presence of a catalyst include: stacked bed reactors, fixed bed reactors, continuous stirred tank reactors (CSTR), spray reactors, Plug flow reactors, and liquid / liquid contactors. Examples of CSTRs include fluidized bed reactors and ebullated bed reactors. Contact conditions typically include temperature, Lili, crude oil feed flow, complete product flow, residence time, hydrogen source Flow rate or their combination. The contact conditions can be controlled to produce crude oil products with specific properties. The contact temperature range can be 200-800, 300-700. (: Or 400-600 ° C. In which the hydrogen source is a gas In specific examples of supply (such as hydrogen, methane, or ethane), the ratio of gas to crude oil feed typically ranges from 6, 6, 0.

Nni3 / m3, 2-8000 Nm3 / m3, 3-4000 Nm3 / m3 or 5-300 Nm3 / m3. Contacting is usually carried out within a pressure range of 0.1-20 Mpa, 1 · 16 Mpa, 2-10 Mpa, or 4-8 MPa. In some specific examples where steam is added 48 200530389, the ratio of 'steam to crude oil feed' is between 38 kg / kg of crude oil feed and ★. · Within the range of 1-1 kg of steam. Crude oil == to maintain the crude oil feed volume in the contact zone at: 0%, at least 50%, or at least 90% by volume. Typically, the original 4 feed volume in the contact zone is the total contact zone 4G%,% of volume. In some specific examples, the contacting can be done under additional gases such as argon, nitrogen, ethane, ethane, propane, butane, propylene, butene, or a combination thereof. Existing Figure 1疋 A schematic diagram of an example of a contact system used to make a complete product of vapor. The crude oil feed leaves the crude feed supply source 101 and passes through: the conduit HM enters the contact zone 1G2. Used in the contact zone The amount of catalyst can be ^ 00 grams, 2-8 grams, grams or 4-60 grams per 100 grams of crude oil feed in the contact zone. In some specific examples, a diluent can be added to the raw Reduce the viscosity of the crude oil feed. In some specific examples, the crude oil is fed into the bottom of the contact H 102 via the conduit 104. In some specific cases, the crude oil feed can be sent to the contact zone 1 ( ) 2 before and / or during the heating of the crude oil feed to a temperature of at least just .C or at least _ 〇c. The crude oil feed is heated to a temperature in the range of 100-500 ... or 200,0 ... In some specific examples, 'the catalyst is combined with the crude oil feed and then transferred to the contact zone 102. The crude oil feed may be The feed / catalyst mixture is heated to a temperature of at least 1000QC or at least 3000c before being sent to the contact zone 102. Typically, the crude oil feed can be heated to 2000-5 ° C. Or 3 ° C -400% temperature within the dry range. In some specific examples, the crude oil feed / catalyst mixture 49 200530389 is a slurry. In some specific financial situations, the TAN of the crude oil feed can be reduced before :, 'The feed is fed into the contact zone at a temperature ranging from 200 to 3.0 ° C. When the crude oil is heated to C at a temperature in the range of 0 ° C or when an acidic component / medium can be formed in the crude oil feed, the formation can be removed from the crude oil feed t. A 4b acid di-salt. The TAN of these metal test salts. A textual component to reduce the crude oil feed-, in the example, the original area. In the waste plant, the continuous addition to the joint angle ^ in Mixing of contact area 102 can be sufficient / inhibitory, Japanese W heart M inhibitor catalyst and crude oil

Branch / catalyst this compound is separated. In a certain example, a catalyst can be removed from the contact area 10 < to a part of the catalyst, and 4 ^ ^ ^ 〆, in the case of 骽 example, is the type In a specific example, fresh catalyst can be added to the contact area 02 during the reaction sequence.

In some embodiments, the crude oil feed and / or a mixture of the crude oil feed and the inorganic salt catalyst is delivered to 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 days, 10 days, 5 days, or 3 days. Surfactants include, but are not limited to: organic polytarctic acid (Tenax 2101; MeadWestvaco Specialty Product Group; Charleston, South Carolina, U.S.A.), C2] dicarboxylic fatty acid (DIACID 1550;

MeadWestvaco Specialty Product Group), petroleum sulfonate (Hostapur SAS 30; Clarient Corporation, Charlotte, North

Carolina, U.S.A.), Tergital NP-40 Surfactant (Union 50 200530389

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

Baker; Phillipsburg, New Jersey, U.S.A.) The circulation catheter 106 may connect the catheter 108 to the catheter 104. In some specific examples, the 'circulation catheter 106' can directly enter and / or leave the contact area 02. The circulation conduit 106 may include a flow control valve. The flow control valve allows at least a portion of the material to be circulated from the conduit 108 to the conduit 104 and / or the contact area 102. In some specific examples, a condensation unit may be placed in the duct 108 to allow at least a portion of the material to be condensed and recycled to the contact zone 102. In some specific examples, the circulation conduit 106 may be a gas circulation line. Area 102. In some Π4, the 102 flow control valves 110 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 substantially selected volume range is maintained during exposure to [102+ 彳]. The feed volume in the contact zone 102 can be monitored using standard equipment. The gas inlet 112 may be used to allow a hydrogen source and / or additional gas to be added to the crude oil feed as it 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 embodiments, the water-containing steam is introduced via steam. In some embodiments, at least a part of the complete product is steam.

51 200530389 Hydrogen source to crude oil in contact zone 102

The ratio of,, +, and / or the M force in the contact area to control the vapor and / or liquid phase generated from the contact ㊣1022, the pressure in the contact blade Λ X ^ a, d,. In some specific examples, the crude oil feed from the contact zone 包含 contains at least 0.5 grams of steam produced per kilogram to ^, 0.8 grams, at least | 0.97 grams of crude product. In some cases, the steam produced from the contact area M kg contains 0.8-0.99 g or 0.9-0.0 g per gram of crude oil, Gucong, and Nv. 98 grams of crude product. Residual crude feed may be included in contact zone 102 as a contact pass

Used catalysts and / or solids can remain in the sequential by-products. Solid and / or used catalyst and / or coke. In Xiaoyuan Xiaoyuan 116, the steam was separated and cooled using private quasi-separation technology to form crude oil products and gases. The crude oil product leaves the separation unit ιΐ6 and then enters the crude oil product receiver n ″ via the conduit 118. The resulting raw product can be transported and / or processed in a palatable manner. The crude product receiver ⑴1 >

: Or more pipelines,-or more storage units, _ or more transport containers "their combinations. In some specific examples, the separated gas, such as hydrogen, carbon monoxide, carbon dioxide, hydrogen sulfide, or methane, is transported to its processing unit (eg, for use in a fuel cell or sulfur recovery facility) and / or by sea 120 Circulate to the contact zone 102. In some specific examples, quasi-physical separation methods (such as filtration, centrifugation, or membrane separation) can be used to remove the solids and / or liquids entrained in the crude oil product. Contact system 1 22 for processing crude oil feed with one or more catalysts to make the finished product, the complete product can be liquid or liquid mixed with gas or solid. Crude oil feed can enter the contact zone via conduit 04 〇2 52 200530389

in. In some specific examples, the crude oil feed is received from a crude feed supply & 104 may include a gas inlet η2. In some specific examples, the gas inlet 112 may directly enter the contact zone 1020. In some specific examples, the krypton inlet 114 may 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 make the complete product. In some specific examples, the catheter 106 allows at least a portion of the complete product to be cycled to contact ^ 102. The mixture containing the complete product and / or solid and / or unreacted crude feed leaves the contact zone 102 and enters the separation zone via conduit 108 "24. In some specific examples, a condensing unit (e.g., in 's 106) can be placed so that at least a portion of the mixture in the conduit can be condensed and shielded to the contact area 102 for further processing. In some specific examples, the circulation conduit 1G6 may be a gas circulation line. In some specific examples, the catheter 108 may include a filter to remove particles from the complete product.

In the knife away zone 1 24. At least a portion of the crude product can be separated from the complete product and / or catalyst. In the specific case where the complete product contains solids, solids can be separated from the complete product using standard solid separation techniques (e.g., centrifugation, transition, decantation, membrane separation). For example, solids, including catalysts, used catalysts and / or coke combinations. In some specific cases, the '-part of the gas system is separated from the complete product. In some specific examples, 'at least a portion of the complete product and, or solids, can be recycled to the lead, 104, and / or in some specific examples,' is recycled to the j-contact zone 102 via the catheter 126. For example, the portion of the cycle may be combined with the crude oil feed and then entered into the contact zone 102 for in-step processing. Crude products can leave the branch 124 via: Officer 128. In some specific examples, crude oil can be transported to a crude product receiver. In some specific examples, the complete product and / or at least one crude oil product may contain catalysts to. Entrained in the complete product and / bite; + _ Kesha Tian Shen, Zhu Zhu a 4 crude oil product J using standard gas / liquid separation technology .. „v 1 J Ge rent injection, membrane separation and pressure reduction, and give Is separated. In some specific examples, $ # ^ i Y is used to transport the separated gas: other processing orders "for example, for use in fuel cells, sulfur recovery equipment, and other processing early yuan or combinations thereof) and / or Cycle to contact area.

In some embodiments, separation of at least a portion of the crude oil feed is performed before the crude oil feed enters the contact zone. Figure 3 is a schematic diagram of a specific example of a combination of a separation zone and a contact system. The contact system 130 may be a contact system 100 m (shown in FIGS. 1 and 2). The crude oil feed enters the separation zone 132 via the guide 104. In the separation zone 132, a standard score is used

Isolation technology separates at least a portion of the crude feed to produce a separate crude feed and hydrocarbons. The separated crude oil feed, in some specific examples, includes a boiling range distribution of at least 100. (:, A mixture of ingredients of at least 1 200 ° C, or, in some specific examples, the system contains a boiling range distribution of at least 200. (3. Typically, the separated crude feed contains a boiling range distribution in the 100- A mixture of ingredients between 1000 ° C, 120-900 ° C, or 200-800 0C. The hydrocarbons separated from the crude oil feed are separated from the separation zone 1 3 2 via conduits 1 3 4 and transported to other processing units and processing facilities. , Storage facilities, or a combination thereof. At least a portion of the separated crude oil feed leaves separation zone 132 and enters contact system 1 30 via conduit 1 36 for further processing to form a crude product, which leaves contact system 130 via conduit 138. 54 200530389 In some specific examples, the crude oil product produced by any of the methods described in this article by using Tai and 隹 M ^ is the same as or different from the crude oil feed

Of crude oil. For example, the crude oil product may be imaginary and present; ^ π # A — Du Qing j Xing crude oil with different viscosities; Kai 'hunting this produces a blended product with a viscosity between the viscosity of the crude product and the viscosity of the crude oil. The resulting blended product may be suitable for transportation and / or handling. Figure 4 shows a specific example of the combination of the blending zone 14o and the contact system 13o. In some specific examples, at least-a portion of the crude product exits the contact system 130 via the guide CU and enters the blending zone-.推 in the push zone

If a lesser portion of the crude oil product is combined with one or more processing streams (e.g., a hydrocarbon stream or light oil made from one or more crude oil feeds), crude oil, crude oil feeds, or mixtures thereof to produce a blended product. Processing stream, crude oil = 'crude oil or its mixture is sent directly to blend @ 140 or upstream of blending zone via h 142. The mixing system can be located in the push zone Mo or near the product can meet specific product specifications. Specific product specifications include, but are not limited to:-Range or limit of API specific gravity, TAN, viscosity or combinations thereof. The cleavage product leaves the blending region 14 through the guide 144 and

Be transported and / or processed. In some specific examples, methanol is produced using a catalyst during the contact process. For example, hydrogen and carbon monoxide can react to form methanol. The recovered methanol may have ridged salts such as potassium hydroxide. The recovered methanol can be combined with additional crude feed to form a crude feed / methanol mixture. Combining methanol with a crude oil feed easily reduces the viscosity of the crude oil feed. Heating the crude feed / alcohol mixture to at most 5000 ° C can reduce the TAN of the crude feed to less than one. 55 200530389 Figure 5 shows the specific example of the combination of separation zone, contact system and blending zone. The crude oil feed enters separation zone 132 through conduit 104. The crude oil feed is separated as described previously to form a separate crude oil feed. The separated crude feed enters the contact system 13 via t136. The crude product leaves the contact system, system 130, and enters blending zone 140 via conduit 138. In the blending zone j40, other processing streams and / or crude oil fed through the conduit 142 are combined with the 3 crude oil product to form a blended product. The blended product exits the blended region 140 via the channel 144.

Schematic diagram of the return contact system 1 46. The contact system 1 00 (f) can be placed before the contact system 148. In an alternative specific example, the system 148 may include-or multiple catalysts. The catalyst of the contact system 14 " may be an inorganic salt catalyst, a transition metal sulfide catalyst, a market catalyst, or a mixture thereof. 、, 山; 隹 利 原 原, enter the contact device from the inlet system through the conduit 104, 100 ', and then contact the hydrogen source in the presence of an inorganic salt catalyst to make a difference. The complete product contains hydrogen, in some specific examples

product. The complete product can be contacted to the system 100 via the catheter 10, 3 ′, ^, t, and 离. The hydrogen produced from the catalyst, the catalyst, and the crude oil feed can be used to connect to the 14 "⑷hara. At least a part of the hydrogen produced is transferred to the contact system M8 via the contact system 100 :: In the alternative embodiment, the chlorine produced as such can be transmitted through the conduit 15. To the contact system, the system 148: In the example, the system 148 can be contacted with the chlorine produced by the state Got directly from the contact system 丨. . Flow to contact system II'1 56 200530389 In some specific examples, the vapour stream produced from the contact system_ is directly fed into the crude oil feed mixture of the contact system M8. The second crude oil feed enters the contact system 148 via the conduit 152 into the contact system 148. The contact of the crude feed with at least a portion of the hydrogen and catalyst produced produces a product. The product is a complete product in some specific examples. The product exits the contact system via conduit 154.

In some specific examples, a system including a contact system, a contact zone, a separation zone, and / or a blending zone, such as those shown in Figure 1.6, may be located at or near a manufacturing site that produces inferior crude oil feeds. After processing through the catalyst system, the crude feed can be considered suitable for transportation and / or use in a refining process. In some specific examples, crude oil products and / or blended products are shipped to refining and / or processing facilities. Crude products and / or blended products can be processed to make commercially available products, such as transportation fuels, heating fuels, lubricants, or chemicals. Processing may include steaming and / or fractionating the crude product and / or blended product to make one or more fractions. In some embodiments, crude oil products, blended products, and / or one or more fractions may be hydrotreated.

In some specific examples, the 'complete product' comprises at most 0.05 g, at most 0.03 g, or at most 0.01 g of coke per gram of complete product. In some instances, the ' complete product is substantially free of coke (i.e., coke-based: undetectable). In some specific examples, the 'crude oil product' may contain at most 0.05 g, at most 0.03 g, at most 0.001 g at most " 05 g or at most 0.003 g of coke per gram of crude product. In some specific examples, the crude oil product has a denier in the range of from 0 to 0.05, 0.0001-grams, 0.0001-0.01 grams, or 0.001-0.005 grams per gram of crude product, … W fire 3 miles' or 57 200530389 is untestable. In some specific examples, the crude product has an MCR content of up to 90%, at most 嶋, at most 50%, at most %%, or at most 10% of the MCR content of the crude feed. In some specific examples, crude oil products have a negligible job content. Some specific crude oil products contain at most 0.05 grams, at most 003 grams at most 200 grams, or at most 0.1 grams. Typically, crude oil products contain MCRs ranging from 0 g to 1 g, G._G1G, G3, or G0 •• g per gram of crude product. ::: In a specific example, the complete product contains a non-condensable gas. Non-condensable gas barriers include, but are not limited to, carbon dioxide, ammonia, hydrogen sulfide, hydrogen, carbon monoxide, methane, other hydrocarbons or their mixtures that cannot be reduced under STp. In some specific examples, hydrogen, carbon dioxide, carbon monoxide, or a combination thereof: steam and light hydrocarbons are in contact with an inorganic salt catalyst and when: in terms of mol, 'under thermodynamic conditions, carbon monoxide on X2 The mole ratio is 0.07. In some specific examples, Shishan Congshan, an Emulsified Emulsified Emulsion Stone 07, was produced. Here: the ear ratio is at least 0.3, at least 0.5, or at least the molar ratio of carbon: in a body example, the carbon monoxide produced versus the dioxide produced. 1.0, 0.4-0.9, or 0.5-. · Within the range of 8. The ability to prioritize carbon dioxide can be beneficial to other processes located in the domain or upstream. For example, the produced -oxidation reaction can be used as a scavenger in the process of processing & a, synthesis gas, or used in other procedures such as 58 200530389. In some specific examples, the complete product as prepared herein can be Spoon containing boiling range is distributed in. C and 538. (: Compound mixture between 2) The mixture may contain hydrocarbons having a carbon number in the range of 1 to 4. The mixture is such that per gram of such a mixture may include 0.001_〇8 丨, 0.003_〇 " Grams or 0.005 to 0.01 grams of q hydrocarbons. The q hydrocarbons can be packaged per gram of q hydrocarbons: 0.001-0.8 g, 0.003 g, or 500,000 g of butadiene. In some specific examples, hetero-chain hydrocarbons are prepared at a weight ratio of at most 15, at most 2.4, at most 0-8, at most 0.3, or at most relative to normal-chain hydrocarbons. In some specific examples, the iso-chain hydrocarbons are weighted in the range of 0.00001-1.5, 0.0000 M.0, or 0.001-0.1 with respect to the normal chain smoke = paraffin. The paraffin may include isoparaffin and / or n-chain Paraffinic hydrocarbons. In some specific examples, the complete product and / or crude oil product may contain olefins and / or chain hydrocarbons that are not normally found in crude oils produced and / or obtained from the product. A mixture of terminal ㈣% olefins ") and olefins with intramolecular double bonds. In some specific instances, the dilute hydrocarbon content of the crude product Is a factor of 2, 10, 50, 100, or at least 200 greater than the olefin content of the crude feed. In some specific examples, the #olefin content of the #crude product is up to 1 greater than the olefin content of the crude feed, Factors of 000, at most 500, at most 300, or at most 25. In some specific examples, hydrocarbons having a boiling range in the range of 20 to 400 γ have a smoke distribution in the range of 20 to 40 C per gram. Flue-cured tobacco content in the range of __ 0.1 grams, 0.0001-0.05 grams or 0.01_0; 04 grams. In some specific examples, at least grams, at least 0.005 grams, or at least 0.01 grams of Alpha olefins. In some specific cases, the number of crude oil products is ^^, and the crude oil product contains 0.0001-0.5 $, 0.001-0.2 g, or 0.0001 · 0.1 g of hydrocarbons. Some specific boiling ranges are in the range of 20-400%, and are distributed in the range of 20-400. The gates of the second group have hydrocarbons between 0.0001-0.08 grams, 0.001_0 05 grams, or 0.01-0.04 per gram of boiling range. Alpha thin smoke content in the gram range. In some specific examples, the boiling range is distributed between 20-204. (: Of = Has at least 0.7, at least .8, at least .9, at least the heart: two it: the weight ratio of the dilute smoke to the intramolecular double bond ene smoke. In one example, the boiling range is 0.7 Weight ratio of -10, 〇8_5, and 的 20 204 C-like dilute hydrocarbons with double bonds in the range of $ _3 or W of 01 dilute hydrocarbons to intramolecular bond dilute hydrocarbons ...: oils and commercially available products An increase in the amount of dilute hydrocarbons in the intramolecular double lip ratio, which is usually i-capacity, produces a commercially available product of alpha dilute smoke in the daily cutting edge with intramolecular double bonds. b, which can help transfer the crude oil product in two specific examples. The connection between the crude oil feed and the hydrogen source in the presence of an inorganic salt catalyst can be used to make a Foten range distribution containing straight-chain smoke. …. 4

The smoke between L and G. ^ M ^ t, M alkene has cis and trans double bonds. The weight ratio of the straight olefins with trans-bonds to the straight-chain dilute hydrocarbons with cis 04, at most, and at the same time is at most 22: 4. In some specific examples, the weight ratio of the linear olefin having a trans double o.om 0 π octa-K / double bond is in the range of 1.0 or 0.4.弗 'Futeng range distribution within range 纟 20-204. (: Hydrocarbons within the range * The boiling range is distributed between 20-400 ° C Fan Xi 0.1 g, at least 0 15 g, at least 0. 20 g or at least 60 200530389 0 30 g positive bond The content of hydrocarbons in the normal chain of Yuluo Dongyin and Shiermen * can be in the range of 0.001-0 9 gram of hydrocarbons, η 1 η 〇 ± ~ gram 〇0.8 ～ 8 or 0.2-0.5 grams In some specific examples, 'such hydrocarbons have at most 15' at most]. 4. Weight ratio of isoparaffins to normal paraffins of at most 1.0, at most 0.8, or at most 0.3: m-type fe normal chain Hydrocarbon content, it can be estimated that the normal bond hydrocarbon content of crude oil products is in the range of 9 grams, ㈣ · q 8 grams, or a 0.5 grams per gram of crude oil product.-In some specific examples, crude oil The product has a total Ni / V / Fe content of up to 90%, up to 50%, up to 10%, up to 5% or up to 3% of the core content of the crude oil feed. In some specific examples, the crude oil product system is Each gram of crude oil product contains at most 0.0001 grams, at most 1 x 105 grams or at most! X grams of Nl / V / Fe. In some specific examples, crude oil production has 1 X 1 per gram of crude oil products. 7 grams Total Ni / v / Fe content in the range of 5 X 10.5 g, 3 X 10.7 g to 2 X 1 0-5 g, or i X 10-6 g to! X 10.5 g. In some specific examples, the 'crude oil product has a TAN that is at most 90%, at most 50%, or at most 10% of the TAN of the crude feed. In some specific examples, the crude product may have at most 1, at most 0.5, at most 0, or TAN up to 0.05. In some specific examples, the TAN of the crude product may be in the range of 0.001 to 0.5, 0.01 to 0.2, or 0.05 to 0.1. In some specific examples, the API specific gravity of the crude product is greater than that of crude oil. The API specific gravity of the feed is at least 10%, at least 50%, or at least 90% higher. In some specific examples, the API specific gravity of the crude product is between 13-50, 15-30, or 16-20. 61 200530389 Eight θ In case A, the crude oil product has a total heterogeneity of crude oil feed: 2%, at most 50% or at most total heteroatoms containing two deniers: In the general example, the 'crude oil product has a total heterogeneity of crude oil feed. 10%, at least 40%, or at least 60% of the total heteroatom content. The crude oil product may have a furnace shield of 70% or up to 60% of the sulfur content of the crude feed. , Li λ 3 li. The sulfur content of crude oil products can be at most ⑽ grams, at most 8 grams, at most 0.005 grams, at most 0.004 grams, at most 0.004 grams per gram, and at most 0.003. Grams or up to 0.001 grams. In the above specific example, crude oil is used as a private product and-広 ,,,,,,,,,,,,,,,,,,,,,,,,, 母 母 原油 原油 crude oil products have a range of 0.0001-0 02 grams or 0.005-0. 01 grams Content of sulfur. -In some specific examples, the crude product may have a nitrogen content of up to 90% or up to 80% of the nitrogen content of the crude feed. The nitrogen content of the crude product may be at most ~ _ {, at most 3 g, or at most 0 · _g per gram of crude product. In some specific examples, the crude oil product has a nitrogen content in the range of 3 grams per gram of crude oil or 3 grams per gram of crude oil. In two specific examples, the crude oil product contains 0.05-0.2 g or 0.09-0.15 g of argon per gram of crude product. The h / c of the crude product may be at most 1.8 to 1.7, at most 16, at most 15 or at most 14. In some cases, the H / c of the 'crude oil product' is 27 or • 或 of the crude oil feed. In other specific examples, the crude oil side H / c is 10 (M20%) of the crude oil feed H / C. Crude product H / C within 20% of the crude oil feed H / c represents the hydrogen in the process. Absorption and / or consumption is a minimum of 62 200530389 .: Raw and oil products contain components with boiling points in the _ range. 纟 In some specific examples, the 'crude oil products contain: at least G • ⑻i grams or from Q • ⑼i to 0.5 grams in 0.101 MPa / forten range distribution for at least 2,000 g of t-class' at most 0.0000 g or at least 0.005 g from 0.001 to 0.05 g boiling at 0.001 Mpa l (L distributed around 200. (: hydrocarbons between 3000 and 300c; at least 0.001 g or from 0.001 to 0.5 g boiling range between 300 C and 400 ° C at 100 mpa Hydrocarbons; and at least 0.001 grams or from 0.001 to 0.5 grams of hydrocarbons having a boiling range between 400 ° C and 53.8 ° C at 0-10.1 MPa. In some specific examples The crude oil product has a light oil content of 0.00000-0.2 g, 0.0001-0.1 g, or 0.001-0.05 g per gram of crude oil product. In some specific examples, the crude oil product contains 0.001-0.2 g or 0.01-0.05 grams of lucky oil. In some specific examples, light oils contain up to 0.15 grams, up to 0.1 grams, or up to 0.05 grams of olefins per gram of light oil. In some specific examples, crude oil products Each gram of crude oil product contains 0.00001-0.15 grams, 0.0000 gram_0.005 grams, or 0 001_00.05 grams of olefins. In some specific examples, spring light oil has 0.01 g at most, 0.005 g at most or at most

Qe () () 2 g of benzene content. In some specific examples, the light oil has an undetectable level or is between 1 X 1〇-7 g to 1 X 1 0-2 g, 1 X 10-6 g to 1 X 1 0-5 g, 5 x 104 Benzene content in the range of grams to 1 X 10-4 grams. Compositions containing benzene can be considered hazardous to the process, so crude oil products with relatively low benzene content do not require special treatment. In some specific examples, the light oil may include aromatic compounds. Aromatization 63 200530389 Compounds can include single ring compounds and / or polycyclic cleavage ring compounds can include but do not require early mounting of benzene, p-diphenyl, ethylbenzyl, methylben, o-xylene, m-dimethyl -Ethylmethylbenzene; Ethyl-2-methyl, 2,3-dimethylbenzene; M earth, Ipropylbenzene; 2-Ethyl 14-methyl, methyl-3propylpropylbenzene , I formamidine?, Earth, monomethylbenzene, 2 · ethyl · 2,4'dimethylbenzene. Methylbenzene; ethyl, fluorenylmethylbenzene ~ diethyl 2 tetramethylbenzyl Isopropyl · o-xylene; benzene, toluenebenzene '' xylene, p-xylylene + * species 1 substituted, homogeneous, homogeneous, homologous. Messaging compounds are commercially available from a variety of commercially available products. Made as described in this article ~ Fly with early ingredients for aromatic content. Yizi's crude oil products usually have an enhanced monocyclic type. 0.05-0.15 grams or 0.0001 grams of product are per gram of crude oil products and there are 0 ...... … 9 grams or t 〇〇〇〇! .〇 This 3 mile crude oil product is per gram of crude oil product, ο · 005 · 0.1 · g or 0.01 · 0.05 grams of o-xylene containing ... a crude oil product has a p-xylene content of 30.0005 g / g per gram of crude oil product. 9 grams, light: The increase in the content of aromatic compounds tends to increase the assessment based on the estimation of the crude gasoline potential. Gasoline is not limited to the scorch value calculated for the light oil portion of crude oil. The original = calculated the scorch value in the range of 35 · 60. Burning Value of Gasoline In specific examples, enter: the demand for additives. In some, the crude oil products include light oil with a Li-Sin value of at least 60, at least 70, at least 80 64 200530389, or at least 90. Typically, the scorch value of light oil is in the range of 60-99, 70.98, or 80-95. " 丨 From the ^ I /, in the examples, compared with the total light oil and total square compound content in kerosene in crude oil feed, crude oil products are distributed in the boiling range at 204 ° C and 500 ° ρ / Among the hydrocarbons (total "light oil and kerosene,") have a higher total aromaticized 4 'human p 0 content, and are higher than at least 5%, at least 10%, at least 50%. % Or at least 99〇 /. ^ ^%. Typically, the total compound content of total light oil and kerosene in crude oil products is higher than the total aromatics content of total light oil and kerosene in crude oil feed. 8%, 20%, 75%, or 100% .: In some specific examples, kerosene and light oil may have a total kerosene per gram of ^ 〇.〇〇〇〇〇〇0.5 grams' 0.0001-0 2 grams or The content of total polyaromatic compounds in 〇00. The crude oil product of Ke'anwei crude oil product has a value of 0.0001 ~ 00 0.001-05 per gram of crude oil product. • Brother / gram, 0.005-0.3 grams or 0 · 01-〇 · 2 grams of library outlet fluid contains 2-in some specific examples, the weight ratio of kerosene to diesel in crane outlet fluid is 4 · 1, 1 · 3 to 3 · 1 or 2: 5 to 5: in the range of 2. Less ; In a specific example, the crude oil product contains up to gram per gram of crude product, from 0 to 0.7 g, 0.001-0 5 $ ten gram of 烨, & such as υι υ. 5 grams or 0.01-0.1 An oil. In some specific examples, crude oil products or 0 01 η 1 7 raw cuts of 0.00K 0.5 grams per gram of kerosene. In some specific examples, glow oil has at least 〇2 纟, less "oil See the content of the mother gram coal U, 3 grams or at least 0.4. In some specific examples, the content of aromatic compounds per gram of kerosene per gram or 4 grams of aromatic compounds ranges from 0.1 to 0.5. In some specific examples, the freezing point of kerosene can be at ^ l Below, -65 200530389 below 40 ° C or jo 〇rr; πτ ^ or below. The increase in the aromatic content of the kerosene portion of the crude oil product tends to increase the density of the kerosene portion of the crude oil product and reduce the freezing point. Ao Nang Qiu Ba Mu > ^ Zi coal knife has a southern density and a low freezing point of crude oil products to refine and manufacture the ancient warehouses and houses fuels divided by the right. / In some specific examples, the crude oil product is per gram of crude oil product and has a diesel content in the range of 0.0000 g to 0.8 g or from 0.01 g to 0.4 g. In some examples, the diesel system has an aromatic content of at least 01 grams, at least 0.32, or at least 0.5 grams per gram of diesel. In some specific examples, the oil series has an aromatic compound content per gram of diesel oil in the range of (Mi grams, 0.3-0.8 grams, or 〇2_〇. In some specific examples, the crude oil The product is a VGO content per gram of crude oil product in the range of 0.0001 to 99 grams, from 0 to 001-0 · 8 grams, or from 0 to 1.00 grams. In some specific examples, the vg0 content in the crude product is 疋 per gram of crude oil The product is in the range of 4-0.9 g or 0.6-0.8 g. In some specific examples, VG0 has per gram of VG0 at 0.009 g, 0.3-0.8 g, or 0.5 Aromatic compound content in the range of -0.6 g. In some specific examples, the crude oil product has a residue of up to 70%, up to 50%, up to 30%, up to 10% or up to 1% of the crude oil feed. Guang Li. In some specific examples, the crude oil product has at most 0.1 grams, at most 0.05 grams, at most 0.03 grams, at most 0.02 grams, at most 0.01 grams, and at most 0.05 grams per gram of crude oil products. Or a residue content of at most 0.001 grams. In some specific examples, the crude oil product has a weight of about 10,000 milligrams per gram of crude oil product. Residue content in the range of 0.00001-0.05 g, 0.001-0.03 g, or 0.005-66 200530389 0.004 g. In some specific examples, the raw material is produced by the production of < 6 eight medium. Here and here / crude oil The product may include at least a portion of the contact with one limb. In the example, the crude oil product is less than 0 g but less than 0 Λ Λ. The crude oil product contains 夯 μ 〇〇〇〇001001_0.001 g or 0.0000 g. -〇0001 gram of catalyst. The catalyst can stabilize the crude oil product during transportation. The catalyst has been used to help find the medium during processing in the facility. It can inhibit corrosion and inhibit the water separation ability of friction products. Second, rubbing and / or increasing the crude oil for further processing to produce "β", crude catalyst, crude oil products, lubricants, and / or other commercially available products. The medium can be used to cut a single contact in the presence of a hydrogen source. The catalyst used by Jinke to make complete products or multiple catalysts. The catalyst precursor for this application, the farm name is _ 卩 μ, when the first contact is made, in contact: the second crude oil feed and the catalyst precursor It will be converted into catalyst when it comes into contact with rafts. It is used to make crude oil feed and hydrogen source. To help crude oil feed molecules contact: The catalyst of the whole product can be low, and the language is low. Without wishing to be bound by theory, the combination of the source and source of the catalyst can be contacted with the alkaline and non-alkaline media and the wind and / or super alkali components: Λ test or Brewster-Rorrow test) and the amount. Examples of molecules that can be used to reduce the composition of crude oil feed include the present / or Bronstror's basic catalysts. The catalysts described. In some specific examples, the touch welding is a TMS always contains a type ™ s catalyst. TMS touches 3 compounds with transition metal sulfides. The weight of the two sulfides in the TMS catalyst is determined by the total weight of the atoms in the catalyst and the total weight of sulfur in the catalyst. The transition metal para-sulfur is all A A in the range of 0.2-20, 0.5 · 10, or bu 5. Examples of "transitions" can be found in G Nickless and edited by G Nickless • Inorganic Sulfur Edited by JNickless

Company; Amsterdam — London-New York; Copyright 1968) Chapter 19. In some specific examples, the TMS catalyst system may comprise 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 0.999 grams. In some specific examples, the TMS catalyst system has a total content of one or more transition metal sulfides per gram of catalyst in the range of 0.4 to 0.0999 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 (FeuNUs), Pyrite (Fe6.75Ni2.25Sll), Pyrite (Fe〇7NiG2C〇GiS2), Square Pyrite (FeG75NiG25SG9), Silver-nickel pyrite (AgFe6Ni2s8), isometric Cuban ore (CuFe2S3), isometric chalcopyrite (Cu8Fe9Si6), sphalerite (Zr ^^ FeG ^ S), limonite (Cu9Fe9Si6), pyrite Copper ore (Cu6FeSn2S8), pyrite (, chalcopyrite (CuFeS2), pyrite (FeS), pyrite (FeS2), pyrrhotite (Fe () _ x) s (x == 0 to 〇] 7)), Hethionite (or Sulfurite (NiSj. Lu) In some specific examples, the TMS catalyst contains one or more combinations of alkali metal, earth, zinc, zinc compounds, or mixtures thereof. Transition metal sulfides. In some specific examples, TMs catalysts are represented by the general chemical formula Ac [MA: U, where A represents an alkali metal, alkaline earth metal, or zinc; M is shown in Table 6-1 from the periodic table. Transition metal; and s is sulfur. The atomic ratio of α is in the range of 0.5 to 2.5 or i to 2. [The atomic ratio of α to α is in the range of 0.0001 to 1, 0.1 to 0.8, or 0.3 to 0.5 68 200530389 In some specific examples, the transition metal is iron. In some specific examples, the ™ s catalyst may include commonly known metal and / or earth metal / transition metal sulfides (such as limonite Potassium Dish (K3Fei〇Sl4), Pyrite Potassium Ore (KFe2S3), Pyrite Copper Potassium Dish (K6NaFei9cU4NlS26C1), Chloro-Pyrite (KuFhCiio 2S26 lCl0 7) and / or ferrite (NaFe3KH2) In some specific examples, the TMS media includes limonite bell ore prepared on the spot. The limonite potassium ore prepared on the spot can be called artificial limonite unloading. Natural and / or artificial limonite potassium ore can be Used in the methods described herein. In some specific examples, the TMS catalyst can contain up to 25 grams, up to 15 grams or up to 1 gram of carrier material per ounce. In terms of industry type, TMS catalysts contain carrier materials of 0 to 25 /, 0.00001 S 20 grams, 0.0001 grams to 10 grams per 100 grams of catalyst. Carrier materials that can be used together with Gamma catalyst Examples include refractory oxides, porous carbons, zeolites, or mixtures thereof. In some specific examples, TMS The medium is substantially free of or without a carrier material. G 3 TMS catalysts of alkali metals, alkaline earth metals, zinc, zinc compounds, or mixtures thereof may contain—or multiple transition metal sulfides, bimetallic metal-transition metal sulfide It is said that you have entered the @ 4 Tongji transition to a sulfide, transition metal oxide, or its compound as measured using χ_ray diffraction. Top S catalyst-part of alkali metal component, alkaline earth metal component, zinc component and / or part of transition metal sulfide component 'In some specific examples, it is an amorphous composition that cannot be detected by X-ray diffraction technology Thing exists. 69 200530389

In some specific examples, the mixture of the daily grains of TMS J and / or TMS contact grains has a particle size of at most 108 A, ′, 、 5 ϋ 1 ϋ A, up to 100 A or 夕 40 A. In general practice, the particle size of the TMS catalyst grains is usually at least 10 A. TMS catalysts containing metal, earth, metal, zinc compounds, or mixtures thereof can be obtained by mixing a sufficient amount of deionized water, a required amount of transition metal oxide, and a required amount of 帛 W 櫊 metal carbonate 1 K2 It is prepared by mixing metal oxalate, 1-2 «metal acetate, zinc carbonate, acetate, zinc oxalate, or a mixture thereof to form a wet paste. The wet paste can be made at ^ ⑻% or 150-250. (: Dried at a temperature to form a transition metal oxide / salt mixture. The transition metal oxide / salt mixture can be in the range of 300-1000 ° C, 500-800. (: Or 600-700 (): Calcined at a temperature to form a transition metal oxide metal salt mixture. The transition metal oxide metal salt mixture can react with hydrogen to form a reduced intermediate solid. The addition of hydrogen may be sufficient to provide excess hydrogen to the transition metal. The oxide metal salt mixture is carried out at a flow rate. Hydrogen can be added to the transition metal oxide metal salt mixture over a period of 10-50 hours or 20-40 hours to make a reduced intermediate solid containing the elemental transition metal. Hydrogen addition Can be performed at a temperature of 35-500 ° C, 50-400 0C, or 100-3 00 ° C and a total pressure of 10-15 MPa, 1 1-14 MPa, or 12-13 MPa. It should be understood that The reduction time, reaction temperature, choice of reducing gas, pressure of reducing gas, and / or flow rate of reducing gas to prepare the intermediate solid are usually changed relative to the absolute mass of the selected transition metal oxide. In some specific examples , After reduction Intermediate solids can be passed through a 40-mesh screen with minimal force. 70 200530389 The reduced intermediate solids can be added to the heat incrementally (eg, 〇〇〇.) Can control the rate of heat release and gas generation. ) Diluent / elemental sulfur and / or sulfur-or mixture of compounds. The diluent may include any suitable diluent that provides a means of dispersing the heat of vulcanization. The diluent contains a Foten range distribution of at least 100c, at least 150c , Less than 2 ~ ζυοc or at least 300 ° C. Usually the diluent has a tracer range distribution between 500 ° C, 15 ° _4 °. ^ 2 0 0-3 0 0 ° C In some specific examples, the Swordsman, the diluent is VGO and / or xylene. Sulfur compounds include, but are not limited to: hydrogen sulfide and / or thiols. The amount of sulfur and / or sulfur compounds is the first The molar number of the metal or zinc in the 1-2th column of the metal salt or the salt is used as a reference, and the range of ι can be from i-HH) mol%, 2-80mol%, 5, mol%, 10: 30 mol%. After adding the reduced intermediate solids to the diluent / elemental sulfur mixture, the resulting mixture can be The material is gradually heated to a final temperature of 200-500 γ, 250-45 ()%, or 300-400, and maintained at this final temperature for at least! Hours, at least, 2 hours, or at least 10 hours. Typically, the final The temperature is maintained for 15 hours, 10 hours, 5 hours, or 15 hours. After heating to an elevated vulcanization reaction temperature, the diluent / catalyst mixture can be cooled to 0-100 ° C, 30-90 γ, or 50_80 Temperature in the range of 0 ° C to help recover the catalyst from the mixture. Standard techniques can be used to isolate the sulfurized catalyst from the diluent in an oxygen-free atmosphere and then use at least a portion of a low boiling point solvent (e.g. pentane, heptane Or hexane) to prepare TMS catalyst. This TMS catalyst can be powdered using standard technology. τ In some specific examples, the catalyst is an inorganic salt catalyst. The anion of the inorganic salt catalyst includes an inorganic compound, an organic compound, or a mixture thereof. Inorganic 71 200530389 Salt catalysts include metal carbonate test, metal hydroxide test, metal hydride test, metal turtle test, metal sulfide test, metal acetate test, metal oxalate test, metal formate test, Test metal pyruvate, test metal carbonate, alkaline earth metal hydroxide, test alkaline earth metal hydride, test alkaline earth 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 / CsOH; NaOH / KOH / RbOH; NaOH / KOH / CsOH; K2C03 / Rb2C03 / Cs2C03; Na20 / K20 / K2C03; NaHC03 / KHC03 / Rb2C03; LiHC03 / KHC03 / Rb2C03; KOH / RbOH / CsOH mixed with K2C03 / Rb2C03 / Cs2C03 mixture; K2C03 / CaC03; K2C03 / MgC03; Cs2C03 / CaC03; Cs2C03 / C0 ; KH / CsC03; KOCHO / CaO; Cs0CH0 / CaC03; CsOCHO / Ca (OCHO) 2; NaNH2 / K2C03 / Rb20; K2C03 / CaC03 / Rb2C03; K2C03 / CaC03 / KsC2 / 03C02 ; Or Ca (OH) 2 mixed with K2C03 / Rb2C03 / Cs2C03 mixture. In some specific examples, the inorganic salt catalyst contains at most 0.00001 g, at most 0.001 g, or at most 0.01 g of lithium per gram of the inorganic salt catalyst, which is calculated based on the weight of lithium. In some specific examples, the inorganic salt catalyst contains lithium from 0 g but less than 0.01 g, 0.000001 to 0.001 g, or 0.0001 g per gram, which is calculated based on the weight of lithium. In some specific examples, the inorganic salt catalyst comprises one or more alkali metal salts containing at least 11 of the original 200530389 subsequence. When the inorganic salt catalyst contains two or more bases in the concrete example of the alkali metal pair, the atomic order of the alkali metal is greater than the base number of n. The atomic order is at least 1: 10, 0.2 to 6, or 0 to 3 to 4. In the range, the atomic ratio is in the range of 0.1 to salts containing sodium, potassium, and rhenium. Among them, sodium to potassium 'inorganic salt catalyst can be included; the ratio of sodium to rhenium is in the range of 0.1 to 6. 〇.1 · 6's around $ 巳. · Within the fence. In another example: "two:" Qing's "sodium and potassium salts, the potassium atom, the inorganic salt catalyst contains

In some specific examples, the inorganic salt is also in the range of 4, and the metal is selected from the range 8 to 10 of the periodic table, and the metal is selected from the metal of the periodic table. Compound, ^ metal from column 6 of the periodic table cousin, chemical compound selected from Zhou Ren 周 ▲ 4 4 cousin 6's metal, or a mixture thereof. The genus selected from 8-10 includes but is not limited to: iron, ruthenium, cobalt or nickel. The metal sentence selected from column 6 ^ ^ The genus includes but is not limited to: chromium, molybdenum, or some specific shots. The inorganic salt catalyst is one gram of inorganic salt catalyst or 0.2-0.4 grams of Raney ( Raney) Nickel.

~ In some specific examples, the inorganic salt catalyst also includes a metal oxide selected from the 1-2 and / or 13th columns of the periodic table. A metal selected from the second group: the kernel is not limited to boron or aluminum. Non-limiting examples of metal oxides include oxide (Li2O), potassium oxide (K2O), and calcium oxide (Al2O3). Milk The inorganic salt catalyst does not contain or in some specific examples Substantially free of Lewis acid (such as Bcl3, Marion 3 and S03), Brewster Lowry: (e.g. H3cr, H2S04, HC1 and HN03), gas-forming compositions (e.g. lithopentates) And fossilates) and halides. Inorganic salt catalyst 73 200530389 per gram of inorganic salt catalyst may contain: from 0 g to (M g, 0.001-001.00 g or 0.00000 g): a) halide; b) a gas-forming composition at a temperature of at least 350 or at most 1000%; e) Lewis acid; d) Cloth T. Rory Z or e) a mixture thereof.夂 Inorganic salt catalysts can be prepared using standard techniques. For example, standard mixing techniques (such as grinding and / or comminuting) can be used to combine the required amounts of catalysts into knives. 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 specific examples, a helmet machine on a carrier can be formed in the body of an inorganic salt catalyst by using the U-catalyst. Examples of carriers include: Oxidation, Oxidation, Oxidation, Oxidation, Hydrotalcite, Oxidation, Oxidation, Germanium, Iron, Nickel Oxide, Zinc Oxide, Oxidation Mixture. In some specific examples, the compounds of antimony, antimony, and / or tertiary genus, and the main metal compounds of rhenium and metal are impregnated in the carrier. The inorganic salt is melted or softened by heat or strong, and the ox flesh β / —,, mongolian carrier or metal oxide is carried on and / or on the surface to form an inorganic salt catalyst on the carrier. = The structure of organic salt catalyst is usually in the preset temperature or the temperature range in which the phase loss occurs in the catalyst structure, usually,,, and erix. Sentence hook, permeable and / or migration. The inorganic salt catalyst can become disordered, and there is no substantial change in the composition (such as the decomposition of 4 salts). Do not want to be bound by theory (migration). When the ion distance ::: ;; :: _ ^^ is penetrated by the inorganic salt catalyst, instead of ^ 4 benefit machine and / or hydrogen source can pass through the surface of the inorganic salt catalyst. Infiltration of crude oil feeds and / or hydrogen sources through inorganic salts often results in an increase in the contact area between the inorganic salt catalyst and the crude oil feed and / or hydrogen source. Increasing the contact area and / or active area of the inorganic salt catalyst can generally increase the yield of crude oil products, limit the production of residues and / or coke, and / or promote changes in properties of crude oil products compared to the same properties of the crude oil feed. The disorder of inorganic salt catalysts (such as nonuniformity, permeability, and / or migration) can be determined using DSC method, ion conductivity measurement method, TAP ', visual, ray diffraction, or a combination thereof. Determination.

The method of using TAP to determine catalyst properties is described in the following US cases: No. 4,626,412 to Ebner et al .; No. 5,039,489 to Eaves et al .; and No. 5 264 183 to Ebner et al. ^ Available from Mithra Technologies (Foley, Missouri, USA) ^ Analysis can be in the warm shoulder of 25-850 γ, 50 · 500%, or 60-400 ° c, to 10-50m 2 〇 · ４〇. . The heating rate was in the range and the vacuum was performed in the range of 1 X 10 13 to 1 X 10-8 Torr. Temperature can be guaranteed to change and / or increase as a function of time. The temperature of the inorganic salt catalyst increases, and it is measured that the gas discharged from the inorganic salt catalyst. Examples of the gas discharged from the inorganic salt catalyst include-carbon oxide, carbon dioxide, hydrogen, water, or a mixture thereof. The temperature at which the turning point (a sharp increase) in the release of organic salt catalyst gas was detected was considered to be the temperature at which the inorganic salt catalyst became disordered. In some specific examples, 'the turning point of the inorganic salt catalyst exhaust gas can be detected within a range of temperatures' as measured using TAP. The temperature is referred to as the "TAP temperature". The temperature range used by T and the starting / dish degree is called "minimum tap temperature". 75 200530389 Exhaust gas exhibited by inorganic salt catalyst suitable for contact with crude oil feed

The turning point is between 100-600 and 200-500. (: Or 300-400 ℃ in butyl AP temperature range. Typically, the TAP temperature is in the range of 300-500. In some specific examples, different compositions of suitable inorganic salt catalysts are also Exhibits gas turning points' but at different TAP temperatures. The size of the ionizing turning points associated with the exhaust gas can be an indicator of the order of particles in the crystal structure. In highly ordered crystal structures, ionic particles are usually tightly associated 'Therefore, the release of ions, molecules, gases, or a combination thereof from this structure requires more energy (that is, more heat). In a disordered Lu crystal structure, ions are not the same as ions in a highly ordered crystal structure. Grounds are strongly associated with each other. Due to this lower ionic association, the release of ions, molecules, and / or gases from the disordered crystal structure usually requires less energy, and therefore, from the disordered crystal at a selected temperature The amount of ions and / or gases released by the structure is usually greater than the amount of ions and / or gases released from the highly ordered crystal structure. In some specific cases, when μ-differential calorimetry is heated at 100 ° C When measuring the rate or cooling rate, the dissociation heat of the inorganic salt catalyst can be observed in the range of 50 ° C to 50000c. In the DSC method, the sample can be heated to the first temperature and cooled to room temperature. It is then heated one more time. The transformations observed during the first heating usually represent entrained water and / or solvents, and may not represent dissociation heat. For example, it is easy to observe the thirst or hydration of samples The heat of drying may usually appear below 2500c, typically between 100: 50c. The transition observed during the cooling cycle and the second heating is equivalent to the heat of dissociation of the sample. 76 200530389 The "thermal transition" system Refers to the process that occurs when the temperature of the DSC analysis increases when the ordered seeds and / or atoms in a structure become disordered. "Cold transition" means during the DSC analysis' when the temperature decreases, A process that occurs when ordered molecules and / or atoms in a structure become more homogeneous. In the body column, the thermal / cold transition of inorganic salt catalysts occurs within the range of D / Q: Inorganic salt contact during the second heating cycle The temperature or temperature range is called the "cold temperature". The lowest Dsc temperature in the temperature range during the second heating of the German nuclear is called the "maximum temperature". The inorganic salt catalyst can be at 20 (M00 〇c, 25 〇 · The thermal transition is exhibited in the range between 45 ° c or 300 ° C. In inorganic salts containing inorganic salt particles in a fairly homogeneous mixture, the spikes of heat absorbed during the second heating cycle may be comparable Narrow = In the case of inorganic salts containing inorganic salt particles in a rather heterogeneous mixture, the peaks of the heat absorbed during the second heating cycle may be phase two. The absence of peaks in the DSC spectrum indicates that the salt is being scanned. Does not absorb or release heat at temperature. No thermal transition usually indicates that the sample structure does not change when heated.: The uniformity of the particles in the inorganic salt mixture increases, and the ability of the mixture to maintain solid and / or semi-liquid decreases. The properties of inorganic mixtures may be related to the ionic radius of the cations in the mixture. Compared with the dihalfnium cation and f, the cation and the corresponding anion have an increased ability to divide the ancient electron density, so the acidity of the corresponding anion increases: = For similarly charged ions, if the anion is the main ion, For the AI test, the smaller + ”results in a higher ion attraction between the cation and the anion 77 200530389 gravity. Higher inter-ionic% α + ^, and gravity tend to lead to higher thermal transition temperatures of the salt and / or more salt in the salt (a sharper spike and increased DSC) ≫ Product below the curve). Mixtures containing cations with a small ionic radius tend to be more acidic than the% ions of the chevrolet heterozygote, so the acid salt of the inorganic salt mixture 卩 左 阻 # 7, 7 is inferior ^ addition the ion radius decreases and increases. For example, the crude oil feed was contacted with a hydrogen source in the presence of an inorganic mixture containing a clock cation before the crude oil feed and the gas source existed in an inorganic salt catalyst containing a cation with a radius greater than that of the clock. Under contact, tend to produce increased amounts of lice 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 ware-less minimum DSC temperatures for each of the inorganic salts. The minimum DSC temperature of the inorganic salt catalyst may be below the minimum DSC and temperature of at least one of the inorganic metal salts in the inorganic salt catalyst. For example, the inorganic salt tentacle may include potassium carbonate and carbonate shavings. Potassium carbonate and carbonate shavings show dsc greater than 500

The K2C〇3 / Rb2C03 / Cs2C03 catalyst exhibits a DSC temperature in the range of 290-300 ° C. In some specific examples, the TAP temperature may be between the DSC temperature of at least one of the inorganic salts and the DSC temperature of the inorganic salt catalyst. For example, the TAP temperature of the inorganic salt catalyst can be in the range of 350-500. The DSC temperature of the same inorganic salt catalyst can be in the range of 200-300, while the DSC temperature of individual salts can be at least 500 ° C or at most 100,000. In many specific examples, there are between 150-500. (:, 2 () () _ 45 () 〇c or 300-400 CC TAP and / or DSC temperature and inorganic salt catalysts that do not decompose at these 78 200530389 / m degrees can be used to catalyze The conversion of high molecular weight and / or high viscosity compositions (such as crude oil feeds) into liquid products. In the course of a 4b: ,,,-/, spiritual example, at 2000_60000c, 300_50000c, or 3 50-450 ° C, Xizhan During heating of the inorganic salt catalyst in the m μ range, the inorganic salt catalyst may exhibit an increased conductivity compared to individual inorganic salts. The increased conductivity of inorganic salt catalysts is usually due to the particles in the inorganic salt catalyst becoming migratable. The temperature at which the ionic conductivity of some inorganic salt catalysts changes is lower than the temperature at which the conductivity of the single-component ions in the inorganic salt catalysts changes.

The ionic conductivity of the inorganic salt can be determined by the ㈣ law to determine n, 疋 r 疋 voltage, / is the current, and is the resistance. To measure ionic conductivity, an inorganic salt catalyst can be placed in a quartz container with two metal wires (such as copper or platinum wires) separated from each other but immersed in the inorganic salt catalyst.

Figure 7 is a schematic diagram of a system that can be used to measure ion conductivity. The quartz container 156 containing the sample 158 may be placed in a heating device t and gradually heated to a desired temperature. A voltage from the power source 16 is applied to the line 162 during heating. The resulting current passes through the metal wire 162 # 164 and is measured at meter ⑹. The meter 166 may be (but not limited to) a multimeter or Wheatstone bridge. As the sample becomes more uneven (more transferable) without decomposition, the resistance of the sample should be reduced and the meter] The observed current should increase. In some specific examples, at the desired temperature, the inorganic salt catalyst may have different ionic conductivity after being force-heated, cooled, and then heated. Differences in ionic conductivity may indicate inorganic The crystal structure of the salt catalyst has been changed from its original shape (section-morphology) during the pupa period. 2005 200530389. After heating, if i ' In ancient times, the ionic conductivity is expected to be similar or the same.… Occasionally / again. In some specific examples, no 20-500 η ^ +… the branch catalyst has a range of 10-1000 microns, 500 ι Card 4 50-100 machine salt catalyst through the net or sieve to determine the size of the mule in the perimeter 'as the inorganic salt-free catalyst is heated to 50... Above and at 500. May soften at temperature. When the machine scoops down / μ I catalyst, Body and the catalyst particles may

In the inorganic salt catalyst matrix, the catalyst particles are heated, and the catalyst particle field is heated to at least 300 ° T. _ 5 ^ 0 c or at most _ ° c, under gravity or under a force of at least G.0G7MPa or at most G1GlMpa, 幵 > 'Make the alpha machine trip data; the total glyph form is transformed into the second form . When the beneficial organic salt catalyst is cooled to 20 ° Γ r ±, the city > Yes, the second form of organic salt catalyst cannot return to the first form of hot branch salt catalyst. The degree of transformation of the helmet from the first form to the second form r is called "deformation, temperature. The deformation temperature can be a temperature range or a temperature earlier. In a certain and" 1 # 者 点 丨 + ". In the example of the eighteenth edition, the deformation temperature of the inorganic salt catalyst particles is increased below the deformation temperature of any of the individual inorganic metal salts;

=: " Or self-deformation under roof force. In some specific examples, the inorganic salt contact contains two or more inorganic salts having different deformation temperatures. In some I

In the example, the change temperature of the inorganic salt catalyst is different from that of the personal computer S. ~, In some specific examples, the inorganic salt catalyst 纟 TAP and / or DSC is liquid and / or semi-liquid at a temperature above or above. In some specific examples, the salt catalyst is liquid or semi-liquid at the minimum TAP and / or Dsc temperature. At 80 200530389, \ AP and 7 or DSC temperature or above 'In some specific examples, a liquid or semi-liquid inorganic salt catalyst that enters u will form a phase separate from the crude feed. In some specific examples, at the minimum M temperature, the = semi-liquid inorganic salt catalyst has a low solubility in the crude oil feed (for example, the mother gram crude oil feed is from 0 grams to G.5 grams, ~ deleted ... grams or Please 〇1_ two grams of inorganic salt catalyst) or insoluble crude oil feed (for example, one gram of original salt inorganic catalyst). 〇〇1_0 · 01 gram-In some specific examples, the method is used to determine the interval between atoms in the plutonium catalyst. The shape of the χ · ray spectrum can be monitored and the inorganic salt particles 001 can be estimated. The peak represents the difference of the inorganic salt catalyst. The sharpness in the second shot can be ^ D 4 In powder diffraction, the GG1 peak can be estimated and the atom can be estimated. Interval. In inorganic salt catalysts containing high-yield shore = salt atoms, the shape of the Dooi peak is quite narrow ^. The order of the inorganic salt atom is in the order of ... (for example, it may not exist. To determine whether the beneficial order of the inorganic salt atom changes during heating, you can obtain this anomaly: P-ray diffraction pattern, and after adding 埶 & ^ The comparison of μ is almost equal to the force of…. After 50. 0…: After the heat is taken, the ray diffraction pattern is taken.

^ r, in the χ-ray diffraction pattern obtained by the degree, D 2 (:: in the inorganic salt atom) may not exist, or ... ο. /: Don't: :: Γ × · The peaks in the diffraction pattern are broad. In addition, the two ::; χ-ray diffraction circular samples can exhibit a relatively narrow temperature at the same temperature. Crude products) may vary for a given crude feed. Complete product compositions include, but are not limited to, paraffins, olefins, aromatics, or mixtures thereof. This difference ^ ^ ^ ^ ^ ^ ^ A G σ matter constitutes a composition of crude oil products and non-condensable hydrocarbon gas.

The combination of controlled contact conditions with the catalysts described herein can produce a complete product with lower radon content than expected. Comparing the contents of various crude oils allows crude oils to be classified according to their tendency to form coke. For example, a crude oil having an MCR content of 0.1 grams of MCR per gram of crude oil is expected to form more coke than a crude oil having an MCR content of 0.0CU grams per 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 up to 0.01 g, up to 0.05 g, or up to 0.03 g of residue and / Or coke. In some specific examples, the weight of the residue and / or coke deposited on the catalyst is in the range of 0.001-0.01 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 per gram of crude product is at most 0.015 g, at most 0.01 g, at most 0.005 g, or at most 0.003 g. The amount of coke and / or residue produced by contacting the crude oil feed with the catalyst under controlled conditions is relative to the amount of coke and / or residue produced by heating the crude oil feed in the presence or absence of a refining catalyst using the same contact conditions. Reduced amount of coke and / or residue. 82 200530389 In some specific examples, the contact conditions can be controlled so that each material is at least. .5 grams, at least. .7 grams, at least. .8 grams or at least = crude feed is converted to crude product. Typically, 0.5 to 0.99 grams, 0. " 9 grams or 0.78 grams of crude oil product is produced per gram of crude oil feed during the contact. The crude feed is converted to a crude product with minimal residue and / or coke production (if any) in the crude product, so that the crude product can be converted to a commercial product at a refinery with minimal pretreatment. In some specific examples, at most 0.2 grams, at most 0.00 grams, at most 0.05 grams, at most 0.03 grams, or at most 0.01 grams of crude oil feed per gram of crude oil feed is converted into crude oil. Into non-condensable hydrocarbons. In some specific examples, 0 to g, 0.0001 to 0.1 g, 0.001 to 0.05 g, or 0.001 to 0.003 g of non-condensable hydrocarbons are produced per gram of crude oil feed. The temperature of the contact zone, the flow rate of the crude oil feed, the flow rate of the complete product, the flow rate of the catalyst feed, and / or the amount, or a combination thereof, are controlled to maintain the desired reaction temperature. In some specific examples, the temperature control in the contact zone can be performed by changing the flow of a gaseous hydrogen source and / or an inert gas through the contact zone to dilute the amount of hydrogen and / or remove excess heat from the contact zone. _ In some specific examples, the temperature in the contact zone can be controlled so that the temperature in the contact zone is the desired temperature "τ], or above or below it. In some specific examples, the contact temperature is controlled such that The contact zone temperature is below the minimum TAP / J2L degree and / or the minimum DSC temperature. In some specific examples, the temperature may be 300 ° C, 2 (C) below the minimum TAP temperature and / or minimum DSC temperature, or The following 10. (: For example, in a specific example, when the minimum TAP temperature and / or the minimum DSC temperature is 400, the contact temperature can be controlled to 370 ° C, 380 ° during the reaction period. C or 390 ° C. In other specific embodiments, the contact temperature is controlled such that the temperature is or above the catalyst TAP temperature and / or the catalyst DSC temperature. For example, when the minimum TAP temperature and / or the minimum DSC temperature When the temperature is 45 ° C, the contact temperature can be changed to 45 ° C, 500 ° C, or 5500c during the reaction =. The contact temperature can be improved according to the catalyst τΑρ μ degree and / or the catalyst DSC temperature, which can be improved. Properties of crude oil products. For example, this control reduces coke Carbon generation, reduction of non-condensable gas generation, or a combination thereof.

In some specific examples, the inorganic salt catalyst can be adjusted before the crude oil feed is added. 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 to 3 G0. (:, The first temperature of at least 4GG ° c or at least 50000C, and then the inorganic salt catalyst is cooled to at most 25 (QC), at most fine. C or at least 100 c. The second temperature. In each case, the inorganic salt catalyst is heated to a temperature in the range of 150-700 ℃, op 々, υ 600 C, or 300-500 Qc, and then cooled to 25-240 J 〇 240 C, 3〇_2〇〇〇c or 5〇_90% range

Within the second temperature. Adjust the temperature and the field temperature, and then determine the ion conductivity at different temperatures. In this case, the adjustment temperature can be determined from the silent temperature of the thermal / cold transition obtained by heating and cooling the inorganic salt catalyst multiple times in DSC. The adjustment of the inorganic salt catalyst can allow the contact of the crude oil feed at a lower reaction temperature than that of conventional hydroprocessing catalysts. The content in the complete product in some specific examples is light. The oil, distillate, VGO or mixtures thereof can be changed by changing the rate of removing the complete product 84 200530389 t from the contact zone. For example, reducing the rate of complete product removal tends to increase the contact time between the crude feed and the catalyst. Alternatively, increasing the pressure of the initial force can increase the contact time, can increase the production of crude oil products / =: Γ speed of crude oil feed or hydrogen source can increase the blending of hydrogen from gas two ... products, or can change these A combination of effects. Increased connection of raw materials and catalyst # μ 、 / Jinhua oil, coal odor to a shorter contact time, the amount of raw oil A VG0, can increase the amount of oil, kerosene or light oil And a reduced amount of VG0. 1: The contact time can also change the average carbon number of crude oil products :::::

Lower carbon number to h weight percentage (hence higher API than Dong). In the specific implementation example of # «, the contact conditions may change with time. It is possible to increase the contact pressure and / or contact, and to make the product of crude oil gas, w4 s, add the wind of the absorbent of the crude oil feed. Change the amount of hydrogen absorption of crude oil feed, and improve the quality of crude oil feed. Other crude oil products can be produced from a single crude feed version. The shipping and / or handling specifications are not met. The absorption of H / d can be compared by comparing the H / C of the crude oil feed with the crude oil product ... The increase in the product H / c relative to the crude feed h / c indicates that oxygen is added to the crude oil from a hydrogen source. Clothing, products. The H / C ratio of crude oil products is quite low (== when compared with crude oil feed), which means that it is equivalent to a wattage during processing. Significant improvements in crude oil properties relative to crude oil feeders with minimal hydrogen consumption are desirable. The ratio of hydrogen source to crude oil can be altered to change the properties of crude oil products. 85 200530389 For example, 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. In some specific examples, the contact between crude oil feed and inorganic salt catalyst in the presence of light hydrocarbons and / or steam ^ compared to crude oil feed and inorganic salt catalyst in lice and steam In the presence of contact, the total amount of liquid smoke and less M 隹 is produced in the crude oil product; ϋ, ",, and fire. Contact with crude oil feed and f-alkane in the presence of inorganic salt catalysts In the case of Jiyin / Fushi, Hongbei, at least a part of the components of the crude oil product may include the ingredients that have been incorporated into the composition; the knife, the atomic carbon and hydrogen in the mouth structure (from the gauge A). In some specific In the example, crude oil produced from crude oil feeds in which β and human lice sources were contacted in the presence of inorganic salt catalysts. Table 4 shows the volume of crude oil products, which are compared to crude oil products produced from the thermal process under STP. The physical volume of the seat is at least 5% larger than the household size of 1 Γ to 1100%. The total volume of the crude oil produced through the contact between the crude oil feed and the inorganic salt catalyst can be as large as 4 Crude oil feed: at least 110% by volume under STP. Zirconium workers' baskets The increase in product volume is due to the decrease in density. Lower density is usually at least-due to use. Caused by the hydrogenation of crude oil feeds In some specific examples, each gram of crude oil feed contains at least 0.05 grams or at least 0 gram of sulfur and / or at least 0.02 grams of crude oil feed system and hydrogen source in inorganic salts Catalytic activity of the vehicle. Removal of one or more stains without impairing the contact includes, but is not limited to. Sulfide Contaminants In some embodiments, inorganic salt catalysts can be regenerated at least partially by fouling catalyst components. Thanks to: Metals, sulfides, nitrogen, coke or mixtures of them: 86 200530389 It can be contacted with inorganic salts that have been used to generate hydrogen sulfide through the transfer of materials, ★ $ _ γ, / fly and carbon dioxide and used catalysts. MEDIA Removed. Nitrogen contamination can be removed by contacting the used inorganic salt catalyst with steam to produce ammonia. Coke pollutants can be removed by contacting the used inorganic salt catalyst with steam and / or methylbenzene to generate hydrogen and carbon oxides. In some specific examples, one or more gas systems are produced from a mixture of an inorganic salt catalyst and a residual crude oil feed. In some specific examples, a used inorganic salt (e.g., K2co3 / Rb2C03 / Cs2C03; κ⑽Al2〇3; Cs2c03 / CaC03); or

Na〇H / KOH / LiOH / Zr〇2), unreacted crude oil feed and / or residue and / or burnt mixture in the presence of steam, hydrogen, carbon dioxide and / or light hydrocarbons heated to 700- A temperature in the range of 1000 ℃ or 800-900 γ, until the generation of gas and / or liquid is minimized to produce a liquid phase and / or a gas. The gas may include an increased amount of hydrogen and / or carbon dioxide relative to the reaction gas. For example, the gas may include from 01 to 99 moles or 0 to 8 moles of hydrogen and / or carbon dioxide per mole of reactive gas. The gas may contain relatively low amounts of light hydrocarbons and / or carbon monoxide. For example, less than 0.05 grams of light hydrocarbons per gram of gas and less than 0.01 grams of carbon monoxide per gram of gas. The liquid phase may contain water, for example, greater than 0.5-0.99 grams or greater than 0.9 · 0.9 grams of water per gram of liquid. In some specific examples, used catalysts and / or solids in the contact zone can be treated to recover metals (such as hunger and / or nickel) from the used catalysts and / or solids. Used catalysts and / or solids can generally be treated using known metal separation techniques, such as heat, 4D treatment and / or gasification. Examples 87 200530389 Non-limiting examples of catalyst preparation, catalyst testing, and systems with controlled contact conditions are described below. . Preparation of K-Fe sulfide catalyst. A K-Fe sulfide catalyst system is prepared as follows: 1. Combine 1000 g of iron oxide (Fe203) and 58 g of potassium carbonate with 4 12 g of deionized water. To form a wet paste. The wet paste was at 200 ° C. (: Dried to form an iron oxide / potassium carbonate mixture. The iron oxide / potassium invertate mixture was calcined at 500 ° C to form an iron oxide / potassium carbonate mixture. The iron oxide / potassium carbonate mixture was reacted with hydrogen to Formed selected intermediate solids containing ferrous metals. The addition of hydrogen was performed at 450 ° C and 1 5-1 · 2.22 MPa (1665-1765 psi) for 48 hours. The intermediates were made with minimal force Pass through a 40-mesh sieve. The intermediate solid is added incrementally at a controlled exothermic rate to produce a gas at 100 C to the VGO / m-xylene / elemental sulfur mixture. After the intermediate 1 solid is added, the resulting mixture is incremented. It is heated to 3⑼❶c and maintained at 300 ° C for 1 hour. The solvent / catalyst mixture is cooled below 1000 and the sulfurized catalyst is separated from the mixture. The sulfurized catalyst is passed to the lice in the dry phase. Filter and isolate in the atmosphere, and then wash with m-xylene to obtain 544.7 g of K-Fe sulfide catalyst. This catalyst was pulverized by passing the K_Fe sulfide catalyst_ through a 40-mesh screen. Analysis of K_Fe sulfides using x-ray diffraction The catalyst was analyzed by X-ray diffraction pattern, and the catalyst was determined to contain sulfide iron (FeS), K Fe sulfide (KFeS2), pyrrhotite and iron oxides (eg magnetite 'Fe3〇4 ). No peaks related to iron disulfide (such as pyrite, FeS2) were observed in the χ provincial line diffraction pattern. Sulfide contacted in Longgong 88 200530389 A 600 ml continuous stirred tank reactor (by 316 stainless steel structure.) With a bottom inlet, a single steam outlet, three thermocouples located inside the reactor, and shaft movement! 25-inch diameter six-blade Rushton turbine. Will be as in Example 1 The K-Fe sulfide catalyst (10.3 g) prepared as described above was filled into this reaction state. Nitrogen was metered into the reaction at 8,000 Nm3 / m3 (50,000 SCFB). The tank is mixed with asphalt (Lloydminster region, Canada). The asphalt enters the reactor through the bottom inlet feed port to form a hydrogen / crude oil feed mixture. During the 85-hour reaction operation period , Hydrogen and crude oil feed are continuously fed into the reactor, and the outflow The product was continuously taken out from the steam port. The crude oil feed was fed at a rate of 67.0 g / hr to maintain the crude oil feed liquid level at 60% of the reactor volume. Use 50 micro courtesy! 37Cs γ-ray source and iodine A sodium hydroxide scintillation detector is used to measure the liquid level in the reactor. The hydrogen / crude oil feed is in contact with the catalyst at an average internal reactor temperature of 430 ° C. The contact between the hydrogen / crude oil feed and the catalyst is rendered as The reactor exits the complete product in the form of vapor. The reactor exit vapor exits the vessel through the single upper exit port. The top of the reactor was electrically heated to 43 ° to avoid the reaction that the effluent vapor was condensed inside the top of the reactor. After leaving the reactor, the reactor effluent vapor was cooled and separated in a high pressure gas / liquid separator and a low pressure gas / liquid separator to produce liquid and gas flows. The gas stream is sent to a countercurrent alkaline scrubber to remove acid gases and then quantified using private quasi-chromatographic techniques. The complete product is 0.918 grams of crude product and 0.089 grams of non-condensable hydrocarbon gas per gram of complete product. In the reactor, there were 0.027 grams of solid residue per gram of 89 200530389 crude oil feed. The properties and composition of the crude product and non-condensable hydrocarbon gas produced by this method are summarized in Table 2 of FIG. 8 and Table 3 of FIG. 10.表表 丨 图 9 This embodiment demonstrates a method for producing a complete product by contacting a crude oil feed with chlorine in the presence of a transition metal sulfide catalyst with minimal coke contamination. The complete product contains crude oil products that are liquid mixtures at STp and contains up to 0.01 grams of non-condensable hydrocarbon gas per gram of complete product. By comparing the MCR content of the crude feed in Table 1 (ΐ3.7 weight by weight with the solids formed during the process (2.7% by weight), it can be seen that the combination of controlled conditions and catalyst produces a ratio by ASTM & D453. The lower amount of coke shown. Non-condensable hydrocarbons include C2, C3 and C4 hydrocarbons. From the sum of the weight percentages of C2 hydrocarbons listed in Table 2 (20.5 grams), the total smoke per gram can be calculated. The C2 hydrocarbons of the hydrocarbon gas in the same kind of ethylene s contain 0.0073 grams of ethylene per gram of total c2 hydrocarbons. From the sum of the weight percentages of c3 hydrocarbons listed in Table 2 (23 · 9), it can be calculated ^ " " The propylene content per gram of total C3 hydrocarbons. The non-condensable hydrocarbon c3 hydrazones contain 0.21 grams of propylene per gram of total and c3 hydrocarbons. The non-condensable hydrocarbon c4 hydrazones have 0.2 isobutylene. The weight ratio of alkane to n-butane. This example demonstrates a recipe for the preparation of a crude oil product containing the following, at least G.GG1 grams of boiling range distribution at the purchase of G1G1 up to 204 C (400 F) Hydrocarbons, at least 100,000 grams of hydrocarbons with a boiling range at 0.001 MPa, knife cloths between 204 c and 300 0C, at least 0.001 grams at .101 MPa / Teng range is distributed between 3⑻.c and 。.c. Smoke and hydrocarbons up to 0.ool gram boiling range at 0101 MPa hydrocarbons distributed between weight 0c and 200530389 538. Sichuan, Gang F) class. The range of radon is in the range of 204 ° c. The hydrocarbons include hetero-bond hydrocarbons and normal-bond hydrocarbons, and the ratio of such hetero-bond normal-chain force element hydrocarbons is at most 1.4. Oil products include with light oil, kerosene, diesel ... g0 = knife cloth. The crude oil product contains at least 0. gram light oil, and the light oil portion has a dazzling value of up to 0. The crude oil production: Daoyao has a benzene content of up to 0.001 g of benzene in light oil. The light oil portion of the product is per silk, and the light oil portion containing up to y oil product is per filament. Kashihara Aromatic compounds. Mother Kefu has at least. Gram of single-ring ring kerosene :::: two substances contain at least _ gram of kerosene. The crude product fraction contains aromatic compounds, while two. The kerosene portion of the crude product has a kerosene fraction of at least 0 3 η and an aromatic compound content per gram of the gram-gram compound. The kerosene part of the Xibian is a compound produced from coal to crude oil. There are up to · 2 grams of monocyclic ring aromatic σ hai crude oil products containing at least diesel oil components containing aromatic 1 into: not 01 grams of diesel. The crude oil product has at least 04 fragrance per gram of diesel oil, and the diesel compound of the crude oil product has an aromatic compound content of square compounds. It is less than 0.5 gm and the VG has an aromatic content of 2 to 2 g of the known compound per gram. The media was prepared as follows: we_g iron oxide and 173 91 200530389 423 g deionized water were combined to form a wet paste. The thirsty paste was treated as described in Example 1 g of potassium carbonate and described above to form intermediate solids. The intermediate solids were passed through a 40-mesh sieve with minimal force. Physical solids and elemental sulfur were mixed in a dry box with an argon atmosphere for hydrocarbon dilution. The intermediate solid was placed in a sealed carbon steel cylinder and heated to 400. In contrast to Example 2, the agent was mixed without powder. Like element sulfur mix,

And maintained at 400 C! hour. The vulcanization catalyst is reacted from carbon steel back to A as a solid. The potassium-iron sulfide catalyst is pulverized into powder using a sintered mortar and a pestle, so that the obtained catalyst powder can pass through a 40-mesh screen. The obtained potassium iron sulfide catalyst was analyzed using X-ray diffraction technology. From the analysis of the X-ray diffraction pattern, it was determined that the catalyst contains pyrite (ring), iron sulfide (FeS), and pyrrhotite (Fei xS). The m-ray diffraction technique did not detect mixed potassium-iron sulfide or iron oxide species. The sulfide contact device, the crude oil feed and reaction steps are the same as in Example 2, but the ratio of hydrogen to crude oil feed is

16,000 NmW (100, _ SCFB). A K_Fe sulfide catalyst (75.0 g) prepared as described in Example 3 was charged into the reactor. The properties of the crude oil product produced by this method are summarized in Table Workers in Fig. 8 and Table 3 in Fig. 10. The weight percentage of VG0 produced in Example 4 is greater than the weight percentage of VG0 produced in Example 2. Example 4 The weight percentage of the distillate obtained was made smaller than the weight percentage of the distillate obtained in Example 2. The Aρ specific gravity of the crude oil product prepared in Example 4 t was lower than the Aρ specific gravity of the crude oil product prepared in Example 2. A higher 92 200530389 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, it can be seen that the transition metal sulfide catalyst, after being in the presence of crude oil feed and hydrogen, is the reaction of taking 3 mg of sample in the TAP system including the gas medium and individual inorganic salts in all TAP tests 5 () per minute. Rates increase from € to room temperature

The water and carbon dioxide systems up to 500 C # were monitored using the system's mass spectrometer. -The catalyst on the carrier side and the oxide surface at 36% shows that the carbon dioxide discharged from the inorganic salt catalyst has a characteristic of greater than 0.2 volts and the discharged water has a current turning point of 01 volts. The minimum one goes to 360 C , As measured by 10 g of ion current and 10 vs. temperature, the j-catalyst exhaust gas separation curve ⑹ > m is the water and ⑺ from the inorganic salt catalyst discharge

The log 10 value of the stream. Exhaust from this inorganic salt catalyst 2: The turning point appears at 360 ° c. The sharpness of 7 σ 〇2 and K2C03 / Rb2C03 / Cs2C03 catalyst phase are at 360. (: Turning point for discharged water and dioxopotassium carbonate and carbonic acid shavings. Both have unpredictable electricity. For K2C03 / Rb2C〇3 / Cs2C〇 quality increase is confirmed by: two or more Different inorganic materials can be more disordered than individual pure carbonates. Nasal inorganic salts can be contacted. 93 200530389 1 Examples of honey catalysts and DSCs of different inorganic compounds. ^ In all DSC tests A 10 mg sample was heated to 520 at a rate of 10σ (:) per minute (:, cooled from 5200c to 0,0 C 'at a rate of 100c per minute and then used differential scanning calorimetry Meter (DSC) Model DSC-7 (manufactured by Perkin-Elmer (Norwalk, Connecticut, USA)) was heated from 00c to 6000c at a rate of 10.0C per minute. During the second heating of the sample, Catalyst DSC analysis showed that the salt mixture exhibited a wide thermal transition between 219 and 26 °. The midpoint of this temperature range was 250 oc. The area under the thermal transition curve was calculated as U5 Joules / Gram. Crystal disorder was first measured at 2 1 9. (: The minimum DSC temperature starts. These two results are opposite, for No clear thermal transition was observed with the acid. DSC analysis of a mixture of Li2C03, Na2c03, and ... during the second heating cycle ... Ll2C (VNa2C (VNa2C (VK2CQ3 mixtures show at 390 C to 400 ° A sharp thermal transition between c. The temperature in the spoon is 385 C. The area under the thermal transition curve is calculated to be -82,6 ears / gram. The onset of migration is determined at 39 °. The minimum DSc temperature begins. A sharp thermal transition indicates a substantially homogeneous salt mixture. 7 · or individual inorganic salts relative to 1 嫠 子 UiM test. All test systems are carried out as follows: · 3.81 cm (1.5 inches) of inorganic The salt catalyst or individual inorganic salt is placed in a muffle furnace (painted)-a quartz container equipped with upper or copper wires separated from each other but immersed in the sample. These metal wires are connected to a 9.55 volt Dry electricity 94 200530389 cell and a 220,000 ohm current-limiting resistor. The muffle furnace was heated to 600 ° C and the current was measured using a micro-ampere meter. Figure 12 shows the sample resistance versus carbonic acid unloading resistance ("i〇 ( rK2c〇3) ,,) plot of temperature ("T") log Illustrated curve 172,174, n6, 178 and 180, respectively k2C03 resistance, CaO resistance, K2C03 / Rb2C03 / Cs2C03 catalyst resistance,

The plot of Li2C03 / K2C03 / Rb2C03 / Cs2C03 catalyst resistance and Na2C03 / K2C03 / Rb2C03 / Cs2C03 catalyst resistance.

CaO (curve 174) is at 380-500. (: At a temperature in the range of _ exhibits a relatively large stable resistance (curve 1 72) relative to κ / Ο3. A stable resistance indicates an ordered structure and / or ions that do not tend to separate from each other during heating K2C03 / Rb2C03 / Cs2C03 catalysts, Li2C03 / K2C03 / Rb2C03 / Cs2C03 catalysts and Na2C03 / K2C03 / Rb2C03 / Cs2C03 angle sintering media (see curves 176, 178, and 180) in the temperature range of 350-500 ° C The following shows a sharp decrease in resistivity relative to k2co3. A decrease in resistivity usually indicates that a current is measured during the application of a voltage to a metal wire embedded in an inorganic salt catalyst. The data in Figure 12 confirms that At temperatures in the range of 600 ° C, inorganic salt catalysts are usually more mobile than pure inorganic salts. Figure 13 shows Na2C〇3 / K2C〇3 / Rb2c〇3 / Cs2c〇3 catalyst resistance relative to k2co3 resistance ( "IOg (r K2co3) ,,) a graph of 10g of temperature (" τ ,,). Curve 182 is the Na2C03 / during Na2C03 / K2C03 / Rb2C03 / Cs2C03 catalyst heating Effect of ratio of K2C03 / Rb2C03 / Cs2C03 catalyst resistance to κ / Ο3 resistance (curve 172) on temperature Figure. After adding 95 200530389 heat, 'the Na2C03 / K2C03 / Rb2C03 / Cs2C03 catalyst was cooled to room temperature, and then heated in a conductive device. Curve 184 is after cooling from 600 QC to 25. (: After, in Na2C03 / K2C03 / Rb2C03 / Cs2C03 During heating of the catalyst, the inorganic salt catalyst resistance is plotted against K2C03 resistance versus temperature log. The ionic conductivity of the reheated Na2C03 / K2C03 / Rb2C03 / Cs2C03 catalyst is relative to the original Na2C〇3 The ionic conductivity of the / K2C〇3 / Rb2C03 / Cs2C03 catalyst is increased. K 4 The difference between the ionic conductivity of the inorganic salt catalyst during the first heating and the second heating, it can be inferred that the inorganic salt catalyst is cooled when it is cooled. Form different shapes _ resentment (second form), which is different from the form before any heating (first form). The flowability of the salt catalyst is suitable for salting and pickling. All ^ cm thick powdery K / The catalyst cvRb ^ h / ChCO3 was placed in a quartz plate. The plate was placed in an oven and heated to 500 ° c for i hours. To measure the flow properties of the catalyst, the plate was manually placed in an oven after heating. Tilt. Λ K2C03 / Rb2C03 / Cs2C03 catalyst does not flow. When used When the spoon pressurized, the catalyst having a consistency of taffy. _ End Conversely, the individual carbonate is a free-flowing powder under the same conditions. Under the same conditions, the catalyst becomes liquid in the pan and is prone to purge (for example, similar to water). The equipment and general steps are used in Example 9-27—except for the case where the variables are explained. 96 200530389 material 576 reaction two 25. ❻mL C ^ autoclave (P-M-) " 0 CT is rated at 35MPa operating pressure (500 psi), equipped with a mechanical wiper Jσ ^ to 625 〇c + 5. Yihe located can enable the genus The heater is maintained at ambient temperature *, ~ 800 watts Gaumer F-type heater, gas A 〇μ on the EUrotherm controller of ~ C ... but m ^, inlet, 瘵 inlet, one outlet and thermocouple to ^ ⑴ ^ The upper part is separated by a glass cloth. —Adding container: The adding container (250 ml, 316 stainless steel Hoke) is equipped with a controlled heating system, appropriate gas control, and constant force. Lifting device, thermocouple, dynamometer and high temperature control valve (㈣⑽ e # SS 4UW) 'can adjust hot, viscous and / or compressed crude oil feed at a flow rate of 0-500 g / min. After the feed is filled to this addition vessel, an outlet side of the high temperature control valve is connected to the first inlet of the reactor. Before use, the line of the addition vessel is isolated. Product collection · Reactor vapor from the reactor outlet Leaving and being sent to a series of decreasing temperature cold traps (connected to a series 150 ml, 316 stainless steel Hawk container immersion tube). The liquid from the vapor is reduced in the cold trap to form a gas stream and a liquid condensate stream. If necessary, use a back pressure regulating valve to adjust the pressure from the reactor and the The flow rate of the vapor in the cold trap. The flow rate and total gas volume of the air stream leaving the cold trap were measured using a wet test meter (Ritter Model # TG 05 Wet Test Meter). After leaving the wet flow meter, the The gas stream is collected in an air bag (a Tedlar gas sampling bag) for analysis. GC / MS (Hewlett-Packard Model 5890, now Agilent Model 5890; Agilent Technologies, Zion 97 200530389

Illinois, manufactured by U.S.A.). The liquid condensate stream is removed from the cold trap and weighed. The crude product and water are separated from the liquid condensate stream. The crude product is weighed and analyzed. Procedure: Fill Cerro Negro (137.5 g) into the addition container. The crude feed has an API specific gravity of 6.7. The crude oil feed had a sulfur content of 0.042 grams per gram of crude feed, a nitrogen content of 0.011 grams, and a total Ni / V content of 0.99 grams. The crude feed was heated to. [. Fill the reactor with K2C03 / Rb2C03 / Cs2C03 catalyst (3 1.39 g). The K2C03 / Rb2C03 / CS2COs catalyst system was prepared as follows: 16.44 g of K2C03, 19.44 g of Rb2C03 and 24.49 g of Cs2c03 were combined. The K2C03 / Rb2C03 / Cs2C03 catalyst has a minimum TAP temperature of 360 ° C. The K2C03 / Rb2C03 / Cs2C03 catalyst has a DSC temperature of 250 0C. Individual salts (K2C03, Rb2C03 and Cs2C03) did not exhibit DSC temperatures in the range of 50-50 ° C. The TAP temperature is higher than the DSC temperature of the inorganic salt catalyst and lower than the dsc temperature of individual metal carbonates. The catalyst is rapidly heated to 450 at a normal pressure flow of 250 cm 3 / min methane. (:. After reaching the desired reaction temperature, steam was metered into the reactor at a rate of 0.4 milliliters / knife and methane at a rate of 250 cm'min. After the crude oil feed was added to the reactor The steam and formazan were continuously metered during the period of 2.6 hours. The crude oil feed was pressurized into the reactor using 15 Mpa (229 psi)% for 16 minutes. After the addition of the crude oil feed was completed, the remaining crude oil was fed. The feed (0.56 g) was left in the addition vessel. A decrease in temperature to 370 was observed during this crude oil feed addition. The catalyst / crude oil feed mixture was heated to a reaction temperature of 4500 and maintained at that temperature. Hours. After two hours, the reactor was cooled and the resulting slag / catalyst mixture was weighed to determine the percentage of coke produced and / or not consumed in the reaction. From the initial catalyst weight to the coke / catalyst mixture The difference in weight indicates that 0.046 grams of coke remained in the mother gram crude feed. The complete product contained 0.87 grams of crude oil products and gas with an average API specific gravity of 13. The gas contained unreacted CH4, hydrogen, and C. : 2 and C4-C6 hydrocarbons And C02 (0.08 grams of CO2 per gram of gas). This crude oil product contains 0.01 grams of sulfur and _ 0.000005 grams of culprit and v per gram of crude oil product. The crude oil product was not further analyzed. In Example 10 The reaction steps, conditions, crude oil feed and catalyst system are the same as in Example 9_. The crude oil product of Example 丨 was analyzed to determine the boiling range distribution of the crude oil product. The crude oil product contained per gram of crude oil product. 0.14 grams of light oil, 0.19 grams of distillate, 0.45 grams of vg0 and 0.001 grams of residue content, and undetectable amounts of coke. Examples 9 and 10 demonstrate crude oil feed and hydrogen Contact of the source in the presence of 100 grams of crude oil feed to 3 grams of catalyst in the presence of a catalyst to produce a complete product containing crude oil products that are liquid blends at sTp. The crude oil product has at most the crude oil feed A residue content of 30% of the residue content. The crude oil product has a sulfur content and a total Ni / V content of at most 90% of the crude feed sulfur content and Ni / V content. The crude oil product contains at least 0.001 g The boiling range distribution is at most 200 at 001 MPa. At least GG〇1 grams of hydrocarbons whose boiling range is distributed between fine-classes under 〇1G1, at least gram 99 200530389 at 0.101 MPa boiling range is distributed between 400-53 8 0C (1000) Hydrocarbons.

1 Example ~ LIrl2: Contact of crude oil feed with hydrogen source in the presence of K ^ CCVRbK) J disc media and steam> Flying reaction steps and conditions in Examples 11 and 12 and K2C03 / Rb2C03 / Cs2C03 contact The media was the same as in Example 9 but using 130 grams of crude oil feed (Cerro Negro) and 60 grams of K2CO3 / Rb2CO3 / CS2CO3 catalyst. In Example 11, formic acid 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 188 _ represent the weight% of coke produced, strips 190 and 192 represent the weight% of liquid hydrocarbons produced, and strips 194 and 196 represent the weight% of produced gas. The weight of the crude feed is based. In Example 11, 93% by weight of crude oil product (strip 92), 3% by weight of gas (strip 196), and 4% by weight of coke (strip 188) were prepared, which was based on Cerro Negro Based on weight. In Example 12, 84% by weight of crude oil product (strip 190), 7% by weight of gas (strip 194), and 9% by weight of coke (strip 186) were prepared. # This is Cerro Negro's Weight as a basis. Examples 11 and 12 provide a comparison using methane as a hydrogen source and using hydrogen as a hydrogen source. Formazan is generally cheaper to manufacture and / or transport than hydrogen, so using formazan is ideal. As proven, when contacting crude oil feeds in the presence of natural salt catalysts to make the final order < 70 King House, methane can be at least as effective a source of tritium as hydrogen. Specific gravity shoulder oil 100 200530389 The device, reaction steps, and inorganic salt catalyst are the same as those described in Example 9 except that the reactor pressure is changed. psi) Example 13 The reactor pressure during the contact was oj MPa (14.7 ℃). The crude product was produced at 15.50 ℃ with a specific gravity of ApI of 25. The complete product had a carbon number distribution of 5 5 2 1 m M ^ hydrocarbons in the range of 5 to 32 (see curve 198 in Fig. 15). In Example 14, the reactor pressure during contact was 3.4 MPa (514.7 psi). When 1550 ° C was obtained Crude oil with a specific gravity of 516

Thing. The complete product has hydrocarbons with carbon numbers ranging from 5 to 15 (see curve 200 in Figure 15). These examples demonstrate a method of contacting a crude oil feed with hydrogen at different pressures in the presence of an inorganic salt catalyst to produce a crude product having a selected specific gravity of # Αρι. By changing the pressure ', a crude oil product having a higher or lower api specific gravity is produced. Under Contact :: 眚 施:

/ A ', the crude oil feed and reaction steps are the same as the phase 1 1 in Example 9 " the crude oil feed and the catalyst (or carbonized carbide) are directly charged into the reaction at the same time, so that Xiao oxide stone (C02) As a carrier gas. In the examples! In 5, the 138 grams of Cerro Negro plate 60 4 ancient γ g ”60 4 grams of K2C03 / Rb2C03 / Cs2C03 catalyst (the same catalyst as in Example 9 with 1 person widely used U) were combined. In Example 16 13: Gram Cerro Negro Plate 83 13 * z Shan λ / ί, Team 13 Gram Stone Anionized Silica (40 mesh, Stanf0rc

Materials; Alis Vi CA)). It is believed that this silicon carbide has, under the conditions of the method described in this article, (with the right) the low catalyst properties. 101 200530389 In each sample, the mixture was heated to a reaction temperature of 500 during the period of 2 ", Sunday, and J &. C02 was metered into the reactor at a rate of 100 MPa / min. Using a back pressure of 3.2 MPa (479 7 ης · η Μ PS!), The steam generated from the reactor was collected in a cold trap and an air bag. #… ^ Consolidate and analyze the crude oil product from the cold trap. In Example 1, 5, from Xi; 5, i, and ^ ^ crude oil feed with inorganic salt catalyst under a dioxy 4 carbon atmosphere The contact ratio was 36.82 grams (Brown I 26.68 weight%, based on the weight of the crude oil feedstock) API ratio will be ^ ^ Dong Zhixi 50 colorless hydrocarbon liquid.

In Example 16, from reading: § ,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,,, t The, The contact of the crude oil feedstock and silicon carbide under carbon dioxide |罝%, based on the weight of the crude oil feed 彳）) yellow hydrocarbon liquid with API specific gravity of 12. Although "e, the yield in Example 15 is low, the on-site production of hydrogen source in the presence of inorganic salt catalyst is greater than the on-site production of hydrogen in the absence of catalyst. The crude product yield in Example 16 is One of the crude product yields in Example 5! Example 2 also confirmed that hydrogen was generated during the contact of the crude feed in the presence of inorganic salts and in the absence of a gaseous hydrogen source.

Example 17-20: £ ^ £ ^ 3_ The number of pupae, plutonium oxide, and the stubby beetle device, reaction steps, crude oil feed and inorganic salt catalyst system carbonized at atmospheric pressure are the same as in Example 9, However, Cerro Negro was added directly to the reactor instead of via the addition volume, and hydrogen was used as the hydrogen source. The reactor pressure during the contact was 0.101 MPa (14.7 psi). The gas flow rate is 250 cm 3 / min. Tables showing the reaction temperature, steam flow rate, and percentages of crude product, gas, and coke produced are shown in Table 4 of Figure 16. 102 200530389 In Examples 17 and 18, the K2C03 / Rb2C03 / Cs2C03 catalyst was used. In Example 17, the contact temperature was 375 ° C. In Example 18, the contact temperature was within a temperature range of 500-600 ° C. As shown in Table 4 (Fig. 16), for Examples 17 and 18, when the temperature was from 375. (: Increased to 500. ^, gas production increased from 0.02 grams per gram of complete product to 0.05 grams of gas. However, coke production decreased at higher temperatures from 0.17 grams per gram of crude feed to 0.99 grams At the higher temperature, the sulfur content of the crude oil product also decreased from 0.01 g per gram of crude oil product to 0.08 g of sulfur. Both crude oil products had a η / of 18. In Example 19 In the crude oil feed, CaCO3 was contacted under conditions similar to those described in Example 18. The series of percentages of crude oil product, gas, and coke production are shown in Table 4 of Figure 16. The gas production is relative in Example 19 The gas production in Example 18 is increased. The desulfurization effect of the crude oil feed is not as effective as in Example 18. Compared to the crude oil product produced in Example 18 per gram of crude oil product, the Sulfur content of 8 grams. The crude oil product produced in Bex Example 19 contains 0.01 grams of sulfur per gram of crude oil product. Example 20 is a comparative example to Example 18. In Example 20 , 83 · 13 grams of silicon carbide instead of inorganic salt catalyst The gas production and coke production in the yoke example 20 were increased relative to those in Example 18, and the volume production and coke production were increased. Under these catalyst-free conditions, 0.22 g per gram of crude oil product was produced. Coke, 0.25 g of non-condensable gas and 0-5 g of crude oil product. Compared to 0.01 g of sulfur per gram of crude oil product produced in Example 8, the crude oil produced in Example 20 The product is 0.036 grams of sulfur per gram of the original 103 200530389 oil product. These examples demonstrate that the catalysts used in the examples and 18 are catalyst-free conditions and conventional metal salts. The result. At 500 »250 cm 3 / min hydrogen flow rate 隹 Γ" the amount of gas that is generated in the absence of catalyst is significantly lower than that in catalyst-free conditions ", which is less The amount of scorching and non-condensable gas. In the example using the inorganic salt catalyst (see Table 16 · yoke example Π] ", compared to the control experiment (such as in Table 4 of Figure 16: Example 20) # The gas formed during the month is the weight of the gas produced. From the amount of smoke in the gas produced, the crude oil is estimated. The feed heat solution is up to 20% by weight, up to 15% 0 / t Wang Xi 15% by weight, up to 10% by weight 2. 5% by weight or none, based on the total amount of crude oil in contact with the hydrogen source is The gaseous plutonium source, 氽 t, and the following piles were deposited in the same embodiment, 21, and 22 as in Example 9, but using hydrogen as the hydrogen source. In Example 21, 130.4 g of CerrONegr ^ 8 grams of K: 2C03 / Rb2C03 / CS2C03 catalysts were combined to form a crude oil feed mixture. In Example 22, 139.6 grams of ^^ 〇 仏 ^ 〇 and 8014 grams of slave fossils were combined to form a crude oil feed mixture. The raw / from feed mixture was charged directly into the reactor. Hydrogen was metered into the reactor at 250 cm 3 / min during the heating and holding period. The crude feed mixture was heated to 300 over 15 hours / month. And maintained at. His Majesty 1 J, Sun $. The reaction temperature was increased to 400 QC during 1 hour and maintained at 400 O p for 1 hour. After the reaction temperature reached 400 ° C, water was fed into the reactor at a rate of 0.4 g / 104 200530389 minutes and combined with chlorine gas. Water and gas were metered to the reaction. To maintain heating and dwell time. After maintaining the reaction mixture at OC, the reaction temperature was increased to 5000C and maintained at $ 100C. . Under 2 hours. The vapour generated from the reactor was collected in cold packs and air bags. In the future, liquid products from the cold trap will be consolidated and analyzed. ^ In Example 21, 86.17 g (6 "wt%, based on the weight of crude oil feed) I red-brown hydrocarbon liquid 胄 (crude product" drool (97.5g)) The contact of the Cs / h catalyst under a hydrogen atmosphere is generated as steam. In Example 22, water vapor and a small amount of gas were generated from the reactor. The reactor was inspected, and a dark brown viscous hydrocarbon liquid was taken out from the reactor. From crude oil Contact of the feed with silicon carbide under a hydrogen atmosphere produced a dark brown, viscous hydrocarbon liquid of less than 50% by weight. Compared to the yield of the crude product produced in Example 22, a crude product was observed in Example 21 Yield increased by 25%. Example 21 demonstrates the improvement in the properties of the crude oil product produced using the method described herein relative to the crude oil product produced using hot water. Specifically, the crude product ratio in Example 21 is derived from the Example The crude oil product of 22 is low, as demonstrated by the fact that the crude oil product produced in Example 22 cannot be produced with steam. Compared with the crude oil product produced in Example 22, the crude oil product produced in Example 21 Crude products have enhanced Flow properties, as determined by visual inspection. ΊΑΜ_24: The contact between the crude oil feed and the hydrogen source at-one by one, _.m below, to create a phase comparable to 无 无 媪 媪 格 # 渔 渔 义 ^ rhyme volume has increased Volume of crude oil product. Device, 105 200530389 Crude oil feed, inorganic catalyst and reaction steps are the same as described in Example 9, but the crude oil feed is directly charged to the reactor and hydrogen is used as the gas source. Crude oil feed (Cerro Negro) has an API specific gravity of 6.7 and a density of 1.02 g / ml at 2.55. In Example 23, 102 g of crude oil was fed (100 liters of crude oil feed) and 31 g The K2C03 / Rb2C03 / Cs2C03 catalyst was charged into the anti-cracker. A crude product (87 · 6 g) with an API specific gravity of 50 and a density of 5 · 5 · 0 · 6976 g (112 ml) was prepared.

In Example 24, 102 g of a crude oil feed (100 ml of a crude oil feed) and 80 g of silicon carbide were charged into a reactor. A crude product (70 g) of 0.961 g / ml (70 ml) at a specific gravity of 12 and a density of 15.5 was prepared. Under these conditions, the volume of the crude product produced from Example 23 was approximately 6% greater than the volume of the crude feed. The volume of the crude oil produced in Example 24 is significantly smaller than (40% less) 纟 The crude oil produced in Example 23

The volume of the product. The significant increase in product volume increases the ability of the producer to produce more volume of crude oil product per volume of crude oil input. 25, ~ ^ J ^^ L ^ A ^ -K2C〇1 / Rb1C〇1 / Cs1CQ hydrogen medium, sulfur, and coke · The device and reaction steps are the same as described in Example 9 ', but the steam is used at 300 cm 3 / The K2C03 / Rb2C03 / Cs2C03 catalyst was metered into the reactor by combining 27.2 g of K2C03, 32 · g of RbWO3 and 40.6 g of CS2C03. Crude oil feed (130 · 35 g) medium (31. 6 g) was charged into the reactor and K2C03 / Rb2C03 / Cs2C03 was contacted. Cerro Negro crude oil was 106 per gram of original. 200530389 The oil feed contained a boiling range of 0.04 g Total aromatics content distributed between 149.2600c (3.500), 0.00064 grams of combined nickel and vanadium, 0.042 grams of sulfur and 0.56 grams of residue. This crude feed had an Aρ specific gravity of 6.7. The contact of this crude oil feed with methane in the presence of K ^ CC ^ RhCOyChCh catalyst, on a gram crude feed basis, produced 0.95 grams of complete product and 0_041 grams of coke. The whole product product contains 0.99 grams of crude oil product and 0.028 grams of hydrocarbon gas per gram of complete product. The total gas system collected contains 0 mol of hydrogen per mol of gas, 0.045 mol of carbon dioxide, and 025 mol of q and broad C6 hydrocarbons, as determined by GC / MS. The remainder of the gas is the product of pinane, air, carbon monoxide, and traces (0.004 mol) of evaporated crude oil. The crude product was analyzed using a combination of gas chromatography and mass spectrometry. Crude oil products contain hydrocarbon mixtures with boiling ranges between 100-538. The total liquid product mixture was 0 g of ethylbenzene per gram of mixture (a monocyclic cyclic compound with a boiling point of 136.2 at 0.1101 MPa). This product was not detected in the crude oil feed. The used catalyst ("first used catalyst,") was removed from the reactor, weighed, and analyzed. The weight of the first used catalyst was increased from 3 to 6 grams to 3 7.38 grams. Total weight (based on the weight of the original K2C03 / Rb2C03 / CS2C03 catalyst, an increase of 18% by weight). The first used catalyst system contains 0.15g per gram of used catalyst Of additional coke, 0.0035 grams of sulfur, 0.0014 grams of Ni / V, and 0.845 grams of K2C03 / Rb2C03 / Cs2C03. Make additional crude feed (152.71 grams) with the first used catalyst 107 200530389 (36.63 grams) was contacted to make i50 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 additional coke, and 0.7 grams The gas system contains 0.18 moles of hydrogen, 0.07 grams of carbon dioxide and 035 moles of C2-C0 hydrocarbons per mole of gas. The remainder of the gas is methane, nitrogen, some air and traces Of evaporated petroleum products (< 1% mole). This crude product contains hydrocarbons with a boiling range of 100-538. (: Mixture. Part of the mixture whose boiling range is below 149 ° C is 0.018 mole% ethylbenzene, 0.004 mole% xylene, 0.03 mole% m-xylene, and 0.03 mole% m-xylene per mole of total liquid hydrocarbons. 〇〇〇〇〇〇〇〇〇 ％ Mole% of p-xylene (monocyclic cyclic compounds with a boiling point below 149 ° C at 0. 101 MPa). These products are not detectable in this crude oil feed. Will be used Catalyst ("second used catalyst") was removed from the reactor, weighed, and analyzed. The weight of the second used catalyst increased from 36.63 grams to a total weight of 45.44 grams (based on the original K2C〇3 / Rb2C (based on the weight of VCs2C03 catalyst, an increase of 43% by weight). The second used catalyst system contains 0.32 g of coke and 0.03 per gram of the second used catalyst. 1 gram of sulfur and 〇67 grams. The additional crude feed (104 grams) was contacted with the second used catalyst (44 84 grams) to make a total of 〇04 grams per gram of crude oil feed. The product was collected and 0.14 g of coke was collected. Since 104_ 1 g of the 133 g crude oil feed transferred was a crude oil feed, a part of the coke was returned The coke produced in the addition container due to excessive heating of the addition container. The complete product is 0.86 grams of crude oil product and 108 200530389 0.025 grams of hydrocarbon gas per gram of complete product. The total gas system contains 0 per mole of gas. · 8 moles of hydrogen, 0.052 moles of carbon dioxide and 0.03 moles of c2-C6 hydrocarbons. The remainder of the gas is methane, air, carbon monoxide, hydrogen sulfide and a small amount of evaporated petroleum. The crude oil product Contains a hydrocarbon mixture with a boiling range between 100-538 cC. Futeng range is distributed in 14-9. The mixtures below C are per gram. · The mixture contains 0.021 grams of ethylbenzene, 0.027 grams of toluene, 0.042 grams of m-xylene, and 0.020 grams of para-xylene, as previously determined by GC / MS. By. The used catalyst ("third used catalyst,") was removed from the reactor, weighed, and analyzed. The weight of the third used catalyst was increased from 44.84 grams to a total weight of 56.59 grams (by The original media weight 1 was based on the increase of 79% by weight.) Detailed elemental analysis of the third used catalyst was performed. The third used catalyst contained 0.90 g of carbon per gram of additional material, and 〇 〇28 grams of rhenium, 000025 grams of oxygen, 〇46 grams of stone ash, 0.017 grams of nitrogen, 0.0018 grams of vanadium, 007 grams of nickel, 0.001

Grams of iron and G.GGG 25 grams of chloride ions, the rest are other transition metals such as chromium, titanium and zirconium. As demonstrated in this example, coke, sulfur and / or metals deposited on and / or in the inorganic salt catalyst do not affect the crude oil produced by the contact in the presence of the chlorine source inorganic salt catalyst in the crude oil feed tray. Total product yield (at least 80% per test). The crude oil product has a monocyclic aromatic compound content of up to 100 times the monocyclic aromatic compound content of the crude oil feed in the following boiling range distribution. 109 200530389-For the test, the average crude product yield (weight of crude oil feed = abundance) is 8 "% by weight 'standard deviation is 26%; average coke households; (27.5 weight s% (using crude oil feed The weight is based on the difference mm mm of the average weight% of dehydrocarbons (based on the weight of the crude oil feed), and the standard deviation is. ": The larger standard deviation of Γ and coke anorexia is due to the third test The middle feed controller is malfunctioning.

: Uniform two! Rb ′ Even the large amount of coke tested here has no significant and significant adverse effect on catalyst activity and washing activity. The ratio of olefins to total C ′ is 0 · 19 ^ 3. The ratio of women's tobacco to total q is 0.4. The ratio of α-olefins of c4 type to the dilute hydrocarbons in the molecule is 0.6! c The cis / anti-lean hydrocarbon ratio is 6.34. This ratio is considerably higher than the predicted 4 thermodynamic C4 cis / transolefin ratio. The ratio of alpha olefins to C5 hydrocarbons to intramolecular olefins is " 2. This ratio is greater than the predicted thermodynamics of 0194. 5 is the ratio of olefins to c5 olefins. The anti-olefin ratio is 125. This ratio is greater than the predicted thermodynamic 05 cis / transolefin ratio of 0.9.

The contact device and reaction steps of the crude oil cliff material and hydrogen source in the presence are the same as those described in Example 9 except that the crude oil feed, methane and steam A are continuously fed into the reactor. The content of the feed in the reactor was monitored using the reaction for changes in gravity. Methane gas was continuously placed in the reactor towel at 500 cm '. Steam was continuously metered into the reactor at 6 g / min. The inorganic salt catalyst was prepared by combining 27.2 grams of K2co3, 32.2 grams of Rb2CO3, and 40.6 grams of Cs2co3. The K2C〇3 110 200530389

Rb'CVCs'O3 touches a woman (π · 88g) and loads it into the reactor. θ A crude oil feed (asphalt, Romenster, Canada) with a specific gravity of 9.4 ㈤Αρι, 0.02 g of sulfur 3 in sulfur and 0.40 g of residue per gram of crude oil feed was heated to 15 in an addition vessel. 〇c. The hot bitumen was metered into the reactor at 10.5 g / min continuously from the added valley state in an attempt to maintain the crude oil feed level at the reactor volume; however, the rate was not sufficient to maintain the level. The pinane / Luo A / crude oil feed was contacted with the catalyst at an average internal reactor temperature of 456. A Yuan / steam / crude oil feed contacted with the catalyst to produce Lu Zhongyuan's whole product (in this example, it is in the form of steam flowing out of the reactor). A total of 640,000 grams of crude oil were processed during 6 days. Feed. From the initial catalyst weight; the difference between S and the weight of the residue / catalyst mixture, it is known that 0.08 5 grams of coke bore per gram of crude oil feed remains in the reactor. From the contact between crude oil feed and sintering in the presence of K ^ CCVRb / CVChCO3 catalyst, 0.93 g of complete product was obtained per gram of crude oil feed. This complete product is a product containing gram of gas and 0.97 grams of crude product per gram of complete product, excluding the amounts of pinane and water used in the reaction. The gas system contains 0.014 grams of hydrogen per gram of gas, 0.018 grams of nitric oxide, 0.08 grams of carbon dioxide, 013 grams of hydrogen sulfide, and 0.68 grams of non-condensing fluid. It is estimated that the amount of hydrogen sulfide produced by the crude oil is reduced by 18% by weight. As shown in this embodiment, hydrogen, carbon monoxide, and carbon dioxide are generated. The molar ratio of carbon monoxide to carbon dioxide is 0.4. The C2-C5 hydrocarbon series contains 0.30 g of the C2 compound, 0.332 111 200530389 g of the C3 compound, 0.26 g of the C4 compound, and 0.10 g of the C5 compound per gram of the hydrocarbon. The weight ratio of isopentane to n-pentane in non-condensing cigarettes was 0.3. The weight ratio of isobutane to n-butane in non-condensable hydrocarbons was 0189. The c4 compound has a butadiene content of gram per gram of the C4 compound. The weight ratio of α (: 4 olefin to intramolecular C: 4 dilute hydrocarbon is 0 75. The weight ratio of aC5 olefin to intramolecular c5 olefin is 1.08. The data in Example 25 confirms that a fairly high sulfur crude feed and Continuous processing of the same catalyst in the presence of coke has not weakened the activity of the inorganic salt catalyst and produced a crude oil product suitable for transportation. The crude oil feed and hydrogen source are called for in the presence of K, CO, / RtKrrK / rirn_ via the presence of Aig-coke The contact, device, and reaction steps were performed using the conditions described in Example 26. The K2C03 / Rb2c03 / Cs2c03 catalyst (56 · 5 g) was charged into the reactor. In 6 hours A total of 2550 grams of crude oil feed was processed during the period. From the difference between the weight of the initial catalyst and the weight of the residue / catalyst mixture, it is known that based on the weight of the crude oil feed, there is 0.14 g of coke per gram of crude oil feed. Remain in the reactor. Each gram of crude oil feed produced a total of 0.89 grams of whole product. This complete product is 0.04 grams of gas spring spear per gram of complete product. 0.96 grams of crude product is not included The amount of methane and water in the reaction ° The gas system contains 0.021 g per gram of gas , 0.018 g of nitric oxide, 0.052 g of carbon monoxide, 0.18 g of hydrogen sulfide and 0.65 g of non-condensable hydrocarbons. From the amount of hydrogen sulfide produced, crude oil can be estimated. The sulfur content of the feed is reduced by 14% by weight, which is based on the weight of the crude oil feed. As shown in this example, hydrogen, carbon monoxide and carbon dioxide are generated. Monooxygen 112 200530389 Moore of carbon dioxide to carbon dioxide The ratio is 0 · 6.

The CrC6 hydrocarbon series contains 0.44 g of the C2 compound, 0.31 g of the C3 compound, 0.19 g of the C4 compound, and 0068 g of the C compound per gram of CVC6 fe. The weight ratio of isopentane to n-pentane in the non-condensable hydrocarbons was 0.25. The weight ratio of isobutane to n-butane in the non-condensable hydrocarbons was 0.15. The C4 compound has a butadiene content of 0.003 g per C: 4 compound.

This example demonstrates that the repetitive processing of a fairly 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 made it suitable for transportation. Crude products. In view of this description, modifications and alternatives of the present invention in various aspects will be obvious 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 parts may replace those exemplified and illustrated herein, number of copies and procedures may be reversed, and certain features of the invention may be unique

After the use of "Li Ying" is explained in the present invention, all of them will be understood by those having ordinary knowledge in the technical field to which the present invention belongs. The elements described herein can be made and modified without departing from the spirit and scope of the present invention described in the scope of the following patent applications. [Brief description of the drawings] After using the above detailed description and referring to the attached drawings, the advantages of this volume will be more apparent to those with ordinary knowledge in the technical field of the present invention. 113 200530389 Figure 1 疋 Used to feed crude oil A schematic illustration of a specific example of a contact system that contacts a hydrogen source in the presence of one or more catalysts to make a complete product. Figure 2 is a schematic illustration 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 3 is a specific example of a separation zone combined with a contact system. Figure 4 is a specific example of a blend zone combined with a contact system. Figure 5 is a specific example of a separation zone, contact zone and blending zone. Figure 6 is a multiple Contact System Figure 7 is a schematic diagram of a specific example of an ion conductivity measurement system. Fig. 8 is a list of crude oil feedability f and crude oil product properties obtained from an example of contacting a crude oil feed with a transition metal sulfide catalyst.

Figure 9 is a list of crude oil feed composition and non-condensable hydrocarbon composition obtained by contacting a crude oil feed with a transition metal sulfide catalyst. It is a list of properties and compositions of crude oil products obtained from contacting crude oil feeds with transition metal sulfide catalysts ". Fig. 11 is a graph of the 'inorganic salt catalyst current vs. temperature' as measured by TAP. Graphical illustration. Out of the milk body ~ resistance pair = yes: for the carbonate salt of inorganic salt catalyst and inorganic salt: 対 / dish degree of the log 10 chart. Figure 13 is a graphical representation of the Na2C03 / K2C03 / Rb2 114 200530389 catalyst resistance versus temperature sound vs. potassium carbonate resistance. Fig. 14 is a graph showing the weight percentage of the hydrogen source produced by the specific examples of contacting the crude oil feed with inorganic salts from various materials such as 隹, Ί, Ί, stylized tobacco, and gases. Do not. The crude oil feed was brought into contact with the inorganic salt catalyst and the quotient " obtained from the crude oil product was smaller than the carbon number graph. Fig. 16 is a list of ingredients prepared from the examples of oyster bean shells that were brought into contact with crude oil.

Although the present invention is susceptible to various modifications and #generation forms, specific examples are shown in the examples below. The schema can be used to #L and will be drawn in detail in this article. It should be understood that the R β # description is not intended to limit the present invention to the particular forms disclosed: the formula and its ❹ The present invention is intended to cover… contrary to the equivalent and alternatives which fall within the spirit and scope of the present invention. All changes, #

[Symbol description of main components] 100 contact system 101 crude oil feed source 102 contact zone 104 conduit 106 circulation conduit 108 conduit 110 flow control valve 110 'flow control valve 112 gas inlet 115 200530389 114 steam inlet 116 separation zone 118 conduit 119 crude oil 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 container 158 samples

116 200530389 160 162 164 166 168-170 172-180 182-184 186-188 190-192 194-196 198-200 Power metal wire metal wire meter ion current vs. temperature plot resistance curve vs. temperature plot relative resistance curve Mapping of temperature% of coke produced% of liquid hydrocarbons produced% of gas produced% of carbon number distribution

117

Claims (1)

200530389 10. Scope of patent application: 1. A kind of crude oil product, each gram of crude oil product contains: 0.15 g of non-condensable hydrocarbon gas at 25 ° C and 0.11 MPa per day, / no injection of working gas Per gram of non-condensable hydrocarbon gas containing up to 3 grams of hydrocarbons having a carbon number of 1 to 3 (C 1 to C 3); to 0.0001 grams of light oil 'which has an octane number of at least 70; at least 〇_〇〇1 kerosene, the kerosene has at most _30. . Warm production; Spinning point, as determined by A q ΤΛ / ί, i »1 M method D2386, and the kerosene system contains at least 0.02 g ta β gram of compound per gram of kerosene, as in ASTM As determined by method D5 1 86; and up to 0.05 g of residuals, as determined by ASTM method 05307. 2. For example, the crude oil product of the patent application item ㈣i, wherein the crude oil product also contains at least 0.001 grams of diesel oil per gram of crude oil product, and the diesel fuel contains gram up to 100 grams of aromatics per gram of diesel oil. Compounds, of which aromatics; compounds are as determined by IP method 368/90. 3. If the scope of the patent application is No. 1 "2, the crude oil product, wherein the crude oil product also contains at least 0.001 g of VG0 per gram of crude oil product, and the 系 VGO series contains at least 0,03 g of VG0 per gram of crude oil product. Aromatic compounds, where = is a compound as determined by IP method 368/90. 4. If the scope of application for a patent is 帛 w, a crude oil product of any one of the above, the light oil contains at most _g of benzene per gram of light oil, as determined by AST "D 6 7 30. For example, the crude oil product of any one of the scope of application for patent (f), where the light oil and non-condensable hydrocarbon gas, when combined, include hetero-bonded smoke and normal chain 118 200530389 hydrocarbon burning, where the combined light oil and The weight ratio of condensed paraffinic hydrocarbons is at most isoparaffin to normal chain • 'and each gram is combined-the oil contains at most .15 grams of dilute hydrocarbons, of which the noncondensable hydrocarbon gas and light weight of chain two are based on ASTM * Measured by D673〇. The weight ratio of the working fluid and the olefin is 6. · As in the scope of the patent application .... The smoke with a carbon number of up to 3 in any two of the members contains a carbon number of 2 (C / crude oil product 'its hydrocarbons and chains. Alkanes, and the weight ratio of the combined c 2) and 3⑹ dilute alkanes is at most 03, and c ^ 4 is combined. 2 and 03: Tonight 0.3, hydrocarbon pair. Weight ratio of 2 chain hydrocarbons Evening and / or C3 olefin pairs. The weight ratio of the chain hydrocarbons is at most 03, wherein the weight ratio is as determined by the eight-lamp method D6730. Its 7. As stated in the scope of the patent, the crude oil product of any of the _Kj members in the crude oil product is 009-0.013 grams of atomic hydrogen per gram of crude oil product. The crude oil product of any one of the crude oil products has a weight ratio of atomic hydrogen to atomic carbon of at most 1.75. 9. A method of manufacturing transportation fuels, heating fuels, lubricants or chemicals, which comprises processing a crude oil product as described in any one of claims 1 to 8 of the patent application scope or a blend of the crude oil product and crude oil. 10. The method of claim 9 in the scope of the patent application, wherein the processing comprises distilling the crude product or the blend into one or more fractions. 1 1. The method of claim 9 or 10, wherein the processing includes steaming the crude product or the blend into one or more points. XI. Schematic: as next page 119