TW200533737A - Systems, methods, and catalysts for producing a crude product - Google Patents

Systems, methods, and catalysts for producing a crude product Download PDF

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Publication number
TW200533737A
TW200533737A TW093139056A TW93139056A TW200533737A TW 200533737 A TW200533737 A TW 200533737A TW 093139056 A TW093139056 A TW 093139056A TW 93139056 A TW93139056 A TW 93139056A TW 200533737 A TW200533737 A TW 200533737A
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TW
Taiwan
Prior art keywords
crude oil
catalyst
feed
product
content
Prior art date
Application number
TW093139056A
Other languages
Chinese (zh)
Inventor
Opinder Kishan Bhan
Scott Lee Wellington
Original Assignee
Shell Int Research
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Application filed by Shell Int Research filed Critical Shell Int Research
Publication of TW200533737A publication Critical patent/TW200533737A/en

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/20—Vanadium, niobium or tantalum
    • B01J23/22—Vanadium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/24—Chromium, molybdenum or tungsten
    • B01J23/28—Molybdenum
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
    • C10G29/04—Metals, or metals deposited on a carrier
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/64—Pore diameter
    • B01J35/647—2-50 nm
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/66—Pore distribution
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/0201—Impregnation
    • B01J37/0203—Impregnation the impregnation liquid containing organic compounds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P
    • C10G2300/203—Naphthenic acids, TAN
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/205—Metal content

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Catalysts (AREA)
  • Liquid Carbonaceous Fuels (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Lubricants (AREA)
  • Manufacture Of Alloys Or Alloy Compounds (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

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

Description

200533737 九、發明說明： 【發明所屬之技術領域】 本毛明大體上係有關處理原油進料之系統、方法和觸 媒二並且有關能使用這類系統、方法和觸媒生產的組成物。 更詳言之，本文中所述的特定具體實例係有關用以將原油 進料轉化成總產物之系統、方法和觸媒，纟巾此總產物含 有原油產物，其在25°C和〇.101 MPa下為液態混合物而且 與原油進料的個別性質相比具有一或多種已改變的性質。 【先前技術】200533737 IX. Description of the invention: [Technical field to which the invention belongs] Ben Maoming is generally related to systems, methods, and catalysts for processing crude oil feeds and to compositions that can be produced using such systems, methods, and catalysts. In more detail, the specific examples described herein relate to systems, methods, and catalysts for converting a crude oil feed to a total product. This total product contains a crude product, which is at 25 ° C and 0. It is a liquid mixture at 101 MPa and has one or more changed properties compared to the individual properties of the crude feed. [Prior art]

具有無法容許原油經濟地輸送，或使用f知設備加I 的一或多種不適當性質之原油通常稱為“劣質原油”。Crude oil that has one or more inappropriate properties that cannot allow crude oil to be transported economically, or using equipment plus I, is often referred to as "inferior crude oil."

劣質原油可能包含造成原油進料之總酸值C‘TAN”）^ 酸性成分。具有相當高TAN的劣質原油在輸送期間及/或 加工此劣質原油期間可能會造成金屬元件的腐敍。移除劣 質原油中的酸性成分可能涉及用各種驗化學中和酸性成 分。或者，耐蝕金屬可用於輸送設備及/或加工設備中。伯 用财姓金屬通常涉及可觀的費用，因此在現行設備中使用 耐蝕金屬可能不是吾人所期望的。抑制腐蝕的另—種方注 可能涉及在輸送及/或加工劣皙历、、山夕俞脏* b 〆 、 4貝原/由之則將腐蝕抑制劑添办 到劣質原油。使用腐蝕抑制劑可能對加工 ATw田所用的設伟 及/或由原油所製造之產物的品質有負面影響。 劣質原油通常包含相當大量的殘留物。 k頰大量殘 物會有使用習知設備難以輸送及/或加工 々战本昂貴的令 问。 5 200533737 〃劣質原油通常包含有機結合的雜原子(例如硫、氧，和 氮）。有機結合的雜原子於若干情況下對觸媒有不利的影 響。 劣質原油可能包含相當大量的金屬污染物，例如鎳、 飢，及/或鐵。在加工這類原油㈣，金屬污染物及/或金 屬污染物的化合物可能會沈積在觸媒表面上或觸媒的孔隙 體積中。這類沈積物可能會導致觸媒活性的下降。 在加工劣質原油期間焦炭可能會急劇地形成及/或沈積 在觸媒表面上。使受到焦炭污染的觸媒之催化活性再生的 能是昂貴的。再生期間所使用的高溫也可能使觸媒 的活性降低及/或導致觸媒劣化。 劣質原油可能包含有機酸金屬鹽形態的金屬(例如鈣、 ’甲及/或鈉）。有機酸金屬鹽形態的金屬典型而言無法 由自：方法’例如脫鹽及/或酸洗從劣質原油中分離。 :存在有機酸金屬鹽形態的金屬_，習知方法常遇到 與典型沈積在觸媒之外表面附近的鎳和釩相比，有 鹽形態的金屬可能會優先沈積在觸媒粒子間的孔 μ 別是在觸媒床的頂部。污㈣，例如有㈣ 床的==金屬沈積在觸媒床頂部通常會導致通過觸媒 金屬鹽形二 際上會堵塞該觸媒床。再者，有機酸 + /〜、金屬可能會導致觸媒的快速減活性。 每克包:有機氧化合物。加工具有含氧量為 借,^ 由中至少含〇.002克的氧之劣質原油的處理設 〇工期間可能會遇到問題。有機氧化合物在加工期間 200533737 又熱恰可此會生成高級氧化物（例如酮及/或由醇的氧化生 成酸，及/或由醚的氧化生成酸），其難以從處理過的原油 中移除及/或在加工期間可能會腐蝕/污染設備並且導致輸 送管線堵塞。 劣貝原/由可旎包含不飽和烴。當加工不飽和烴時，特 別疋如果會產生由裂解法而來的不飽和片段，則氫的均量 通常必須增加。加工期間的氫化，其典型而言涉及活性氳 化觸媒的使用，可能需要抑制不飽和片段形成焦炭。氣的 生產成本昂貴及/或輸送到處理設備成本昂貴。 ,名質原油在以習知設備加工期間也會傾向於表現出不 -疋性。原油不穩定性會有導致在加工期間成分相分離及， 或生成非理想副產物（例如硫化氫、水，和二氧化碳）的傾 向。 習知方法通常缺乏改變劣質原油之選定性質，而不會 顯著改變劣質原油之其他性質的能力。舉例而$，習知； 法通常缺乏顯著降低劣質原油中的TAN而同時僅以期望量 改變劣質原油中特定成分(例如硫或金屬污染物)之含量的 所 一…，ν π τ干’坪j艰刀口主 貝原油以降低造成不利性質之成分的重量百分率。然而 添加稀釋劑通常會因為稀釋劑的成本及/或加工劣質原油 加的成本而增加處理劣質屌油的杰太 貝屌，由的成本。稀釋劑添加至劣 原油於若干情況下可能會降低此種原油的穩定性。 頒予Sudhakar等人的美國專利案號6,547,957 ;頒 200533737 寺人的 6,277,269;頒予 Grande 等人的 M63 266; 頒予Bearden等人@ 5,928,5〇2 ;頒予細如等人的 5,914’〇3G;頒予—等人的5,897,769;頒予如⑽ 等人的5,871，636;及頒予Tanaka等人的5,85i，38i係㈣ 加工原油的各種方法、系統及觸媒。’然而，這些專利中所 述的方法、系統及觸媒因為以上提出的許多技術問題而具 有受限的適用性。 簡言之’劣質原油通常具有非理想性質(例如相當高的 tan，在處理期間變得不穩定的傾向，及/或在處理期間消 耗相當大量氫的傾向）。其他非理想性f包括相當大量的非 理想成分（例如殘留物、有機結合雜原子、金屬污染物、有 機酸金屬鹽形態之金屬’及/或有機氧化合物）。這類性質 會傾向於導致習知輸送及/或處理設備方面的問題，包括在 處理期間腐姓增加，觸媒壽命減短，製程堵塞，及/或氯使 用i曰加S)此，對於使劣質原油轉化成具有更多理想性質 之原油產物的改良系統、方法，及/或觸媒仍有顯著經濟上 和技術上的需求。同樣對於能改變劣質原油之選定性質而 只有選擇性改變劣質原油之其他性質的系、统、方法，及/或 觸媒也有顯著經濟上和技術上的需求。 【發明内容】 本I明大體上係有關用以將原油進料轉化成含有原油 產物而在右干具體實例中含有非可凝氣體的總產物之系 統、方法和觸媒。本發明大體上亦有關含有其中成分之新 穎組合的組成物。這類組成物能使用本文中所述的系統和 200533737 方法來獲得。 本發明係提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25°C和0.101 MPa下為液態混合物，該 原油進料具有至少〇·3的TAN，該至少一種觸媒具有中位 孔徑在90 A至1 80人之範圍内的孔徑分佈，該孔徑分佈中 至少60%的總孔數具有在45 A之中位孔徑範圍内的孔徑， 其中孔徑分佈係藉由ASTM法D4282測定；及控制接觸條 件以便使該原油產物具有TAN最多為9〇%之該原油進料的 TAN，其中TAN係藉由ASTM法D664測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25。(：和0·101 MPaT為液態混合物，該 原油進料具有至少〇·3的TAN，該至少一種觸媒具有中位 孔徑至少為90λ的孔徑分佈，其藉由aSTm法〇4282測定， 该觸媒在每克觸媒中，以鉬的重量計，含有〇 〇〇〇1克至〇 克的翻 或夕種錮化合物，或其混合物；及控制接觸條 件以便使該原油產物具有TAN最多為9〇%之該原油進料的 TAN，其中TAN係藉由ASTM法D664測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25。(：和0.101 MPa下為液態混合物，該 原油進料具有至少〇·3的TAN，其藉由ASTMD664測定， 該至少一種觸媒具有中位孔徑至少為18〇人的孔徑分佈， 200533737 其藉由ASTM法D4282測定，該觸媒具有包含週期表第6 欄的一或多種金屬，週期表第6攔之一或多種金屬的一或 多種化合物，或其混合物的孔徑分佈；及控制接觸條件以 便使該原油產物具有TAN最多為90%之該原油進料的 TAN ’其中TAN係藉由ASTM法D664測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25。(：和〇·1〇1 MPa下為液態混合物，該 原油進料具有至少〇·3的TAN，其藉由ASTM法D664測 疋，該至少一種觸媒包含：（a)週期表第6攔的一或多種 金屬，週期表第6欄之一或多種金屬的一或多種化合物， 或其混合物；及（b)週期表第1〇攔的一或多種金屬，週 期表第10欄之一或多種金屬的一或多種化合物，或其混 合物，其中第10欄金屬總量與第6攔金屬總量的莫耳比 在1至10的範圍内；及控制接觸條件以便使該原油產物 具有TAN最多為90%之該原油進料的TAN，其中TAN係 藉由ASTM法D664測定。 本發明亦提供生產原油產物之方法，其包括：使原油 2料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25t和0.101 MPa下為液態混合物，該 原/由進料具有至少〇·3的TAN’該一或多種觸媒包含：（a)第 種觸媒，其係於每克第一種觸媒中，以金屬重量計，含 :0.0001至0.06克之週期表第6欄的一或多種金屬，週 期表第6欄之—或多種金屬的一或多種化合物，或其混合 200533737 物；及⑻第二種觸媒’該第二種觸媒在每克 中，以金屬重量計，含有至少。 觸 ,.^ . s 見之週期表弟6攔的一 或多種金屬，週期表第6欄之-或多種金屬的-或多種化 合物，或其混合物；及控制接觸條件以便使該原 有最多^啊之該原油進料的⑽’其中了夢 由ASTM法D664測定。 精Inferior crude oil may contain the total acid value C'TAN ") ^ acidic component of the crude oil feed. Inferior crude oil with a relatively high TAN may cause metal components to rot during transportation and / or processing of this inferior crude oil. Remove The acidic component of inferior crude oil may involve neutralizing the acidic component with various chemical tests. Alternatively, the corrosion-resistant metal may be used in conveying equipment and / or processing equipment. The metal of the primary wealth usually involves considerable costs, so the use of corrosion resistance in existing equipment Metals may not be what we expect. Another way to suppress corrosion may involve transporting and / or processing inferior calendars, saplings * b 〆, 4 shellfish / by adding corrosion inhibitors to Poor quality crude oil. The use of corrosion inhibitors may have a negative impact on the quality of the products used in the processing of ATwfield and / or crude oil. Poor quality crude oil usually contains a considerable amount of residues. It is difficult to transport and / or process equipment that is known to be expensive and expensive. 5 200533737 737 Inferior crude oil often contains organically bound heteroatoms (such as sulfur, oxygen And nitrogen). Organically bound heteroatoms can adversely affect catalysts in a number of situations. Poor crude oil may contain a significant amount of metal contaminants such as nickel, zinc, and / or iron. In processing this type of crude oil, metals Contaminants and / or metal contaminant compounds may be deposited on the catalyst surface or in the catalyst's pore volume. Such deposits may cause a decrease in catalyst activity. Coke may form sharply during processing of inferior crude oil And / or deposited on the catalyst surface. The energy to regenerate the catalytic activity of the catalyst contaminated with coke is expensive. The high temperature used during regeneration may also reduce the catalyst's activity and / or cause the catalyst to deteriorate. Inferior Crude oils may contain metals in the form of metal salts of organic acids (such as calcium, formazan and / or sodium). Metals in the form of metal salts of organic acids typically cannot be separated from inferior crudes by: methods such as desalting and / or pickling : There are metals in the form of metal salts of organic acids. Conventional methods often encounter metals with salt forms compared to nickel and vanadium, which are typically deposited near the outer surface of the catalyst. Can be preferentially deposited in the holes between the catalyst particles, μ is not on the top of the catalyst bed. Fouling, such as ㈣ bed = = metal deposition on the top of the catalyst bed usually results in the catalyst metal salt-shaped second Will clog the catalyst bed. In addition, organic acids + / ~, metals may cause rapid deactivation of the catalyst. Per gram package: organic oxygen compounds. Processing has oxygen content to borrow, ^ contains at least 0. Problems may be encountered during the processing of 002 grams of inferior crude oil of oxygen. Organic oxygen compounds may be heated during the processing of 200533737, which may generate higher-level oxides (such as the oxidation of ketones and / or alcohols to alcohols, and (Or generate acid from oxidation of ether), which is difficult to remove from processed crude oil and / or may corrode / contaminate equipment during processing and cause blockage of pipelines. Inferior hydrocarbons / contains unsaturated hydrocarbons. When processing unsaturated hydrocarbons, the average amount of hydrogen must usually be increased, especially if unsaturated fragments are produced by the cracking method. Hydrogenation during processing, which typically involves the use of active tritiated catalysts, may require suppression of unsaturated fragments to form coke. Gas is expensive to produce and / or expensive to transfer to processing equipment. During the processing of well-known crude oil with conventional equipment, they will also tend to show non-stability. Crude instability has a tendency to cause component phase separation and / or generation of undesirable by-products (such as hydrogen sulfide, water, and carbon dioxide) during processing. Conventional methods often lack the ability to change selected properties of inferior crudes without significantly altering other properties of inferior crudes. For example, $, known; the method usually lacks a significant reduction in TAN in inferior crude oil while only changing the content of specific components (such as sulfur or metal contaminants) in inferior crude oil by the desired amount ..., ν π τ dry 'ping j Hard knife main shell crude oil in order to reduce the weight percentage of components causing adverse properties. However, the addition of diluent usually increases the cost of processing low-quality tartar oil because of the cost of diluent and / or the cost of processing inferior crude oil. Addition of diluents to inferior crude oils may reduce the stability of such crude oils under several circumstances. U.S. Patent Case No. 6,547,957 to Sudhakar et al .; 6,277,269 to 200533737 Temple; M63 266 to Grande et al .; to Bearden et al. @ 5,928,5〇2; 5,914 'to Xiru et al. 3G; 5,897,769 awarded to others; 5,871,636 awarded to Rugao et al .; 5,85i, 38i awarded to Tanaka et al. Various methods, systems, and catalysts for processing crude oil. ’However, the methods, systems, and catalysts described in these patents have limited applicability due to the many technical issues raised above. In short ', inferior crude oils often have non-ideal properties (e.g., a relatively high tan, a tendency to become unstable during processing, and / or a tendency to consume a substantial amount of hydrogen during processing). Other non-idealities include a considerable amount of non-ideal ingredients (e.g. residues, organically bound heteroatoms, metal contaminants, metals in the form of metal salts of organic acids' and / or organic oxygen compounds). This type of property tends to cause problems with conventional conveying and / or processing equipment, including increased surnames during processing, reduced catalyst life, blocked processes, and / or chlorine use. Improved systems, methods, and / or catalysts for converting inferior crudes into crude products with more desirable properties still have significant economic and technical needs. There is also a significant economic and technical need for systems, systems, methods, and / or catalysts that can change the selected properties of inferior crudes, but only selectively change other properties of inferior crudes. [Summary of the Invention] The present invention is generally related to a system, method, and catalyst for converting a crude oil feed to a total product containing a crude oil product and a non-condensable gas in a right-dried embodiment. The present invention also relates generally to compositions containing novel combinations of ingredients therein. Such compositions can be obtained using the system and 200533737 method described herein. The invention provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25 ° C and 0.101 MPa, the The crude feed has a TAN of at least 0.3, the at least one catalyst has a pore size distribution with a median pore size in the range of 90 A to 180 people, and at least 60% of the total pore size in the pore size distribution has a value in the range of 45 A. The pore size in the median pore size range, where the pore size distribution is determined by ASTM method D4282; and the contact conditions are controlled so that the crude oil product has a TAN of the crude oil feed with a TAN of up to 90%, where TAN is determined by the ASTM method D664 determination. The present invention also provides a method of producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is at 25. (: And 0 · 101 MPaT is a liquid mixture, the crude oil feed has a TAN of at least 0.3, the at least one catalyst has a pore size distribution with a median pore size of at least 90λ, and it is measured by the aSTm method 04282, and the contact The catalyst contains 0.001 g to 0 g of hydrazone or hydrazone compound, or a mixture thereof, based on the weight of molybdenum per gram of catalyst; and controlling the contact conditions so that the crude oil product has a TAN of at most 9 0% of the TAN of the crude oil feed, where TAN is determined by ASTM method D664. The present invention also provides a method of producing a crude oil product, comprising: contacting the crude oil feed with one or more catalysts to produce a crude oil product containing The total product, wherein the crude product is a liquid mixture at 25 ° C. and 0.101 MPa, the crude feed has a TAN of at least 0.3, as determined by ASTM D664, the at least one catalyst has a median pore size of at least 18 〇Personal pore size distribution, 200533737, measured by ASTM method D4282, the catalyst has one or more compounds containing one or more metals in column 6 of the periodic table, one or more compounds of one or more metals in periodic table 6, or a mixture thereof of Pore size distribution; and controlling contact conditions so that the crude oil product has a TAN of the crude oil feed with a TAN of at most 90%, wherein the TAN is determined by ASTM method D664. The present invention also provides a method for producing a crude oil product, comprising: The crude oil feed is contacted with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25 ° C. and 0.11 MPa, the crude oil feed having at least 0.3 TAN, measured by ASTM method D664, the at least one catalyst comprises: (a) one or more metals in column 6 of the periodic table, one or more compounds of one or more metals in column 6 of the periodic table, or Mixtures; and (b) one or more metals in column 10 of the periodic table, one or more compounds of one or more metals in column 10 of the periodic table, or mixtures thereof, wherein the total amount of metals in column 10 and metal in column 6 The total molar ratio is in the range of 1 to 10; and the contact conditions are controlled so that the crude oil product has a TAN of the crude oil feed with a TAN of at most 90%, where TAN is determined by ASTM method D664. The present invention also Provide methods for producing crude oil products It includes: contacting crude oil 2 with one or more catalysts to produce a total product containing crude oil products, wherein the crude oil product is a liquid mixture at 25t and 0.101 MPa, and the raw material / feedstock has at least 0.3 TAN 'The one or more catalysts include: (a) the first catalyst, which is based on the metal weight per gram of the first catalyst, and contains one or more of column 6 of the periodic table from 0.0001 to 0.06 grams; Metal, column 6 of the periodic table—one or more compounds of the metal, or a mixture thereof 200533737; and ⑻ second catalyst 'the second catalyst contains at least one gram of metal by weight of the metal . Touch,. ^. S See one or more of the metals in the Periodic Table, 6-or more metals-or more compounds, or mixtures thereof, in column 6 of the Periodic Table; and control the contact conditions to maximize the original ^ Ah, the ⑽ of this crude oil feed was determined by ASTM method D664. fine

本發明亦提供觸媒組成物，其包括：⑷週期表第$ 攔的-或多種金屬，週期表帛5欄之—或多種金屬的—或 多種化合物’或其混合物；(b)載體，其具有Θ氧化銘含量 為每克載體中至少(M克的θ氧化紹，其藉由χ射線繞射測 定二其中該觸媒具有中位孔徑至少為23〇人的孔徑分佈， 其藉由ASTM法D4282測定。The present invention also provides a catalyst composition, which includes: (i) the metal of the periodic table-or a plurality of metals, column 5 of the periodic table-or a plurality of metals-or a plurality of compounds' or a mixture thereof; (b) a carrier, which It has a θ oxide content of at least (M grams of θ oxide) per gram of the carrier, which is determined by X-ray diffraction. The catalyst has a pore size distribution with a median pore size of at least 23 people. D4282 determination.

本發明亦提供觸媒組成物，其包括：（a)週期表第6 攔的-或多種金屬’週期表帛6攔之—或多種金屬的—或 多種化合物’或其混合物；（b)載體，其具有0氧化鋁含量 =每克載體中至少（M克的θ氧化銘，其藉由4線繞射= 定；其中該觸媒具有中位孔徑至少為23〇Α的孔徑分佈， 其藉由ASTM法D4282測定。 本發明亦提供觸媒組成物，其包括··（a)週期表第5 攔的一或多種金屬，週期表第5攔之一或多種金屬的一或 多種化合物，週期表第6攔的一或多種金屬，週期表第6 欄之一或多種金屬的一或多種化合物，或其混合物；（b)載 體，其具有Θ氧化鋁含量為每克載體中至少〇1克的㊀氧化 铭’其藉由X射線繞射測定；其中該觸媒具有中位孔接至 11 200533737 m 少為230A的孔徑分佈，其藉由ASTM法D4282測定。 ： 本發明亦提供生產觸媒之方法，其包括：使載體與一 或多種金屬結合以形成載體/金屬混合物，其中該載體包含 Θ氧化鋁，而一或多種金屬包括週期表第5攔的一或多種 金屬，週期表第5欄之一或多種金屬的一或多種化合物， 或其混合物；於至少40(TC的溫度下熱處理θ氧化鋁載體/ 金屬混合物；及形成觸媒，其中該觸媒具有中位孔徑至少 為230人的孔徑分佈’其藉由ASTM法D4282測定。 本發明亦提供生產觸媒之方法，其包括：使載體與一鲁 或多種金屬結合以形成載體/金屬混合物，其中該載體包含 Θ氧化鋁，而一或多種金屬包括週期表第6襴的一或多種 金屬，週期表第6攔之一或多種金屬的一或多種化合物， 或其混合物；於至少400°C的溫度下熱處理㊀氧化鋁載體/ 金屬混合物；及形成觸媒，其中該觸媒具有中位孔徑至少 為230A的孔徑分佈，其藉由ASTM法m282測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產·， · 其中遠原油產物在25°C和0.101 MPa下為液態混合物，該 原油進料具有至少0.3 # TAN，該至少一種觸媒具有中位 孔咎至J為180A的孔徑分佈，其藉由ASTM法D4282測 定，該觸媒具有包含Θ氧化鋁和週期表第6欄的一或多種 金屬，週期表第6欄之一或多種金屬的一或多種化合物，The present invention also provides a catalyst composition, which includes: (a) 6th or more metals of the periodic table '6th of the periodic table'-or more metals-or multiple compounds' or a mixture thereof; (b) a carrier , Which has a content of 0 alumina = at least (M grams of θ oxidized oxide per gram of carrier, which is determined by 4-wire diffraction = where; the catalyst has a pore size distribution with a median pore size of at least 23〇A, and it borrows Determined by ASTM method D4282. The present invention also provides a catalyst composition, which includes (a) one or more metals of the fifth block of the periodic table, one or more compounds of one or more metals of the fifth block of the periodic table, the period One or more metals listed in Table 6, one or more compounds of one or more metals in column 6 of the Periodic Table, or a mixture thereof; (b) a carrier having a Θ alumina content of at least 0.01 g per gram of carrier The ㊀oxidation inscription 'is measured by X-ray diffraction; wherein the catalyst has a pore size distribution with a median hole connected to 11 200533737 m and less than 230A, which is measured by ASTM method D4282. The invention also provides production catalysts A method comprising: combining a support with one or more metals Forming a support / metal mixture, wherein the support comprises Θ alumina, and the one or more metals include one or more metals in column 5 of the periodic table, one or more compounds of one or more metals in column 5 of the periodic table, or a mixture thereof ; Heat-treating the θ alumina support / metal mixture at a temperature of at least 40 ° C .; and forming a catalyst, wherein the catalyst has a pore size distribution having a median pore size of at least 230 people, which is determined by ASTM method D4282. The present invention is also Provide a method for producing a catalyst, comprising: combining a support with one or more metals to form a support / metal mixture, wherein the support comprises Θ alumina and the one or more metals include one or more metals of Period 6 of the Periodic Table , One or more compounds of one or more metals, or a mixture thereof, of the sixth table of the Periodic Table; heat-treating the alumina carrier / metal mixture at a temperature of at least 400 ° C; and forming a catalyst, wherein the catalyst has a median position A pore size distribution having a pore size of at least 230 A, as determined by ASTM method m282. The present invention also provides a method for producing a crude oil product, which comprises: feeding a crude oil with one or more The catalyst is contacted to produce a total output containing crude oil products, where the crude oil product is a liquid mixture at 25 ° C and 0.101 MPa, the crude oil feed has at least 0.3 # TAN, and the at least one catalyst has a median porosity To J is a pore size distribution of 180A, measured by ASTM method D4282, the catalyst has one or more metals including Θ alumina and column 6 of the periodic table, and one or more metals of column 6 of the periodic table. Compounds,

或其混合物的孔徑分佈；及控制接觸條件以便使該原油產 物具有TAN最多為90%之該原油進料的TAN，其中TAN 12 200533737 係错由A S Τ Μ法D 6 6 4測定。 本發明亦提供生產原油產物之方法，其包括：於氣源 存在下，使原油進料與一或多種觸媒接觸以生產含有原由 產㈣總產物，其中該原油產物在坑和〇 i〇i Mpa;為 液態混合物，該原油進料具有至少〇 3 # tan，該原油進 料具有含氧量為每克原油進料至少有請Gi克的氧，节至 少一種觸媒具有中位孔徑至少為90A的孔徑分佈，其藉由 ASTM法D4282敎；及控制接觸條件使⑽減少以^使 該原油產物具有TAN最多為9〇%之該原油進料的m 並且減少含有機氧化合物的含量以便使該原油產物具有含 氧量最多為90%之該原油進料的含氧量，其中ταν係藉由 STM法D664測定’而含氧量係藉由astm法Ε385測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與-或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25t和請i略下為液態混合物，該 原油進料具有至少（Μ @ TAN，該至少—種觸媒在每克觸 媒中，以金屬重量計，含有至少〇〇〇1克之週期表第6攔 的一或多種金屬，週期表第6攔之一或多種金屬的一或多 種化合物，或其混合物；及控制接觸條件以便使接觸區中 :液體空間速度㈣1〇 h'並且使該原油產物具有TAN 取夕為90%之該原油進料的ΤΑΝ，其中ΤΑΝ係藉由 法D664測定。 本發明亦提供生產原油產物之方法，其包括·於氮源 存在下，使原油進料與一或多種觸媒接觸以生產含有原油 13 200533737 產物的總產物，其中該原油產物在说和〇 ι〇ι 下為 液態混合物’該原油進料具有至少〇 ·…AN，該原油進 料具有含硫量為每克原油進料至少有請G1克的硫，該至 少-種觸媒包含週期表第6欄的一或多種金屬，週期表第 6欄之-或多種金屬的—或多種化合物，或其混合物；及 控制接觸條件以便使該原油進料於接觸期間在選定率下吸 取分子氫以抑制該原油進料在接觸期間的相分離，使—或 多個接觸區中的液體空間速度超㉟1Qh·,，使該原油產物 具有TAN最多為9〇%之該原油進料的Μ，並且使兮原 油產物具有含硫量為70至13〇%之該原油進料的含硫量:、 其中TAN係藉由ASTM法D664測定，而含硫量係藉由 ASTM 法 D4294 測定。 〃本發明亦提供生產原油產物之方法，其包括：於氣態 虱源存在下，使原油進料與—或多種觸媒接觸以生產含有 原油產物的總產物，其中該原油產物纟说和q igi他 下為液態混合物；及控制接觸條件以便使該原油進 觸期間在選定率下吸取氫以抑制 相分離。 卩t亥原油進枓在接觸期間的 本發明亦提供生產原油產物之方法，其包括：於 多種觸媒存在下，使原油進料與氯接觸以生產含有產 物的總產物’其中該原油產物在说和〇 i〇i奶；為 態混合物，·及控制接觸條件以便使該原油進料於第—气:： 取條件下及接著於第二氯吸取條件下與氯接觸，第_ = 取條件與第二氫吸取條件不同，控制第-氫吸取條件^ 14 200533737 的淨吸取以防止原油進料/總產物混合物的p值減至15以 下，该原油產物的一或多種性質與該原油進料的一或多種 個別性質相比最多有9〇%的改變。 本發明亦提供生產原油產物之方法，其包括··於第一 溫度下，使原油進料與一或多種觸媒接觸，接著於第二溫 度下接觸以生產含有原油產物的總產物，纟中該原油產物 在25°C和0.101 MPa下為液態混合物，該原油進料具有至 少〇·3的TAN ;及控制接觸條件使第一接觸温度至少低於 第二接觸溫度3(TC，使該原油產物與該原油進料的TAN 相比，具有最多為9〇%的ΤΑΝ，其中ΤΑΝ係藉由astm 法D664測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25。。和0·101 MPa下為液態混合物該 原油進料具有至少0.3的TAN，該原油進料具有含硫量為 每克原油進料至少有0.0001克的硫，該至少一種觸媒包含 週期表第6攔的一或多種金屬，週期表第6欄之一或多種 金屬的一或多種化合物，或其混合物；及控制接觸條件以 便使該原油產物具有TAN最多為90%之該原油進料的 TAN 並且使该原油產物具有含硫量為70至1 3〇%之該原 油進料的含硫量，其中TAN係藉由ASTM法D664測定， 而含硫量係藉由ASTM法D4294測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 15 200533737 其中該原油產物在25X：和〇.1()1 MPa下為液態混合物，該 原油進料具有至少0·1的TAN，該原油進料具有殘留物含 量為每克原油進料至少有〇.丨克的殘留物，該至少一種觸 媒包含週期表第6攔的一或多種金屬，週期表第6欄之一 或多種金屬的一或多種化合物，或其混合物；及控制接觸 條件以便使該原油產物具有TAN最多為9〇%之該原油進料 的TAN，使為原油產物具有殘留物含量為7〇至1 之該 原油進料的殘留物含量，其中TAN係藉由astm法加64 測定，而殘留物含量係藉由ASTM法D5307測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25。(：和0.ΠΗ MPa下為液態混合物，該 f油進料具有至少〇」的TAN，該原油進料具有vg〇含 里為每克原油進料至少有〇」克的VG〇，該至少一種觸媒 包含週期表第6攔的一或多種金屬，週期表第6攔之一或 多種金屬的一或多種化合物，或其混合物；及控制接觸條 件以便使該原油產物具彳TAN最多為9〇%之該原油進料的 tan，使該原油產物具有VG0含量為7〇至13〇%之該原油 進料的VGO含量，其中VG0含量係藉由八灯馗法D53〇7 測定。 本發明亦提供生產原油產物之方法，其包括；使原油 進料與-或多種觸媒接觸以生產含有原油產物的總產物: 其中該原油產物在25。(；和0.ΗΗ MPa下為液態混合物，該 原油進料具有至少〇·3的TAN，玆空儿、^ 16 200533737 二獲得：使載體與週期表第6欄的一或多種金屬，週期表 第6搁之-或多種金屬的-或多種化合物，或其混合物結 合以產生觸媒前驅物；於一或多種含硫化合物存在下，在 低於500t：的溫度下加熱此觸媒前驅物形成觸媒；及控制 接觸條件以便使該原油產物具有TAN最多為9〇%之該原油 進料的TAN。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25。(：和〇·1〇1 MPa下為液態混合物，該 原油進料在37_8°C(10〇T)下具有至少i〇cSt的黏度，該原 油進料具有至少1 〇的API比重’該至少一種觸媒包含週 期表第6欄的一或多種金屬，週期表第6攔之一或多種金 屬的一或多種化合物，或其混合物；及控制接觸條件以便 使該原油產物具有在37.8°C下的黏度最多為9〇%之該原油 進料在37.8°C下的黏度，並且使該原油產物具有API比重 為70至130%之該原油進料的API比重，其中API比重係 藉由ASTM法D6822測定，而黏度係藉由ASTM法D2669 測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25°C和0.101 MPa下為液態混合物，該 原油進料具有至少〇·1的TAN，該一或多種觸媒包含：一 或多種含有釩，一或多種釩化合物，或其混合物的觸媒； 與附加觸媒，其中該附加觸媒包含一或多種第6欄金屬， 200533737 一或多種第6攔金屬的一或多種化合物，或其組合；及控 制接觸條件以便使該原油產物具有TAN最多為90%之該原 油進料的TAN，其中TAN係藉由ASTM法D664測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25°C和0.101 MPa下為液態混合物，該 原油進料具有至少Ο·!的TAN ;在接觸期間產生氫；及控 制接觸條件以便使該原油產物具有TAN最多為90%之該原 油進料的TAN，其中TAN係藉由ASTM法d664測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25。(：和0.101 MPa下為液態混合物，該 原油進料具有至少0.1的TAN，該至少一種觸媒包含釩， 一或多種釩化合物，或其混合物；及控制接觸條件以便使 接觸溫度至少為20(rc，使該原油產物具有tAN最多為9〇% 之該原油進料的TAN，其中TAN係藉由Astm法d664測 定。 本發明亦提供生產原油產物之方法，其包括；使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25T：和0.101皿卜下為液態混合物，該 原油進料具有至少〇.丨的TAN，該至少一種觸媒包含釩f 或多種釩化合物，或其混合物；在接觸期間供應含有氫 的氣體源，該氣流係以原油進料流動相反的方向供應；及 控制接觸條件以便使該原油產物具有TAN最多為9〇%之該 18 200533737 原油進料的TAN，其中TAN係藉由ASTM法D664測定。 ： 本發明亦提供生產原油產物之方法，其包括··使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中该原油產物在25°C和0· 101 MPa下為液態混合物，該 原油進料在每克原油進料中具有至少〇 〇〇〇〇2克的總 Ni/V/Fe含量，該至少一種觸媒包含釩，一或多種釩化合 物，或其混合物，該釩觸媒具有中位孔徑至少為i 8〇A的 孔徑分佈，及控制接觸條件以便使該原油產物具有總 Ni/V/Fe含量最多為90%之該原油進料的Ni/V/Fe含量，其鲁 中Ni/V/Fe含量係藉由ASTM法D5708測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在2代和〇·1()1 MPa下為液態混合物，該 至少-種觸媒包含釩，一或多種釩化合物，或其混合物， 該原油進料包含-或多種有機酸的_或多種驗金屬鹽，一 或多種有機酸的一或多種鹼土金屬鹽，或其混合物，該原 油進料在每克原油進料中具有至彡〇 〇〇〇〇1克之有機酸金 φ 屬鹽形態的驗金屬和驗土金屬總含量；及控制接觸條件以 便使該原油產物具有有機酸金屬鹽形態之金屬牙口鹼土金 屬總含量最多之該原油進料中有機酸金屬鹽形態的 驗金屬和驗土金屬含量，豆φ右她 蜀3里具中有機酸金屬鹽形態的鹼金屬 和鹼土金屬含量係藉由ASTM法D1318測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與-或多種觸媒接觸以生產含有原油產物的總產物， 19 200533737 其中該原油產物在25°C和0.101 MPa下為液態混合物，該 ： 原油進料包含一或多種有機酸的一或多種驗金屬鹽，一或 多種有機酸的一或多種驗土金屬鹽，或其混合物，該原油 進料在每克原油進料中具有至少〇·〇〇〇〇1克之有機酸金屬 鹽形態的鹼金屬和鹼土金屬總含量，該至少一種觸媒具有 中位孔徑在90 Α至180人之範圍内的孔徑分佈，該孔徑分 佈中至少60%的總孔數具有在45人之中位孔徑範圍内的 孔徑，其中孔徑分佈係藉由ASTM法D4282測定；及控制 接觸條件以便使該原油產物具有有機酸金屬鹽形態之鹼金 _ 屬和驗土金屬總含量最多為90%之該原油進料的有機酸金 屬鹽形態的鹼金屬和鹼土金屬含量，其中有機酸金屬鹽形 恶的驗金屬和驗土金屬含量係藉由ASTM法D1 3 1 8測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25°C和0.101 MPa下為液態混合物，該 原油進料在每克原油進料中具有至少〇 〇〇〇〇2克的總 Ni/V/Fe含量，該至少一種觸媒具有中位孔徑在9〇a至ι8〇 · A之範圍内的孔徑分佈，該孔徑分佈中至少6〇%的總孔數 具有在45 A之中位孔徑範圍内的孔徑，其中孔徑分佈係藉 由ASTM法D4282測定；及控制接觸條件以便使該原油產 物具有總Ni/V/Fe含量最多為9〇%之該原油進料的Ni/V/Fe 含量，其中Ni/V/Fe含量係藉由ASTM法D57〇8測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 20 200533737 其中該原油產物在25°C和0.101 MPa下為液態混合物，該 ： 原油進料在每克原油進料中具有至少〇〇〇〇〇1克之有機酸 金屬鹽形態的驗金屬和驗土金屬總含量，該至少一種觸媒 具有中位孔徑至少為18〇A的孔徑分佈，其藉由ASTM法 D4282測定，該觸媒具有包含週期表第6欄的一或多種金 屬，週期表第6攔之一或多種金屬的一或多種化合物，或 其混合物的孔徑分佈；及控制接觸條件以便使該原油產物 具有有機酸金屬鹽形態之鹼金屬和鹼土金屬總含量最多為 90%之該原油進料中有機酸金屬鹽形態的鹼金屬和鹼土金春 屬含量，其中有機酸金屬鹽形態的鹼金屬和鹼土金屬含量 係藉由ASTM法D1318測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25°C和0.101 MPa下為液態混合物，該 原油進料包含一或多種有機酸的一或多種鹼金屬鹽，一或 多種有機酸的一或多種鹼土金屬鹽，或其混合物，該原油 進料在每克原油進料中具有至少0·00001克之有機酸金屬 春 鹽形態的鹼金屬和鹼土金屬總含量，該至少一種觸媒具有 中位孔徑至少為230Α的孔徑分佈，其藉由ASTM法D4282 測定，該觸媒具有包含週期表第6欄的一或多種金屬，週 期表第6欄之一或多種金屬的一或多種化合物，或其混合 物的孔徑分佈；及控制接觸條件以便使該原油產物具有有 機酸金屬鹽形怨之驗金屬和驗土金屬總含量最多為之 該原油進料中有機酸金屬鹽形態的鹼金屬和鹼土金屬含 21 200533737 里，其中有機酸金屬鹽形態的驗金屬和驗土金屬含量係藉 由ASTM法D1318測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25。(：和〇·1〇1 MPa下為液態混合物，該 原油進料具有總Ni/V/Fe含量為每克原油進料中至少有 0.00002克的Ni/V/Fe，該至少一種觸媒具有中位孔徑至少 為230A的孔徑分佈，其藉由ASTM法D4282測定，該觸Or its mixture; and controlling the contact conditions so that the crude oil product has a TAN of the crude oil feed with a TAN of at most 90%, where the TAN 12 200533737 is determined by the AS TM method D 6 64. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts in the presence of a gas source to produce a total product containing a source of plutonium, wherein the crude oil product is in a pit and 〇i〇i Mpa; is a liquid mixture, the crude oil feed has at least 0 3 # tan, the crude oil feed has an oxygen content of at least Gi grams of oxygen per gram of crude oil feed, and at least one catalyst has a median pore size of at least 90A pore size distribution by ASTM method D4282 敎; and control of contact conditions to reduce ⑽ so that the crude oil product has m of the crude oil feed with a TAN of up to 90% and reduce the content of organic oxygen compounds so that The crude oil product has the oxygen content of the crude oil feed with an oxygen content of up to 90%, where ταν is determined by STM method D664 'and the oxygen content is determined by astm method E385. The present invention also provides a method for producing a crude oil product, which comprises: contacting a crude oil feed with-or a plurality of catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25 t and 1 o The feed has at least (M @ TAN, the at least one catalyst in one gram of catalyst, based on the weight of the metal, contains one or more metals in the sixth table of the periodic table, the sixth table of the periodic table One or more compounds of one or more metals, or a mixture thereof; and controlling the contact conditions so that in the contact zone: the liquid space velocity is 〇10h 'and the crude product has a TAN of 90% of the crude feed TAN, where TAN is determined by method D664. The present invention also provides a method for producing a crude oil product, which comprises: contacting a crude oil feed with one or more catalysts in the presence of a nitrogen source to produce a total product containing crude oil 13 200533737 Product, where the crude product is a liquid mixture at 100 mM, the crude feed has at least 0 .... AN, the crude feed has a sulfur content of at least G1 gram of sulfur, the at least one catalyst comprising one or more metals in column 6 of the periodic table,-or more metals in column 6 of the periodic table-or more compounds, or mixtures thereof; and controlling the contact conditions so that the The crude oil feed absorbs molecular hydrogen at a selected rate during the contact period to suppress the phase separation of the crude oil feed during the contact period, so that—or the liquid space velocity in the multiple contact zones exceeds 1Qh ·, so that the crude oil product has the most TAN. Is 90% of the crude oil feed, and the crude oil product has a sulfur content of 70 to 13% of the crude oil feed: where TAN is determined by ASTM method D664, and Sulfur content is determined by ASTM method D4294. 〃 The present invention also provides a method for producing crude oil products, which includes: contacting a crude oil feed with—or multiple catalysts in the presence of a gaseous lice source—to produce a total product containing crude oil products Where the crude oil product is a liquid mixture; and control the contact conditions so that hydrogen is absorbed at a selected rate during the contact of the crude oil to inhibit phase separation. The present invention during contact Provide a method for producing a crude oil product, comprising: contacting a crude oil feed with chlorine in the presence of various catalysts to produce a total product containing the product 'wherein the crude oil product is said to be oi milk; as a mixture, · And control the contact conditions so that the crude oil is fed in the first gas :: under the conditions of extraction and then in contact with the second chlorine absorption conditions, the _ = extraction conditions are different from the second hydrogen absorption conditions, control the-hydrogen absorption Condition ^ 14 200533737 Net draw to prevent p value of crude oil feed / total product mixture from falling below 15, one or more properties of the crude oil product are up to 90% compared to one or more individual properties of the crude oil feed The present invention also provides a method for producing a crude oil product, which includes contacting a crude oil feed with one or more catalysts at a first temperature and then contacting at a second temperature to produce a total product containing a crude oil product. The crude oil product is a liquid mixture at 25 ° C and 0.101 MPa, and the crude feed has a TAN of at least 0.3; and the contact conditions are controlled so that the first contact temperature is at least lower than the second contact temperature 3 (TC Compared with the TAN of the crude oil feed, the crude oil product has a TAN of up to 90%, wherein the TAN is determined by the astm method D664. The present invention also provides a method of producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is at 25. . And a liquid mixture at 0 · 101 MPa. The crude oil feed has a TAN of at least 0.3, the crude oil feed has a sulfur content of at least 0.0001 g of sulfur per gram of crude oil feed, and the at least one catalyst comprises the sixth periodic table One or more metals, one or more compounds of one or more metals in column 6 of the periodic table, or a mixture thereof; and controlling the contact conditions so that the crude oil product has a TAN of up to 90% of the TAN of the crude oil feed and The crude product is made to have a sulfur content of 70 to 130% of the crude feed, wherein TAN is measured by ASTM method D664 and sulfur content is measured by ASTM method D4294. The invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing the crude oil product, 15 200533737 wherein the crude oil product is at 25X: and 0.1 (1) MPa The following is a liquid mixture, the crude feed has a TAN of at least 0.1, the crude feed has a residue content of at least 0.1 g per gram of crude feed, and the at least one catalyst contains the first One or more metals, one or more compounds of one or more metals in column 6 of the periodic table, or a mixture thereof; and controlling the contact conditions so that the crude oil product has a TAN of up to 90% of the crude oil feed TAN is a residue of the crude oil feed having a residue content of 70 to 1 of the crude oil feed, wherein TAN is determined by the astm method plus 64, and the residue content is determined by the ASTM method D5307. The present invention also provides a method of producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is at 25. (: And a liquid mixture at 0. ΠΗ MPa, the f oil feed has a TAN of at least 0 ", the crude oil feed has vg0 containing at least 0" grams of VG0 per gram of crude oil feed, the at least A catalyst comprising one or more metals of the sixth table of the periodic table, one or more compounds of one or more metals of the sixth table of the periodic table, or a mixture thereof; and controlling the contact conditions so that the crude oil product has a TAN of at most 9 0% of the tan of the crude oil feed, so that the crude oil product has a VGO content of 70 to 130% of the crude oil feed, where the VG0 content is determined by the eight lamp method D5307. The present invention A method of producing a crude oil product is also provided, comprising: contacting a crude oil feed with-or a plurality of catalysts to produce a total product containing the crude oil product: wherein the crude oil product is a liquid mixture at 25 ° (; and 0.ΗΗ MPa, The crude oil feed has a TAN of at least 0.3, Zikonger, ^ 16 200533737, two obtained: the carrier and one or more metals in column 6 of the periodic table, the sixth-or more metals-or more of the periodic table Compounds, or mixtures thereof, to produce catalyst precursors In the presence of one or more sulfur-containing compounds, heating the catalyst precursor at a temperature below 500 t: to form a catalyst; and controlling the contact conditions so that the crude oil product has a maximum TAN of 90% of the crude oil. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is at 25 ° (: and 0.1 〇1 MPa is a liquid mixture, the crude oil feed has a viscosity of at least 10cSt at 37_8 ° C (100 ° T), the crude oil feed has an API specific gravity of at least 10, the at least one catalyst contains a periodic table One or more metals in column 6, one or more compounds of one or more metals in the sixth table of the periodic table, or a mixture thereof; and controlling the contact conditions so that the crude oil product has a viscosity of up to 97.8 ° C at 37.8 ° C. % Of the crude oil feed at 37.8 ° C, and the crude oil product has an API specific gravity of 70 to 130% of the crude oil feed, wherein the API specific gravity is determined by ASTM method D6822, and the viscosity is Measured by ASTM method D2669 The invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25 ° C and 0.101 MPa, The crude feed has a TAN of at least 0.1, and the one or more catalysts include: one or more catalysts containing vanadium, one or more vanadium compounds, or a mixture thereof; and an additional catalyst, wherein the additional catalyst comprises One or more column 6 metals, 200533737 one or more compounds of the sixth metal, or a combination thereof; and controlling the contact conditions so that the crude product has a TAN of the crude feed of up to 90% of the TAN, wherein TAN is measured by ASTM method D664. The invention also provides a method for producing a crude product, comprising: contacting a crude feed with one or more catalysts to produce a total product containing a crude product, wherein the crude product is a liquid mixture at 25 ° C and 0.101 MPa, the The crude oil feed has a TAN of at least 0 !; hydrogen is produced during the contacting; and the contacting conditions are controlled so that the crude oil product has a TAN of the crude oil feed with a TAN of up to 90%, where TAN is determined by ASTM method d664. The present invention also provides a method of producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is at 25. (: And a liquid mixture at 0.101 MPa, the crude oil feed has a TAN of at least 0.1, the at least one catalyst contains vanadium, one or more vanadium compounds, or a mixture thereof; and controlling the contact conditions such that the contact temperature is at least 20 ( rc, so that the crude oil product has a TAN with a tAN of up to 90% of the crude oil feed, where TAN is determined by the Astm method d664. The present invention also provides a method for producing a crude oil product, comprising: Or more catalysts are contacted to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25T: and 0.101 liters, the crude oil feed has a TAN of at least 0.1, and the at least one catalyst contains vanadium f Or more vanadium compounds, or mixtures thereof; supplying a hydrogen-containing gas source during the contact, the gas stream being supplied in the opposite direction of the crude oil feed flow; and controlling the contact conditions so that the crude product has a TAN of up to 90% of the 18 200533737 The TAN of crude oil feed, where TAN is determined by ASTM method D664. The present invention also provides a method for producing a crude oil product, which includes ... Various catalysts are contacted to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25 ° C and 0. 101 MPa, and the crude oil feed has at least 20000 per gram of crude oil feed Grams of total Ni / V / Fe content, the at least one catalyst comprises vanadium, one or more vanadium compounds, or a mixture thereof, the vanadium catalyst has a pore size distribution with a median pore size of at least i 8OA, and controlled contact conditions In order to make the crude oil product have the Ni / V / Fe content of the crude oil feed with a total Ni / V / Fe content of up to 90%, the Ni / V / Fe content in the middle is determined by ASTM method D5708. The present invention also Provide a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at generation 2 and 0.1 (1) MPa, The at least one catalyst comprises vanadium, one or more vanadium compounds, or a mixture thereof, the crude feed comprises one or more metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, Or a mixture thereof, the crude oil is fed in per gram The oil feed has an organic acid gold content of up to 10,000 g of organic metal in the form of a salt and a metal content of the soil test; and controlling the contact conditions so that the crude oil product has a metal tooth alkaline earth in the form of an organic acid metal salt The metal content of the organic acid metal salt and the metal content of the organic acid metal salt in the crude oil feed with the most total metal content. The alkali metal and alkaline earth metal content of the organic acid metal salt in the soybean oil 3 are measured by the ASTM method. Determination of D1318. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with-or a plurality of catalysts to produce a total product containing a crude oil product, 19 200533737 wherein the crude oil product is at 25 ° C and 0.101 MPa Is a liquid mixture, the: crude oil feed comprising one or more metal test salts of one or more organic acids, one or more earth test metal salts of one or more organic acids, or a mixture thereof. The material has a total alkali metal and alkaline earth metal content in the form of an organic acid metal salt of at least 0.0000 g. The at least one catalyst has a median pore size of 90 A to 180 people. Pore size distribution within the range, at least 60% of the total number of pores in the pore size distribution having a pore size in the median pore size range of 45, wherein the pore size distribution is determined by ASTM method D4282; and controlling the contact conditions so that the crude oil product Alkali metals in the form of metal salts of organic acids. The content of alkali metals and alkaline earth metals in the form of organic acid metal salts of the crude oil feed with a total content of up to 90% of the genus and test soil metals. The test soil metal content was measured by ASTM method D1 3 1 8. The invention also provides a method for producing a crude product, comprising: contacting a crude feed with one or more catalysts to produce a total product containing a crude product, wherein the crude product is a liquid mixture at 25 ° C and 0.101 MPa, the The crude oil feed has a total Ni / V / Fe content of at least 20000 grams per gram of crude oil feed, and the at least one catalyst has a median pore size in the range of 90a to 80m. A pore size distribution in which at least 60% of the total number of pores has a pore size in the range of 45 A median pore size, wherein the pore size distribution is determined by ASTM method D4282; and the contact conditions are controlled so that the crude oil product has a total The Ni / V / Fe content of the crude oil feed with a Ni / V / Fe content of up to 90%, wherein the Ni / V / Fe content is determined by ASTM method D5708. The present invention also provides a method for producing a crude product, comprising: contacting a crude feed with one or more catalysts to produce a total product containing the crude product, 20 200533737 wherein the crude product is a liquid mixture at 25 ° C and 0.101 MPa The crude oil feed has at least 10,000 grams of organic acid metal salt in the form of metal and soil test metal content per gram of crude feed, and the at least one catalyst has a median pore size of at least 18. The pore size distribution of A, which is determined by ASTM method D4282, has a pore size of one or more compounds containing one or more metals in column 6 of the periodic table, one or more metals in column 6 of the periodic table, or a mixture thereof. Distribution; and controlling the contact conditions so that the crude oil product has an alkali metal and alkaline earth metal content in the form of organic acid metal salts of up to 90% of the alkali metal and alkaline earth metal springs in the form of organic acid metal salts in the crude oil feed, The content of alkali metals and alkaline earth metals in the form of metal salts of organic acids was determined by ASTM method D1318. The invention also provides a method for producing a crude product, comprising: contacting a crude feed with one or more catalysts to produce a total product containing a crude product, wherein the crude product is a liquid mixture at 25 ° C and 0.101 MPa, the A crude oil feed comprising one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or a mixture thereof, the crude oil feed having at least 0.0001 per gram of crude oil feed The total content of alkali metal and alkaline earth metal in the form of organic acid metal spring salt. The at least one catalyst has a pore size distribution with a median pore size of at least 230A, which is determined by ASTM method D4282. The catalyst has column 6 of the periodic table. Pore size distribution of one or more metals, one or more compounds of one or more metals in column 6 of the periodic table, or a mixture thereof; and controlling the contact conditions so that the crude oil product has an organic acid metal salt-shaped metal and metal The total content of soil metal is up to the alkali metal and alkaline earth metal in the form of organic acid metal salt in the crude oil feed. The content of the organic acid metal salt is 21 200533737. The inspection and test earth metal-based metal content measured by means of ASTM method D1318. The present invention also provides a method of producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is at 25. (: And 0.10 MPa is a liquid mixture, the crude feed has a total Ni / V / Fe content of at least 0.00002 grams of Ni / V / Fe per gram of crude feed, and the at least one catalyst has The median pore size is a pore size distribution of at least 230A, which is determined by ASTM method D4282.

媒具有包含週期表第6欄的一或多種金屬，週期表第6欄 之一或多種金屬的一或多種化合物，或其混合物的孔徑分 佈；及控制接觸條件以便使該原油產物具有總Ni/v/Fe含 量最多為90%之該原油進料的Ni/V/Fe含量，其中Ni/v/Fe 含量係藉由ASTM法D5708測定。 本發明亦提供生產原油產物之方法，其包括：使原油The medium has a pore size distribution containing one or more metals in column 6 of the periodic table, one or more compounds of one or more metals in column 6 of the periodic table, or a mixture thereof; and controlling the contact conditions so that the crude oil product has a total Ni / The Ni / V / Fe content of the crude oil feed whose v / Fe content is at most 90%, wherein the Ni / v / Fe content is determined by ASTM method D5708. The invention also provides a method for producing a crude oil product, comprising:

進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25t和㈣！ Mpa下為液態混合物該 原油進料包含-或多種有機酸的_或多種驗金屬鹽，—或 多種有機酸的一或多種鹼土金屬#，或其混合物，該原油 進料在每克原油進料中具有至少〇〇〇〇〇1纟之有機酸金屬 鹽形態的鹼金屬和鹼土金屬總含量，該至少一種觸媒具有 中位孔徑至少為90A的孔徑分佈，其藉由…頂法D4282 測定，該觸媒在每克觸媒中，以銷的重量計，H總含钥 量為_克至0.3克的銦、—或多種翻化合物，或其混 合物；及控制接觸條件以便使該原油產物具有有機酸金屬 22 200533737 鹽形悲之驗金屬和鹼土金屬總含量最多為9 〇 %之該原油進 料中有機酸金屬鹽形態的鹼金屬和鹼土金屬含量，其中有 機酸金屬鹽形態的驗金屬和驗土金屬含量係藉由ASTM法 D 1 3 1 8測定。The feed is contacted with one or more catalysts to produce a total product containing a crude product, where the crude product is at 25t and ㈣! Mpa is a liquid mixture. The crude oil feed contains-or more organic acid _ or more metal test salts,-or more organic acid one or more alkaline earth metals #, or a mixture thereof. The crude oil feed is per gram of crude oil feed. The total alkali metal and alkaline earth metal content in the form of an organic acid metal salt of at least 10,000, the at least one catalyst has a pore size distribution with a median pore size of at least 90A, which is determined by the top method D4282, The catalyst in each gram of catalyst, based on the weight of the pin, H has a total key content of _ grams to 0.3 grams of indium, or a plurality of compounds, or a mixture thereof; and controlling the contact conditions so that the crude oil product has Organic acid metal 22 200533737 Alkaline metal and alkaline earth metal content in the form of organic acid metal salt in the crude oil feed with a total content of up to 90% of the test metal and alkaline earth metal in the crude oil feed. The soil metal content was determined by ASTM method D 1 3 1 8.

本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25°C和0.101 MPa下為液態混合物，該 原油進料具有至少0.3的TAN且該原油進料在每克原油進 料中具有至少為0.00002克的總Ni/V/Fe含量，該至少一 種觸媒具有中位孔徑至少為90A的孔徑分佈，其藉由astm 法D4282測定，該觸媒在每克觸媒中，以鉬的重量計，具 有總含鉬量為0.0001克至〇·3克的鉬、一或多種鉬化合物， 或其混合物；及控制接觸條件以便使該原油產物具有tan 最多為90%之該原油進料的ΤΑΝ且該原油產物具有總 Ni/V/Fe含量最多為90%之該原油進料的Ni/V/Fe含量，其 中驗/Fe含量係藉由ASTM法D57〇8測定而tan係 藉由ASTM法D664測定。 本發明亦提供生產原油產物之方法，其包括：使原 進料與-或多種觸媒接觸以生產含有原油產物的總產物 其中該原油產物在饥和G1G1 MPa下為液態混合物， 原油進料包含-或多種有機酸的__或多種驗金屬鹽，— 多種有機酸的一或多種鹼土金屬鹽，或其混合物，該原 進料：每克原油進料中具有至少〇〇〇〇〇1克之有機酸金 鹽形悲的鹼金屬和鹼土金屬總含量，肖至少一種觸媒 23 200533737 含· Ο)週期表第6攔的一或多種金屬，週期表第6攔之 ： 一或多種金屬的一或多種化合物，或其混合物；及（b)週 期表第1 0攔的一或多種金屬，週期表第1 〇欄之一或多種 金屬的一或多種化合物，或其混合物，其中第丨〇攔金屬 總量與第6攔金屬總量的莫耳比在1至10的範圍内；及 控制接觸條件以便使該原油產物具有有機酸金屬鹽形態之 鹼金屬和鹼土金屬總含量最多為9〇%之該原油進料中有機 酸金屬鹽形態的鹼金屬和鹼土金屬含量，其中有機酸金屬 鹽形態的鹼金屬和鹼土金屬含量係藉由ASTM法D1318測 春 定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25°C和0.101 MPa下為液態混合物，該 原油進料具有總Ni/V/Fe含量為每克原油進料中至少有 〇·〇〇〇〇2克的Ni/V/Fe，該至少一種觸媒包含：（a)週期表 第6欄的一或多種金屬，週期表第6攔之一或多種金屬的 一或多種化合物，或其混合物；及（b)週期表第1〇攔的 _ 或夕種金屬，週期表第10欄之一或多種金屬的一或多 種化合物，或其混合物，其中第1 〇欄金屬總量與第6搁 金屬總量的莫耳比在1至10的範圍内；及控制接觸條件 以便使該原油產物具有總Ni/V/Fe含量最多為90%之該原 油進料的Ni/V/Fe含量，其中Ni/V/Fe含量係藉由ASTM 法D5708測定。 本發明亦提供生產原油產物之方法，其包括：使原油 24 200533737 進料與-或多種觸媒接觸以生產含有原油產物的總產物，： 其中該原油產物在25°C和（M01 MPa下為液態混合物，該 原油進料包含一或多種有機酸的一或多種鹼金屬鹽，一或 夕種有機酸的一或多種鹼土金屬鹽，或其混合物，該原油 進料在每克原；由進料中具有至少、〇.〇〇〇〇1克之有機酸金屬 鹽形態的鹼金屬和鹼土金屬總含量’該一或多種觸媒包 含：⑷帛―種觸媒，該第一種觸媒在每克第—種觸媒中， 以金屬重量計，含有0.0001至0.06克之週期表第6攔的 -或多種金屬，週期表第6欄之一或多種金屬的一或多種魯 化合物’或其混合物；&⑻第二種觸媒，該第二種觸媒 在每克第二種觸媒中’以金屬重量計，含有至少〇.02克之 週期表第6欄的-或多種金屬’週期表第6搁之一或多種 益屬的-或多種化合物’或其混合物；及控制接觸條件以 I使該原油產物具有有機酸金屬冑形態之驗金屬和驗土金 屬總含量最多4 90%之該原油進料中有機酸金屬鹽形態的 驗金屬和驗土金屬含量，其中有機酸金屬鹽形態的驗金屬 和鹼土金屬含量係藉由ASTM法D丨3丨8測定。 _ 本發明亦提供生產原油產物之方法，其包括：使原油 進料與-或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在2代和〇.1〇1 MPa下為液態混合物，該 原油進料包含-或多種有機酸的一或多種鹼金屬鹽，一或 多種有機酸的-或多種驗土金屬鹽，或其混合物，該原油 進料在每克原油進料中且右$卜n %了十甲具有至少0·00001克之有機酸金屬 鹽形態的驗金屬和驗土金屬總含量，該至少一種觸媒在每 25 200533737 克觸媒中，以金屬重量計，含有至少0 001克之週期表第 6欄的一或多種金屬，週期表第6欄之一或多種金屬的一 或多種化合物，或其混合物；及控制接觸條件以便使接觸 區中的液體空間速度超過101γ1，並且使該原油產物具有 有機酸金屬鹽形態之鹼金屬和鹼土金屬總含量最多為 之該原油進料中有機酸金屬鹽形態的鹼金屬和鹼土金屬含 量’其中有機酸金屬鹽形態的鹼金屬和鹼土金屬含量係藉 由ASTM法D1318測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25t：和〇.1()1 MPa下為液態混合物，該 原油進料在每克原油進料中具有至少〇 〇〇〇〇2克的總 Ni/V/Fe含量，該至少一種觸媒在每克觸媒中，以金屬重 量計，含有至少0.001克之週期表第6欄的一或多種金屬， 週期表第6欄之一或多種金屬的一或多種化合物，或其混 合物，及控制接觸條件以便使接觸區中的液體空間速度超 過10 h，並且使該原油產物具有總Nj/v/Fe含量最多為 之該原油進料的Ni/V/Fe含量，其中Ni/V/Fe含量係藉由 ASTM 法 D5708 測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25。(：和0_101 MPa下為液態混合物，該 原油進料在每克原油進料中具有含氧量至少為〇〇〇〇1克的 乳 δ &里至少為〇 · 〇 0 0 1克的硫，該至少一種觸媒包含週 26 200533737 期表第6攔的一或多種金屬，週期表第6欄之一或多種金 屬的一或多種化合物，或其混合物；及控制接觸條件以便 使该原油產物具有含氧量最多為9〇%之該原油進料的含氧 里’並且使該原油產物具有含硫量為70至1 30%之該原油 進料的含硫量，其中含氧量係藉由ASTM法E3 85測定， 而含硫量係藉由ASTM法D4294測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25°C和0.101 MPa下為液態混合物，該 原油進料在每克原油進料中具有至少〇 〇〇〇〇2克的總 Ni/V/Fe含量，含硫量至少為0·0001克的硫，該至少一種 觸媒包含週期表第6欄的一或多種金屬，週期表第6攔之 一或多種金屬的一或多種化合物，或其混合物；及控制接 觸條件以便使該原油產物具有總Ni/V/Fe含量最多為9〇% 之該原油進料的Ni/V/Fe含量，並且使該原油產物具有含 石’il里為7 0至1 3 0 %之该原油進料的含硫量，其中Ni/V/Fe 含量係藉由ASTM法D5708測定，而含硫量係藉由A$TM 法D4294測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25°C和0.101 MPa下為液態混合物，該 原油進料包含一或多種有機酸的一或多種驗金屬鹽，一或 多種有機酸的一或多種鹼土金屬鹽，或其混合物，該原油 進料在每克原油進料中具有至少0.00001克之有機酸金屬 27 200533737 鹽形態的鹼金屬和鹼土金屬總含量，殘留物含量至少為〇·丨 · 克的殘留物，該至少一種觸媒包含週期表第6欄的一或多 種金屬，週期表第6欄之一或多種金屬的一或多種化合物， 或其混合物；及控制接觸條件以便使該原油產物具有有機 酸金屬鹽形態之鹼金屬和鹼土金屬總含量最多為9〇%之該 原油進料中有機酸金屬鹽形態的鹼金屬和鹼土金屬含量， 並且使該原油產物具有殘留物含量為7〇至130%之該原油 進料的殘留物含量，其中有機酸金屬鹽形態的鹼金屬和鹼 土金屬含量係藉由ASTM法d 1 3 1 8測定，而殘留物含量係 _ 藉由ASTM法D5307測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中该原油產物在25°C和0· 1 〇 1 MPa下為液態混合物，該 原油進料在每克原油進料中具有殘留物含量至少為〇1克 的殘留物，至少0.00002克的總Ni/V/Fe含量，該至少一 種觸媒包含週期表第6攔的一或多種金屬，週期表第6攔 之一或多種金屬的一或多種化合物，或其混合物；及控制 鲁 接觸條件以便使該原油產物具有總Ni/V/Fe含量最多為9〇% 之忒原油進料的Ni/V/Fe含量，並且使該原油產物具有殘 留物含量為70至130%之該原油進料的殘留物含量，其中 Ni/V/Fe含量係藉由ASTM法D5708測定，而殘留物含量 係藉由ASTM法D5307測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 28 200533737 其中該原油產物在25°C和0.101 MPa下為液態混合物，該 原油進料包含一或多種有機酸的一或多種鹼金屬鹽，一或 多種有機酸的一或多種鹼土金屬鹽，或其混合物，該原油 進料在每克原油進料中具有至少〇.丨克的減壓瓦斯油 (“VGO”）含量，0.0001克之有機酸金屬鹽形態的鹼金屬和 鹼土金屬總含量，該至少一種觸媒包含週期表第6攔的一 或多種金屬，週期表第6欄之一或多種金屬的一或多種化 合物，或其混合物；及控制接觸條件以便使該原油產物具 有有機酸金屬鹽形態之鹼金屬和鹼土金屬總含量最多為 90%之該原油進料中有機酸金屬鹽形態的鹼金屬和鹼土金 屬含量，並且使該原油產物具有VG0含量為7〇至13〇% 之該原油進料的VG0含量，其中VG〇含量係藉由astm 法D5 307測定，而有機酸金屬鹽形態的鹼金屬和鹼土金屬 含量係藉由ASTM法D1 3 1 8測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25。。和0·101 MPa下為液態混合物，該 原油進料在每克原油進料中具有至少〇 〇〇〇〇2克的總 Ni/V/Fe含量，至少克的VG〇含量，該至少一種觸媒 包含週期表第6攔的一或多種金屬，週期表第6欄之一或 多種金屬的一或多種化合物，或其混合物；及控制接觸條 件以便使該原油產物具有總Ni/V/Fe含量最多為9〇%之該 原油進料的Ni/V/Fe含量，並且使該原油產物具有vg〇含 量為70至130%之該原油進料的VG〇含量，其中VG〇含 29 200533737 里係猎由 A S Τ Μ法η $ 1 η 7 、B I — 53〇7測疋，而Ni/v/Fe含量係藉由 ASTM 法 D5708 測定。 本發明亦提供生產焉、、士吝你 座京油產物之方法，其包括：使原油 進料與一或多種觸婼技 ’、^ 生產έ有原油產物的總產物， 其中該原油產物在2 5 °Γ和η 1 m μ η ϋ和0.101 Mpa下為液態混合物，該 原油進料包含一或多插右撼鮮i从 > 义夕種有機g文的一或多種鹼金屬鹽，一或 多種有機酸的一或多插^ 飞夕種鹼土金屬鹽，或其混合物，該原油 進料在每克原油進料中且古5卜 适1*叶〒具有至少0·00001克之有機酸金屬 鹽形態的驗金屬和驗土金屬總含量，該至少—種觸媒可藉 由下列獲得：使載體與週期表第6欄的一或多種金屬，‘ 期表第6攔之-或多種金屬的一或多種化合物，或其混合 物結合以產生觸媒前驅物，於一或多種含硫化合物存在 下，在低& 40(TC的溫度下加熱此觸媒前驅物形成觸媒； 及控制接觸條件讀使該原油產物具有有韻金屬鹽形態 之鹼金屬和鹼土金屬總含量最多為9〇%之該原油進料中有 機酸金屬鹽形態的鹼金屬和鹼土金屬含量，其中有機酸金The invention also provides a method for producing a crude product, comprising: contacting a crude feed with one or more catalysts to produce a total product containing a crude product, wherein the crude product is a liquid mixture at 25 ° C and 0.101 MPa, the The crude feed has a TAN of at least 0.3 and the crude feed has a total Ni / V / Fe content of at least 0.00002 grams per gram of crude feed, the at least one catalyst has a pore size distribution with a median pore size of at least 90A, It is determined by the astm method D4282, the catalyst has a total molybdenum content of 0.0001 g to 0.3 g of molybdenum, one or more molybdenum compounds, or a mixture thereof, based on the weight of molybdenum per gram of the catalyst; And controlling the contact conditions so that the crude oil product has a TAN of 90% of the crude oil feed and the crude product has a total Ni / V / Fe content of 90% of the crude feed Ni / V / Fe content Where the test / Fe content is determined by ASTM method D5708 and tan is determined by ASTM method D664. The present invention also provides a method for producing a crude oil product, comprising: contacting a raw feed with-or a plurality of catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture under the condition of G1G1 MPa, and the crude oil feed contains -One or more metal acid salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or a mixture thereof, the raw feed: at least 100,000 g per gram of crude oil feed The total content of alkali and alkaline earth metals in the form of gold salts of organic acids, at least one catalyst. 23 200533737 Contains · 0) One or more metals listed in Period 6 of the Periodic Table, and one of one or more metals listed in Period 6: Or more compounds, or mixtures thereof; and (b) one or more metals of block 10 of the periodic table, one or more compounds of one or more metals of column 10 of the periodic table, or mixtures thereof, wherein The molar ratio of the total amount of metal to the total amount of the sixth metal is in the range of 1 to 10; and the contact conditions are controlled so that the crude oil product has a total alkali metal and alkaline earth metal content of organic acid metal salt form of up to 90% Should The content of alkali metals and alkaline earth metals in the form of metal salts of organic acids in the crude oil feed. The content of alkali metals and alkaline earth metals in the form of metal salts of organic acids is determined by ASTM method D1318. The invention also provides a method for producing a crude product, comprising: contacting a crude feed with one or more catalysts to produce a total product containing a crude product, wherein the crude product is a liquid mixture at 25 ° C and 0.101 MPa, the The crude feed has a total Ni / V / Fe content of at least 0.0002 grams of Ni / V / Fe per gram of crude feed, the at least one catalyst comprising: (a) column 6 of the periodic table One or more metals, one or more compounds of one or more metals in the Periodic Table of the Periodic Table, or a mixture thereof; and (b) _ or evening metals in the tenth Table of the Periodic Table, one of the tenth column of the Periodic Table One or more compounds of one or more metals, or a mixture thereof, in which the molar ratio of the total amount of the metal in column 10 to the total amount of the sixth metal is in the range of 1 to 10; and controlling the contact conditions so that the crude oil product has The Ni / V / Fe content of the crude oil feed with a total Ni / V / Fe content of up to 90%, wherein the Ni / V / Fe content is determined by ASTM method D5708. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil 24 200533737 feed with-or a plurality of catalysts to produce a total product containing a crude oil product: wherein the crude oil product is at 25 ° C and (M01 MPa is A liquid mixture, the crude oil feed comprising one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or a mixture thereof; The total content of alkali metal and alkaline earth metal in the form of organic acid metal salt of at least 0.0000 g of the material, the one or more catalysts include: ⑷ 帛-a catalyst, the first catalyst in each Gram-type catalyst, based on the weight of the metal, contains 0.0001 to 0.06 grams of the sixth or more metals of the periodic table, one or more of the compounds of one or more metals in column 6 of the periodic table, or a mixture thereof; & ⑻ The second catalyst, which contains at least 0.02 grams of column 6 or more metals per gram of the second catalyst in the second catalyst per gram of the second catalyst 6 one or more beneficial-or more Or a mixture thereof; and controlling the contact conditions so that the crude oil product has an organic acid metal rhenium form and a metal test soil content of up to 4 90% of the metal acid form of the organic acid metal salt in the crude oil feed And test soil metal content, in which the test metal and alkaline earth metal content in the form of organic acid metal salt are determined by ASTM method D 丨 3 丨 8. _ The present invention also provides a method for producing crude oil products, which includes: -Contacting one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at generation 2 and 0.11 MPa, the crude oil feed comprising-or one or more alkali metals of organic acids Salt, one or more organic acids-or more earth-testing metal salts, or mixtures thereof, the crude oil feed is in a gram of crude oil feed and the amount of n is 10% and the organic acid metal salt has at least 0.0001 g The total content of metal and soil metal in the form of the at least one catalyst in each 25,2005,33,737 grams of catalyst, based on the weight of the metal, contains at least 0,001 grams of one or more metals in column 6 of the periodic table. Column One or more compounds of one or more metals, or a mixture thereof; and controlling the contact conditions so that the liquid space velocity in the contact zone exceeds 101γ1, and the crude oil product has the largest total alkali metal and alkaline earth metal content in the form of an organic acid metal salt For this purpose, the content of alkali metals and alkaline earth metals in the form of metal salts of organic acids in the crude oil feed, wherein the content of alkali metals and alkaline earth metals in the form of metal salts of organic acids is determined by ASTM method D1318. The present invention also provides a method for producing crude oil products. Which includes: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25 t: and 0.1 (1 MPa), and the crude oil feed is A gram of crude oil feed has a total Ni / V / Fe content of at least 20000 grams, and the at least one catalyst contains at least 0.001 grams of column 6 of the periodic table per gram of catalyst based on the weight of the metal. One or more metals, one or more compounds of one or more metals in column 6 of the periodic table, or a mixture thereof, and controlling the contact conditions so that the liquid space in the contact zone Of ultra over-10 h, and the crude product that has a total Nj / v / Fe content of at most of the crude feed Ni / V / Fe content, wherein Ni / V / Fe content is measured by ASTM-based method D5708. The present invention also provides a method of producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is at 25. (: And 0-101 MPa is a liquid mixture, the crude oil feed has at least 0.0001 grams of milk δ & in each gram of crude oil feed has at least 0.001 gram of sulfur The at least one catalyst comprises one or more metals in the sixth table of the weekly table of 2005200533737, one or more compounds of one or more metals in column 6 of the periodic table, or a mixture thereof; and controlling the contact conditions so that the crude oil product The oxygen content of the crude oil feed having an oxygen content of up to 90% and the crude product has a sulfur content of the crude oil feed having a sulfur content of 70 to 130%, wherein the oxygen content is borrowed It is determined by ASTM method E3 85, and the sulfur content is measured by ASTM method D4294. The present invention also provides a method for producing a crude oil product, which comprises contacting a crude oil feed with one or more catalysts to produce a total crude oil product-containing product. Product, wherein the crude oil product is a liquid mixture at 25 ° C and 0.101 MPa, and the crude oil feed has a total Ni / V / Fe content of at least 20,000 g per gram of crude oil feed, and a sulfur content At least 0.0001 grams of sulfur, the at least one catalyst comprising One or more metals in column 6 of the table, one or more compounds of one or more metals in periodic table 6, or mixtures thereof; and controlling the contact conditions so that the crude oil product has a total Ni / V / Fe content of up to 9 0% of the Ni / V / Fe content of the crude oil feed, and the crude oil product has a sulfur content of 70 to 130% of the crude oil feed, including Ni / V / Fe The content is determined by ASTM method D5708, and the sulfur content is determined by A $ TM method D4294. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a content containing The total product of a crude oil product, wherein the crude oil product is a liquid mixture at 25 ° C and 0.101 MPa, and the crude oil feed contains one or more metallographic salts of one or more organic acids, and one or more alkaline earths of one or more organic acids. Metal salt, or a mixture thereof, the crude oil feed has at least 0.00001 grams of organic acid metal per gram of crude oil feed 27 200533737 total alkali metal and alkaline earth metal content in salt form and a residue content of at least 〇. Substance, the at least one catalyst One or more metals comprising column 6 of the periodic table, one or more compounds of one or more metals of column 6 of the periodic table, or a mixture thereof; and controlling the contact conditions so that the crude oil product has an organic acid metal salt in the form of an alkali metal And alkaline earth metal content of up to 90% of the organic acid metal salt form of the alkali metal and alkaline earth metal content in the crude oil feed, and the crude oil product has a residue content of 70 to 130% of the crude oil feed. Residue content, in which the content of alkali metals and alkaline earth metals in the form of metal salts of organic acids is determined by ASTM method d 1 3 1 8 and the content of residues is determined by ASTM method D5307. The invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is at 25 ° C. and 0.1 MPa Liquid mixture, the crude oil feed has a residue content of at least 0.01 g per gram of crude feed, a total Ni / V / Fe content of at least 0.00002 g, and the at least one catalyst comprises the sixth block of the periodic table One or more metals, one or more compounds of one or more metals of the Periodic Table, or mixtures thereof; and controlling the contact conditions so that the crude oil product has a total Ni / V / Fe content of up to 90%的 The Ni / V / Fe content of the crude oil feed, and the crude product has a residue content of 70 to 130% of the crude feed, wherein the Ni / V / Fe content is determined by ASTM method D5708 , And the residue content is measured by ASTM method D5307. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing the crude oil product, 28 200533737 wherein the crude oil product is a liquid mixture at 25 ° C and 0.101 MPa The crude oil feed contains one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or a mixture thereof. The crude oil feed has at least 0 per gram of crude oil feed. . 丨 gram of vacuum gas oil ("VGO") content, 0.0001 grams of the total content of alkali metals and alkaline earth metals in the form of metal salts of organic acids, the at least one catalyst containing one or more metals in the sixth table of the periodic table, the periodic table One or more compounds of one or more metals in column 6, or mixtures thereof; and the crude oil feed that controls the contact conditions so that the crude oil product has an organic acid metal salt in the form of a total alkali metal and alkaline earth metal content of up to 90% Alkali metal and alkaline earth metal content in the form of a metal salt of an organic acid, and the crude oil product has a VG0 content of 70 to 130% of the VG0 content of the crude oil feed, which VG〇 Method D5 307 astm content-based assay, by the alkali metal salt of an organic acid and alkaline earth metal content of morphology-based assay by ASTM Method D1 3 1 8. The present invention also provides a method of producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is at 25. . And a liquid mixture at 0 · 101 MPa, the crude oil feed has a total Ni / V / Fe content of at least 20000 grams per gram of crude oil feed, a VG0 content of at least grams, and the at least one contact The medium contains one or more metals in column 6 of the periodic table, one or more compounds of one or more metals in column 6 of the periodic table, or a mixture thereof; and controlling the contact conditions so that the crude oil product has a total Ni / V / Fe content The Ni / V / Fe content of the crude oil feed is at most 90%, and the crude oil product has a VG0 content of the crude oil feed with a vg0 content of 70 to 130%, of which VG0 contains 29 200533737 Hunting was measured by the AS TM method η $ 1 η 7 and BI — 5307, and the Ni / v / Fe content was measured by the ASTM method D5708. The present invention also provides a method for producing 焉, 吝, and 吝 京 Beijing oil products, which includes: crude oil feed and one or more technologies to produce a total product of crude oil products, wherein the crude oil product in 2 5 ° Γ and η 1 m μ η ϋ and 0.101 Mpa is a liquid mixture, the crude oil feed contains one or more plug-in fresh from one or more alkali metal salts of organic compounds, one or more One or more insertions of various organic acids ^ Feixi alkaline earth metal salt, or a mixture thereof, the crude oil feed is in each gram of crude oil feed and the Gu 5 Bu Shi 1 * leaf tincture has at least 0.0001 grams of organic acid metal salt The total content of metal and soil in the form of the test, the at least one catalyst can be obtained by the following: the carrier and one or more metals in column 6 of the periodic table, Or more compounds, or mixtures thereof, to produce a catalyst precursor, heating the catalyst precursor at a low & 40 ° C in the presence of one or more sulfur-containing compounds to form a catalyst; and controlling contact conditions to read Give the crude oil product an alkali metal in the form of a rhyme metal salt The total content of alkaline earth metal up to 9〇% of the crude feed with a metal salt of organic acid alkali metal and alkaline earth metal content form, wherein the organic acid metal

屬鹽形態的鹼金屬和鹼土金屬含量係藉由ASTM法BUM 測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25Ϊ：和0.101 MPa下為液態混合物，該 原油進料在每克原油進料中具有至少〇 〇〇〇〇2克的i Ni/V/Fe含量，該至少一種觸媒可藉由下列獲得：使載體 與週期表第6攔的一或多種金屬，週期表第6攔之一或多 30 200533737 種金屬的一或多種化合物，或其混合物結合以產生觸媒前 ： 驅物，於一或多種含硫化合物存在下，在低於4〇〇它的溫 度下加熱此觸媒前驅物形成觸媒；及控制接觸條件以便使 該原油產物具有總Nl/V/Fe含量最多為9〇%之該原油進料 的Ni/V/Fe §畺，其中Ni/v/Fe含量係藉由ASTM法D5708 測定。 本發明亦提供在每克原油組成物中含有下列者的原油 組成物：至少0.001克之沸程分佈在〇1〇1 MPa下介於95 C和26〇 C之間的烴；至少0·001克之彿程分佈在〇 1〇1 Mpa籲 下介於260°C和320°C之間的烴；至少0·001克之沸程分佈 在0_101 MPa下介於32(^和65(TC之間的烴；以及在每克 原油產物中含有大於〇克，但小於〇〇1克的一或多種觸媒。 本發明亦提供在每克原油組成物中含有下列者的原油 組成物：至少〇·〇1克的硫，其藉由ASTM法D4294測定； 至少0·2克的殘留物，其藉由ASTM法D5307測定，該組 成物具有至少1.5之MCR含量與C5瀝青質含量的重量比， 其中MCR含量係藉由ASTM法D4530測定，C5瀝青質含 籲 量係藉由ASTM法D2007測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中該原油產物在25°C和0.101 MPa下可冷凝，該原油進 料在每克原油進料中具有至少〇·〇〇1克的MCR含量，該至 少一種觸媒可藉由下列獲得：使載體與週期表第6欄的一 或多種金屬’週期表第6攔之一或多種金屬的一或多種化 31 200533737 合物，或其混合物結合以產生觸媒前驅物；於一或多種含 硫化合物存在下，在低於50(rc的溫度下加熱此觸媒前驅 物形成觸媒；及控制接觸條件以便使該原油產物具有McR 含量最多為90%之該原油進料的MCR含量，其中mcr含 量係藉由ASTM法D4530測定。 本發明亦提供生產原油產物之方法，其包括··使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其中该原油產物在25 °C和〇· 1 〇 1 MPa下可冷凝，該原油 進料在母克原油進料中具有至少〇 〇〇1克的MCR含量，該 至少一種觸媒具有中位孔徑在7〇人至18〇人之範圍内的孔 徑分佈’該孔徑分佈中至少6〇%的總孔數具有在45 a之 中位孔徑範圍内的孔徑，其中孔徑分佈係藉由ASTM法The contents of alkali metals and alkaline earth metals in the form of salts are determined by ASTM method BUM. The invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25 ° C and 0.101 MPa, and the crude oil is The feed has an i Ni / V / Fe content of at least 20000 grams per gram of crude feed, and the at least one catalyst can be obtained by: the carrier and one or more of the sixth block of the periodic table Metals, one or more 30 200533737 metals of one or more compounds of the Periodic Table, or mixtures thereof to produce catalysts: Precursors, in the presence of one or more sulfur compounds, at less than 400. Heating the catalyst precursor at its temperature to form a catalyst; and controlling the contact conditions so that the crude oil product has Ni / V / Fe of the crude oil feed with a total Nl / V / Fe content of up to 90% § 畺, The Ni / v / Fe content is determined by ASTM method D5708. The present invention also provides a crude oil composition containing per gram of crude oil composition: at least 0.001 g of a hydrocarbon having a boiling range distribution between 95 C and 26 ° C. at 0.001 MPa; at least 0.001 g of Buddhist process distribution of hydrocarbons between 260 ° C and 320 ° C at 010 MPa; at least 0.001 g of boiling range distribution of hydrocarbons between 32 (^ and 65 (TC) at 0_101 MPa And one or more catalysts per gram of crude oil product, but less than 0.001 grams. The present invention also provides a crude oil composition containing the following in each gram of crude oil composition: at least 0.001 Grams of sulfur, determined by ASTM method D4294; at least 0.2 grams of residue, measured by ASTM method D5307, the composition has a weight ratio of MCR content to C5 asphaltene content of at least 1.5, where MCR content It is determined by ASTM method D4530, and the C5 asphaltene content is determined by ASTM method D2007. The present invention also provides a method for producing a crude oil product, which comprises: contacting a crude oil feed with one or more catalysts to produce crude oil containing Total product of the product, where the crude product is condensable at 25 ° C and 0.101 MPa The crude feed has an MCR content of at least 0.001 grams per gram of crude feed, and the at least one catalyst can be obtained by combining the carrier with one or more metals in the column 6 of the periodic table. One or more compounds of one or more metals in the sixth block 31 200533737, or a combination thereof to produce a catalyst precursor; in the presence of one or more sulfur-containing compounds, heat this at a temperature below 50 (rc) The catalyst precursor forms a catalyst; and controls the contact conditions so that the crude oil product has an MCR content of the crude oil feed with a McR content of up to 90%, where the mcr content is determined by ASTM method D4530. The present invention also provides the production of crude oil A method of producing a product comprising contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is condensable at 25 ° C and 0.11 MPa, and the crude oil is fed The at least one catalyst has a MCR content of at least 0.001 grams in the mother gram crude feed, and the at least one catalyst has a pore size distribution with a median pore size ranging from 70 to 180 people. The pore size distribution is at least 60. % Of total holes Pore sizes in the range of 45 a median pore size, where the pore size distribution is determined by the ASTM method

D4282測定；及控制接觸條件以便使該原油產物具有McR 最多為90。/〇之該原油進料的MCr，其中MCR係藉由ASTM 法D4530測定。 本發明亦提供在每克組成物中含有下列者的原油組成 物·最多0.004克的氧，其藉由ASTM法E385測定；最 多0.003克的硫，其藉由ASTM法D4294測定；及至少0.3 克的殘留物，其藉由ASTM法D5307測定。 本發明亦提供在每克組成物中含有下列者的原油組成 物：最多0.004克的氧，其藉由ASTM法E385測定；最 多0.003克的硫，其藉由ASTM法D4294測定；最多0.04 克的驗性氮’其藉由ASTM法D2896測定；至少0.2克的 殘留物’其藉由ASTM法D5307測定；及該組成物具有最 32 200533737 多為0.5的TAN，其藉由ASTM法D664測定。 ： 本發明亦提供在每克組成物中含有下列者的原油組成 物：至少0.001克的硫，其藉由ASTM法D4294測定；至 少〇·2克的殘留物，其藉由ASTM法D5307測定；該組成 物具有至少1.5之MCR含量與c5瀝青質含量的重量比， 及该組成物具有最多為〇·5的TAN，其中TAN係藉由ASTM 法D664測定，MCR的重量係藉由ASTM法D4530測定， 而C5瀝青質的重量係藉由ASTM法D2007測定。 於若干具體實例中，本發明與結合本發明之一或多種 籲 方法或組成物者亦提供下列原油進料：（a)尚未於精煉廉 中處理，蒸餾及/或分餾者；（b)含有碳數大於4之成分者， 该原油進料在每克原油進料中含有至少〇 · 5克的這類進 料；（c)包含烴，其部分具有：在0.101 MPa下低於100°C 的沸程分佈，在〇·1〇1 MPa下介於l〇〇°C和200°C之間的沸 程分佈，在0.101 MPa下介於200°C和3 00°C之間的沸程分 佈，在0.101 MPa下介於300°C和400°C之間的沸程分佈， 以及在0.101 MPa下介於400°C和650°C之間的沸程分佈； · (d)在每克原油進料中含有至少：o.ooi克之具有沸程分佈 在0.101 MPa下低於l〇(TC的烴，0.001克之具有沸程分佈 在0.101 MPa下介於l〇〇°C和200°C之間的烴，0.001克之 具有沸程分佈在0.101 MPa下介於200°C和300。(：之間的 烴，0.001克之具有沸程分佈在〇.1〇1 MPa下介於300°C和 400°C之間的烴，及o.ooi克之具有沸程分佈在0.101 MPa 下介於400°C和650°C之間的烴；（e)具有至少為0.1，至 33 200533737 少為0.3’或是在〇·3至20’ 〇.4至1〇，或〇.5至5之範圍 内的TAN ; (f)具有在0.101 MPa下至少為20(rc的起始 沸點；（g)包含鎳、飢和鐵；（h)在每克原油進料中含有 至少0.00002克的總Ni/V/Fe ;⑴包含硫；⑴在每克原 油進料中含有至少0.0001克或〇·〇5克的硫；（k)在每克原 油進料中含有至少0.001克的VG0; (1)在每克原油進料 中含有至少〇·1克的殘留物；（m)包含含氧烴；（n) 一或 多種有機酸的一或多種驗金屬鹽，一或多種有機酸的一或 多種鹼土金屬鹽，或其混合物；（0)包含有機酸的至少一 種鋅鹽，及/或（P)包含有機酸的至少一種石申鹽。 於若干具體實例中，本發明與結合本發明之一或多種 方法或組成物者亦提供可藉由移除原油中的石腦油及比石 腦油更具揮發性之化合物而得到的原油進料。 於若干具體實例中，本發明與結合本發明之一嘎多種 方法或組成物者亦提供使原油進料與一或多種觸媒接=以 生產含有原油產物之總產物的方法，其中該原油進料和原 油產物兩者都具有Cs瀝青質含量和MCR含量，a r、、 、 （a)原 油進料之cs瀝青質含量和原油進料之MCR含量的和為$ 原油產物之C5瀝青質含量和原油產物之MCr含量的和、 S’，控制接觸條件以便使s，最多為99%的S;及/或（b)為 制接觸條件以便使原油產物之MCR含量與原油產物之上 瀝青質含量的重量比在1.2至2·0,或u至19的範園内°。5 於若干具體實例中，本發明與結合本發明之一 、、 、 4多種 方法或組成物者亦提供氫源，其中該氫源為：（a)氣態·（匕） 34 200533737 氫氣；⑷甲貌’·⑷輕烴；⑷惰性氣體；及/或⑺其 混合物。 於若干具體實例中，本發明與結合本發明之一或多種 方法或組成物者亦提供使原油進料與—或多種觸媒接觸以 生產含有原油產物之總產物的方法’其中該原油進料在位 於或連接到近海設備的接觸區中進行接觸。 於若干具體實例中，本發明與結合本發明之一或多種 方法或組成物者亦提供一種方法，其包含於氣體及/或氫源 存在下，使原、；由進料與一或多#觸媒接觸及控制接觸條件 # 以便使：⑷氣態氫源與原油進料的比在與一或多種觸媒 接觸之每立方米的原油進料中為5至8〇〇標準立方米之氣 態氫源的範m·⑻藉自改、變氫源分壓以控制氯的選定 淨吸取率；（c)氫的吸取率使原油產物具有小於〇·3的 TAN，但氫的吸取係小於在接觸期間會導致原油進料和總 產物之間實質上相分離的氫吸取量；（d)氳的選定吸取率 在每立方米的原油進料中為丨至30或丨至8〇標準立方米 之氫源的範圍内，（e)氣體及/或氫源的液體空間速度至少 籲 為11 h-ι，至少為15 或最多為2〇 h-1;⑺在接觸期 間控制氣體及/或氫源之分壓；（g)接觸溫度在5〇至5〇〇χ： 的範圍内，氣體及/或氫源的總液體空間速度在〇 ·丨至3 〇 1的範圍内，氣體及/或氫源的總壓力在1 ·〇至2〇 MPa的範 圍内；（h)氣體及/或氫源的流動係朝著與原油進料流動相 反的方向；（i)該原油產物具有H/C為70至i 3〇%之該原 油進料的H/C ; (j)由該原油進料吸取的氫在每立方米的 35 200533737 原油進料中最多為8〇及/或1 S 8。或1至50標準立方米 之氫的範圍内，（k)該原油產物具有總Ni/V/Fe含量最多 為9〇%’取多為50%’或最多為10%之該原油進料的Ni/V/Fe έ i (1) 4原油產物具有硫含量為7〇至13〇%或至 之該原油進料的硫含(m)肖原油產物具有v⑻含量 為7〇入至13〇%或90至110%之該原油至130%或9進料的 VG〇含里，（n)該原油產物具有殘留物含量為7〇〇至i 1〇% =該原油進料的殘留物含量；（〇)該原油產物具有氧含量 2為90%，最多為7〇%，最多為5〇%，最多為4〇%，或 取夕為10%之該原油進料的氧含量；該原油產物具有 有機魷金屬鹽形態的鹼金屬和鹼土金屬總含量最多為 9〇%’取多為5G%，或最多a 1()%之該原油進料的有機酸 金屬鹽形態的鹼金屬和鹼土金屬含量；⑷在接觸期間， 該原油進料的P值至少為15;⑴該原油產物具有在37.8 °ct的黏度最多為9G%，最多為·，或最多& ι〇%之該 原油進料纟37.rc下的黏度；(s"亥原油產物具有趟比 重為70至13〇%之該原油進料的Αρι比重；及/或⑴該 2油產物具有TAN最多為90%，最多為5〇%，最多為3〇%， 最多為20%，或最多為1〇%之該原油進料的tan及/或在 0.001至0.5，〇.〇1至〇.2，或〇 〇5至〇1的範圍内。 於若干具體實例中，本發明與結合本發明之一或多種 方法或組成物者亦提供一種方法，其包含使原油進料與一 或=種觸媒接觸及控制接觸條件以減少含有機氧化合物的 3里，其中.（a)減少選定有機氧化合物的含量以便使該 36 200533737 原油產物具有含氣I I & 入士 最為90〇/〇之該原油進料的人g旦· 含有機氧化合物的至少一鍤人^ ^ 十的3虱里，（b) 八士， 種化合物包含羧酸之全屬_· Μ 含有機氧化合物的至少一插 金屬|，（c) 含有機氧化合物的至少— 双金屬瓜，（d) 趟.^種化合物包含羧酸之鹼土金屬 :’⑷纟有機氧化合物的至少一種化 屬鹽，其中此全屬白杯、闲# 士 匕3竣酉夂之金 ” 期表第12攔的-或多種金屬.m ^油產物具有含錢酸有機化合物含量最多 原油進料中的含非缓酸有機化合物含量；及蜮⑻ =料中的至少-種含氧化合物係產自 料酸 的有機氧化合物。 馱次非羧i 於若干具體實例中，本發明盥έ士人 a，、、、、口 口本發明之一或多種 7組成物者亦提供_種方法，其包含使原油進料與一 或夕種觸媒接觸，其中：⑷第一、、w 料 弟皿度下，使該原油進 科〜至少一種觸媒接觸，接著 _ 第一溫度下接觸，控制接 L =便使第-接觸溫度至少低於第二接觸溫度3〇。。； ()於第一氫吸取條件下缺接A | Μ 1术旰卜然後在第二氫吸取條件下，使該 ，油進料與氫接觸’第一吸取條件的溫度係至少低於第二 °取條件的溫度30 C，⑷於第_溫度下，使該原油進料 ”至少-種觸媒接觸，接著於第二溫度下接觸，控制接觸 條件以便使第-接觸溫度最多低於第二接觸溫度2G(rc;⑷ 在接觸期間產生氫氣；（e)在接觸期間產生氫氣，並且控 制接觸條件以便使該原油進料吸取至少一部分的生成氫；（〇 ^該原油進料與第一和第二種觸媒接觸，該原油進料與第 一種觸媒的接觸生成初原油產物，其中此初原油產物具有 37 200533737 Π進最二Γ%之該原油進料的叫 口口 Τ進订接觸； 該原油進料在與一或多觸媒應^中進订接觸；⑴使 該-或多種觸媒為_婵：=後與附加觸媒接觸’·⑴ 觸之後、 料在與該叙觸媒接 曼於風源存在下與附加觸媒 方米原油進料42〇俨進古士丄 ^風係以母立 如^ Μ軚準立方米之範圍内的速率產生；⑴ 在接觸期間產生氫，於氧俨“， 《半屋生，(1) 下，蚀# K、、 孔體和至少一部分生成氫的存在 Μ原油進料與附加觸嬋 # # ^ Α ϋ 觸琛接觸，並且控制接觸條件以 更使乳體〜動朝著與原油 ^ ^ 才机動和生成虱流動相反的方 σ ,()使該原油進料於第一、、w 於第二π译π我 /皿度下與釩觸媒接觸，隨後 /皿又”附加觸媒接觸，控制接觸條件以便使第一 h度至少低於第二溫 ,,_ ^ 0 C，（n)在接觸期間產生氫氣， 使该原油進料與附加觸飞乳 ήυ m^rn ^ 7, I 控制接觸條件以便使該附 产使 〉、一部分的生成氫，·及/或（〇)隨後於第二溫 第二進料與附加觸媒接觸， 罘一 /皿度至少為1 8 0 °C。 於若干具體實例中，本發 月、、Ό a本發明之一或多種 方法或組成物者亦提供一種 或多種觸媒接m⑷^，、^使原油進料與一 含氣 （）°亥觸媒為党載觸媒而載體包 化鎂，或其混合物，.(b)兮觸::：氧化欽、氧化錯、氧 H · , 、 , ^ μ觸媒為文載觸媒而載體為多孔 ’⑷此方法尚包括在硫化前已在高於彻。C之溫 處理過的附加觸媒；W該至少一種觸婵里又 玍· a 、 種觸嫖的哥命至少為0.5 ，$ e該至少一種觸媒係於固定床中或懸浮於原 38 200533737 油進料中。 於若干具體實例中，本發明與結合本發明之一或多種 方法或組成物者亦提供一種方法，其包含使原油進料與一 或多種觸媒接觸，該至少一種觸媒為受載觸媒或塊狀金屬 觸媒’該受載觸媒或塊狀金屬觸媒：⑷&含週期表第5 至10欄的-或多種金屬，週期表第5至1〇攔之—或多種 金屬的-或多種化合物，或其混合物；⑻在每克觸媒中 含有至少0·0001克’ 0.0001至0·6克，或0.001至〇 3克 之·週期表第5至10攔的一或多種金屬，週期表第5至W 2之一或多種金屬的一或多種化合物，或其混合物；（匀包 各週期表第6至1G攔的-或多種金屬，週期表第6至1〇 2之一或二種金屬的一或多種化合物，或其混合物；（d)包 3週期表第7至1G攔的-或多種金屬，週期表第7至1〇 攔之一或多種金屬的一或多種化合物，或其混合物；（ ^克觸媒中含有至0.6克或0·_至0.3克之：週 月表第7至1〇攔的_或多種金屬，週期表第7至^ —或多種金屬的-或多種化合物，或其混合物；（f 週期表第5至6搁的一或多種金屬，週期表第5至6棚 一或多種金屬的-或多種化合物，或其混合物 ^ =期表第—5攔的-或多種金屬，週期表第5攔之-或^ | ^多種化合物，或其混合物；(h)在每克觸媒中 :；\·0001 克，〇·_ 至 〇·6 克，0.001 至 0.3 克，〇〇〇5 金I1 _或〇 〇1至〇·08克之：週期表第5攔的-戈多種 金屬，週期…搁之一或多種金屬的一或多種化=種 39 200533737 或其混合物；⑴包含週期 6 弟6攔的一或多種金屬，週 物: 一或多種金屬的-或多種化合物，或其混合 :勿，=母克觸媒中含有。._至〇6克，_至。3 ^種全/0.1克，G.G1至謂克之週期表第6欄的一 或多種金屬，週期矣筐& _ ^ 、 ’ 攔之一或多種金屬的一或多種化 口物、或其此合物’（k)包含週期表第1G攔的-或多種金 屬’週期表第1〇_之_或多種金屬的—或多種化合物， 或其此口物’⑴在每克觸媒中含有G·咖i至。6克或〇術 至〇·3克之·週期表第1〇攔的一或多種金屬，週期表第⑺ 搁之或多種金屬的一或多種化合物，或其混合物»包 3釩 &多種釩化合物，或其混合物；⑻包含鎳，一 或多種錄化合物’或其混合物；（〇)包含鈷，一或多種鈷 化口物’或其混合物；（p)包含鉬，一或多種鉬化合物， 或其混合物；（q)在每克觸媒中含有〇〇〇1至〇·3克或〇 〇〇5 至〇· 1克的：姻’ 一或多種鉬化合物，或其混合物；（Γ)包 3嫣’ 一或多種鎢化合物，或其混合物；在每克觸媒 中含有0.001至0.3克的··鎢，一或多種鎢化合物，或其 混合物；（t)包含週期表第6攔的一或多種金屬和週期表 第10攔的一或多種金屬，其中第10攔金屬與第6欄金屬 的莫耳比為1至5，（u)包含週期表第15欄的一或多種元 素，週期表第15攔之一或多種元素的一或多種化合物， 或其混合物；（V)在每克觸媒中含有〇 〇〇〇〇1至〇 〇6克之： 週期表第1 5欄的一或多種元素，週期表第丨5欄之一或多 種凡素的一或多種化合物，或其混合物；磷，一或多 40 200533737 ’（X)在每克觸媒中含有最多0.1 在每克觸媒中含有至少0.5的Θ 種磷化合物，或其混合物 克的α氧化鋁；及/或（y) 氧化紹。 於若干具體實例中，本發明盥社人士政 + S咧興結合本發明之一或多考| 方法或組成物者亦提供形成觸 取啁琛之方法，其包括使載體輿 一或多種金屬結合以形成載护/全厘 7取戰體/金屬混合物，其中該載體包 含Θ氧化铭，於至少 、 L的，皿度下熱處理Θ氧化鋁載體/金 屬混合物，而且尚包括：/古莽 ^ (a)使載體/金屬混合物與水結合 以形成糊狀物，擠壓此棚此輪· /U、, ^ 併至此糊狀物，（b)於至少800°C的溫度 下藉由熱處理氧化鋁而得到θ氣化4 乳化鋁，及/或（^使該觸媒 硫化。D4282 determination; and controlling the exposure conditions so that the crude product has a McR of up to 90. The MCr of this crude oil feed, where the MCR is determined by ASTM method D4530. The present invention also provides a crude oil composition containing the following in each gram of composition: up to 0.004 grams of oxygen, as measured by ASTM method E385; up to 0.003 grams of sulfur, as measured by ASTM method D4294; and at least 0.3 grams Residue as determined by ASTM method D5307. The present invention also provides a crude oil composition containing the following in each gram of composition: up to 0.004 g of oxygen, as measured by ASTM method E385; up to 0.003 g of sulfur, as measured by ASTM method D4294; up to 0.04 g Experiential nitrogen 'was measured by ASTM method D2896; at least 0.2 g of residue was measured by ASTM method D5307; and the composition had a maximum TAN of 32 200533737 and 0.5 as measured by ASTM method D664. : The present invention also provides a crude oil composition containing the following in each gram of composition: at least 0.001 g of sulfur, which is determined by ASTM method D4294; at least 0.2 g of residue, which is determined by ASTM method D5307; The composition has a weight ratio of MCR content to c5 asphaltene content of at least 1.5, and the composition has a TAN of at most 0.5, where TAN is determined by ASTM method D664 and MCR weight is by ASTM method D4530 The weight of C5 asphaltene was measured by ASTM method D2007. In several specific examples, the present invention and those combining one or more of the methods or compositions of the present invention also provide the following crude oil feeds: (a) those that have not been processed in a refinery, distilled and / or fractionated; (b) contain For components with a carbon number greater than 4, the crude oil feed contains at least 0.5 grams of such feeds per gram of crude oil feed; (c) contains hydrocarbons, part of which has a temperature below 100 ° C at 0.101 MPa Boiling range distribution between 0.1 ° C and 200 ° C at 0.101 MPa, boiling range between 200 ° C and 300 ° C at 0.101 MPa Distribution, boiling range distribution between 300 ° C and 400 ° C at 0.101 MPa, and boiling range distribution between 400 ° C and 650 ° C at 0.101 MPa; (d) per gram The crude oil feed contains at least: o.ooi grams of hydrocarbons with a boiling range distribution below 0.10 MPa at 0.101 MPa, 0.001 grams of hydrocarbons with a boiling range distribution between 0.1 ° C and 200 ° C at 0.101 MPa Intermediate hydrocarbons, 0.001 grams have a boiling range distribution between 200 ° C and 300 at 0.101 MPa. (: Hydrocarbons, 0.001 grams have a boiling range distribution between 300 ° C and 400 at 0.101 MPa ° Hydrocarbons between C and o.ooi grams of hydrocarbons having a boiling range distribution between 400 ° C and 650 ° C at 0.101 MPa; (e) having at least 0.1 to 33 200533737 and less 0.3 'or TAN in the range of 0.3 to 20 '0.4 to 10, or 0.5 to 5; (f) has an initial boiling point of 0.1 (MPa) at 0.101 MPa; (g) contains nickel, Starch and iron; (h) contains at least 0.00002 grams of total Ni / V / Fe per gram of crude feed; ⑴ contains sulfur; ⑴ contains at least 0.0001 grams or 0.05 gram of sulfur per gram of crude feed (K) contains at least 0.001 grams of VG0 per gram of crude feed; (1) contains at least 0.1 grams of residue per gram of crude feed; (m) contains oxygenated hydrocarbons; (n) a One or more metal test salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or a mixture thereof; (0) at least one zinc salt comprising an organic acid, and / or (P) an organic acid comprising At least one type of naphtha salt. In some specific examples, the present invention and those who combine one or more methods or compositions of the present invention also provide the ability to remove naphtha from crude oil and more than naphtha. Crude oil feed obtained from volatile compounds. In some specific examples, the present invention and a combination of various methods or compositions of the present invention also provide the crude oil feed with one or more catalysts = to produce containing Method for total product of crude oil product, wherein the crude oil feed and crude oil product both have Cs asphaltene content and MCR content, ar,,, (a) cs asphaltene content of crude oil feed and MCR content of crude oil feed The sum of S is the sum of the C5 asphaltene content of the crude oil product and the MCr content of the crude oil product, S ′, to control the contact conditions so that s is at most 99% of S; and / or (b) are the contact conditions to make the crude oil The weight ratio of the MCR content of the product to the asphaltene content above the crude product is within the range of 1.2 to 2.0, or u to 19. 5 In some specific examples, the present invention and one or more of the methods or compositions of the present invention also provide a hydrogen source, wherein the hydrogen source is: (a) gaseous (dagger) 34 200533737 hydrogen; Appearances: ⑷ light hydrocarbons; ⑷ inert gases; and / or ⑺ mixtures thereof. In several specific examples, the present invention and those combining one or more methods or compositions of the present invention also provide a method of contacting a crude oil feed with—or a plurality of catalysts to produce a total product containing a crude oil product ', wherein the crude oil feed Make contact in a contact zone located or connected to offshore equipment. In a few specific examples, the present invention and those who combine one or more methods or compositions of the present invention also provide a method, which comprises, in the presence of a gas and / or a hydrogen source, the original; from the feed and one or more # Catalyst contact and control contact conditions # In order to make: the ratio of radon gaseous hydrogen source to crude oil feed is 5 to 800 standard cubic meters of gaseous hydrogen per cubic meter of crude oil feed in contact with one or more catalysts The range of the source m · ⑻ is adjusted by changing the partial pressure of the hydrogen source to control the selected net absorption rate of chlorine; (c) The hydrogen absorption rate makes the crude oil product have a TAN less than 0.3, but the hydrogen absorption system is less than that in contact. The amount of hydrogen uptake that results in substantial phase separation between the crude oil feed and the total product during this period; (d) The selected absorption rate of plutonium is 丨 to 30 or 丨 to 80 standard cubic meters per cubic meter of crude oil feed. Within the range of the hydrogen source, (e) the liquid space velocity of the gas and / or hydrogen source is at least 11 h-ι, at least 15 or at most 20 h-1; ⑺ control the gas and / or hydrogen source during contact Partial pressure; (g) contact temperature in the range of 50 to 500 ×: of gas and / or hydrogen source The space velocity of the liquid is in the range of 0.1 to 3.0, and the total pressure of the gas and / or hydrogen source is in the range of 1.0 to 20 MPa; (h) the flow of the gas and / or hydrogen source is toward The direction opposite to the flow of the crude oil feed; (i) the crude oil product has an H / C of 70 to i 30% of the H / C of the crude oil feed; (j) hydrogen absorbed by the crude oil feed per cubic meter The maximum of 35 200533737 crude oil feed is 80 and / or 1 S 8. Or within the range of 1 to 50 standard cubic meters of hydrogen, (k) the crude oil product has a total Ni / V / Fe content of up to 90%, 'take up to 50%' or up to 10% of the crude feed Ni / V / Fe i (1) 4 The crude oil product has a sulfur content of 70 to 130%, or the sulfur-containing (m) of the crude oil feed has a sulfur content of 70% to 13%. Or 90 to 110% of the crude oil to 130% or 9 VG0 feed, (n) the crude oil product has a residue content of 700 to i 10% = the residual content of the crude oil feed; (0) The crude oil product has an oxygen content of 90%, a maximum of 70%, a maximum of 50%, a maximum of 40%, or an oxygen content of 10% of the crude oil feed; the crude product The total content of alkali metals and alkaline earth metals in the form of organic squid metal salt is at most 90%, which is more than 5G%, or at most a 1 ()% of the alkali metal and alkaline earth metals in the form of organic acid metal salts of the crude oil feed. Content; ⑷ the P value of the crude oil feed during contact is at least 15; ⑴ the crude oil product has a viscosity at 37.8 ° ct of at most 9G%, at most ·, or at most & 5% of the crude feed纟 37. viscosity at rc; (s " Hai crude oil product has a specific gravity of 70% to 130% of the crude oil feed; and / or the 2 oil product has a TAN of at most 90% and at most 50%, The tan of the crude oil feed is at most 30%, at most 20%, or at most 10% and / or in the range of 0.001 to 0.5, 0.001 to 0.2, or 0.05 to 0.01. In some specific examples, the present invention and a combination of one or more methods or compositions of the present invention also provide a method comprising contacting a crude oil feed with one or more catalysts and controlling the contact conditions to reduce the content of organic compounds. 3 of the oxygen compounds, of which. (A) reduce the content of selected organic oxygen compounds so that the 36 200533737 crude oil product has gas content II & 90% of the crude oil feed. At least one person of oxygen compounds ^ ^ Ten of the three lice, (b) eight species, compounds containing all carboxylic acids _ M at least one metal containing organic oxygen compounds |, (c) containing organic oxygen compounds At least — bimetallic melon, (d) trips. ^ Compounds of alkaline earth metals containing carboxylic acids: '⑷ 纟 organic At least one of the compounds is a salt, all of which belong to Baibei, Xian # 士 匕 3 完 酉 夂 金 ”in the 12th table of the schedule-or more metals. M ^ oil products have the highest content of organic compounds containing lenic acid crude oil The content of non-latent acid-containing organic compounds in the feed; and 蜮 ⑻ = at least one oxygen-containing compound in the feed is an organic oxygen compound produced from the feed acid. 驮 次 非 carboxyi In several specific examples, the present invention Scholars a ,,,,, and one or more of the seven components of the present invention also provide a method, which comprises contacting the crude oil feed with one or more catalysts, wherein: Under the degree of contact, the crude oil is brought into contact with at least one catalyst, and then contacted at the first temperature, and the control contact L = makes the first contact temperature at least lower than the second contact temperature by 30. . () Missing A | M1 under the first hydrogen absorption condition and then bringing the oil feed into contact with hydrogen under the second hydrogen absorption condition. The temperature of the first absorption condition is at least lower than the second ° Take the condition temperature 30 C, let the crude oil feed "at least one catalyst contact at the first temperature, and then contact at the second temperature, control the contact conditions so that the first contact temperature is lower than the second Contact temperature 2G (rc; 产生 generates hydrogen during the contact; (e) generates hydrogen during the contact, and controls the contact conditions so that the crude oil feed absorbs at least a portion of the generated hydrogen; (0 ^ the crude oil feed and the first and The second catalyst is contacted. The contact between the crude oil feed and the first catalyst generates an initial crude oil product, wherein the initial crude oil product has 37 200533737 Π, which is the second most Γ% of the crude feed. Contact; the crude oil feed is in contact with one or more catalysts; make the-or multiple catalysts be _ =: = after contact with additional catalysts; In the presence of a wind source, the catalyst was fed 42 square meters of crude oil with additional catalyst. The wind of the Jinshi 丄 系 system is generated at a rate in the range of ^ M 軚 quasi-cubic meters; 产生 generates hydrogen during the contact, in oxygen 俨 ”,“ Half House, (1), Eclipse # K, The presence of pores and at least a portion of the generated hydrogen. The crude oil feed is in contact with additional contact ## ^ Α 触 contact, and the contact conditions are controlled so that the milk body moves toward the crude oil and moves to produce lice. The opposite side, σ, () makes the crude oil feed at the first and second contact with the vanadium catalyst at the second π I / plate degree, and then "addition of the catalyst" contact, control the contact conditions so that The first h degree is at least lower than the second temperature, _ ^ 0 C, (n) Hydrogen is generated during the contact, so that the crude oil feed and additional contact milk m rn ^ 7, I control the contact conditions so that the The by-products are produced, part of the hydrogen is generated, and / or (〇) is then contacted with the additional catalyst at the second temperature and the second feed, at a temperature of at least 180 ° C. In several specific examples This month, one or more of the methods or compositions of the present invention also provide one or more catalysts to connect m⑷ ^ ,, ^ to feed crude oil A gas-containing catalyst is a party-supported catalyst and the carrier contains magnesium, or a mixture thereof. (B) Xiqiao ::: Oxidation, oxidation, oxygen H ·,,, ^ μ The catalyst is The catalyst is contained in the text and the carrier is porous. This method also includes an additional catalyst that has been treated at a temperature higher than that before vulcanization; the at least one catalyst is also a. The life is at least 0.5, the at least one catalyst is in a fixed bed or suspended in the original 38 200533737 oil feed. In several specific examples, the present invention and one or more methods or compositions of the present invention are also combined. Provide a method comprising contacting a crude oil feed with one or more catalysts, the at least one catalyst being a supported catalyst or a bulk metal catalyst 'the loaded catalyst or a bulk metal catalyst: ⑷ & containing -Or more metals in columns 5 to 10 of the periodic table, or 5-10 of the periodic table-or more of the metals-or compounds, or mixtures thereof; 含有 contains at least 0 · 0001 g per gram of catalyst ' 0.0001 to 0.6 grams, or 0.001 to 0.3 grams of one or more metals in the 5th to 10th periodic table, 5th in the periodic table W 2 one or more compounds of one or more metals, or a mixture thereof; (all or more of the metals listed in Periods 6 to 1G of the periodic table-one or more metals, one or two of the Periodic Tables of one or two metals Or one or more compounds, or mixtures thereof; (d) one or more compounds of one or more metals of Groups 7 to 10 of the Periodic Table, or mixtures thereof; ^ Grams of catalyst contains up to 0.6 grams or 0 · _ to 0.3 grams: _ or more metals from the 7th to 10th of the weekly table, 7 to ^-or more metals-or more compounds, or Mixtures; (f one or more metals from 5 to 6 of the Periodic Table, one or more metals-or more compounds from Shelf 5 to 6 of the Periodic Table, or mixtures thereof ^ =-5 or more of the Periodic Table-or more metals ,-Or ^ | ^ multiple compounds of the periodic table, or mixtures thereof; (h) in each gram of catalyst: \ · 0001 grams, 〇 · ~ to 0.6 grams, 0.001 to 0.3 grams, 〇 〇〇5 gold I1 _ or 〇001 to 〇. 08 grams of: the fifth table of the periodic table-Ge a variety of metals, the cycle ... one or more of the metal or more = = 39 200533737 or mixtures thereof; ⑴ Contains one or more metals from the 6th to 6th cycle, weekly: one or more metals-or more compounds, or a mixture thereof: no, = contained in the mother gram catalyst. ._ to 〇6 grams, _ to. 3 ^ all kinds / one or more metals, one or more metals in column 6 of the periodic table from G.G1 to Ug, periodic baskets & _ ^, 'one or more chemical substances of one or more metals, or This compound '(k) contains 1 or more metals of the Periodic Table of the Periodic Table, or one or more of the Metals of the Periodic Table, or multiple compounds, or it's contained in each gram of catalyst. G · Cai to. 6 g or 0 g to 0.3 g of one or more metals in the periodic table, one or more compounds in the periodic table or one or more metals, or mixtures thereof »3 vanadium & multiple vanadium compounds , Or a mixture thereof; (i) containing nickel, one or more compounds' or a mixture thereof; (0) containing cobalt, one or more cobalt compounds, or a mixture thereof; (p) containing molybdenum, one or more molybdenum compounds, or A mixture thereof; (q) containing from 0.001 to 0.3 g or from 0.05 to 0.1 g per gram of catalyst: '' one or more molybdenum compounds, or a mixture thereof; (Γ) package 3 'One or more tungsten compounds, or mixtures thereof; 0.001 to 0.3 g of tungsten per gram of catalyst, one or more tungsten compounds, or mixtures thereof; (t) Or more metals and one or more metals in column 10 of the periodic table, wherein the molar ratio of metal in column 10 to metal in column 6 is 1 to 5, (u) contains one or more elements in column 15 of the periodic table, the period Table 15. One or more compounds of one or more elements, or mixtures thereof; (V) in grams per gram The medium contains 10,000 to 006 g of: one or more elements in column 15 of the periodic table, one or more compounds of one or more vanillin in column 5 of the periodic table, or a mixture thereof; phosphorus , One or more 40 200533737 '(X) contains at most 0.1 per gram of catalyst contains at least 0.5 Θ phosphorus compounds per gram of catalyst, or a mixture of gram alpha alumina; and / or (y) oxidation Shao. In several specific examples, the present invention of the present invention is combined with one or more of the present inventions. The method or composition also provides a method for forming a contact, which includes combining the carrier with one or more metals. In order to form a support / full weight 7 war body / metal mixture, wherein the carrier contains a Θ oxide, heat treatment Θ alumina carrier / metal mixture at a temperature of at least, L, and also includes: / 古 芒 ^ ( a) Combining the carrier / metal mixture with water to form a paste, squeeze this wheel this round / U ,, ^ and to this end, (b) heat treat the alumina at a temperature of at least 800 ° C Then, θ gasified 4 emulsified aluminum is obtained, and / or the catalyst is vulcanized.

於若干具體實例中，本發明與結合本發明之一或多種 方法或組成物者亦提供一種方法，其包含使原油進料盥一 或多種觸媒接觸，其中該一或多種觸媒的孔徑分佈具有：（a) 至少為60人，至少$ 90 A，至少為18〇 A，至少為2〇〇人， 至少為230人，至少為30oA，最多為23〇入，最多為5〇〇人， 或是在 90 至 180 A，100 至 140 A，12〇 至 13〇 A，23〇 至 250 A，180 至 500 A，230 至 500 A ;或 60 至 300 A 之範 圍内的中位孔徑；（b)至少60%的總孔數具有在45A、35a， 或25A之中位孔徑範圍内的孔徑；（c)至少為6〇 m2/g，至 少為90 m2/g，至少為1〇〇 mvg，至少為12〇 m2/g，至少為 150 m2/g，至少為2〇〇 m2/g，或至少為22〇 m2/g的表面積； 及/或（d)至少為0.3 cm3/g，至少為0.4 cm3/g，至少為〇 5 cm3/g ’或至少為0.7 Cm3/g之所有孔徑的總體積。 41 200533737 於若干具體實例中，本發明與結合本發明之一或多種 方法或組成物者亦提供一種方法，其包含使原油進料與一 或多種受載觸媒接觸，#中該載體：⑷包含氧化铭、氧 化矽'氧化矽-氧化鋁、氧化鈦、氧化鉛、氧化鎂，或其混 合物，及/或沸石；（b)包含γ氧化鋁及/或5氧化鋁；在 母克載體中含有至彡0.5克的γ氧化銘；⑷在每克載體中 含有至少0.3克或至少〇·5克的㊀氧化鋁；⑷包含α氧化 鋁、γ氧化鋁、δ氧化鋁、Θ氧化鋁，或其混合物；（f)在每 克載體中含有最多0.1克的(X氧化鋁。 鲁 於若干具體實例中，本發明與結合本發明之一或多種 方法或組成物者亦提供一種釩觸媒：（a)具有中位孔徑至 乂為60A的孔徑分佈；（b)包含載體此載體包含θ氧化 鋁，而該釩觸媒具有中位孔徑至少為60Α的孔徑分佈；⑷ 包含週期表第6攔的一或多種金屬，週期表第6攔之一或 ^種金屬0或多種化合物，或其混合物；及/或⑷在 每克觸媒中含有至少〇.〇〇1克之：週期表第6欄的一或多 種金屬’週期表第6攔之-或多種金屬的—或多種化合物，· 或其混合物。 於若干具體實例中，本發明與結合本發明之一或多種 方法或組成物者亦提供—種原油產物，其具有：⑷最多 為 0.1，—0.001 至 0.5,0.01至0.2;或 〇〇5至 01的_; ()在每克原油產物中最多為〇 ·咖⑼9克之有機酸金屬鹽 形態的驗金屬和驗土金屬；⑷纟每克原油產物中最多為 0.00002克之Ni/V/Fe;及/或（d)在每克原油產物中大於 42 200533737 〇克，但小於〇.01克的至少—種觸媒。 於右干具體實例中，太私Λ 、 、 本1明與結合本發明之一或多種 方法或組成物者亦提供一式客 種有機酸的一或多種驗金屬 鹽’-或多種有機酸的一或多種驗土金屬鹽，或其混合物， 其中：⑷該至少-種驗金屬為鐘、納，或卸；及/或（b)該 至少一種鹼土金屬為鎂或鈣。 於若干具體實例中，本發明與結合本發明之一或多種 方法或組成物者亦提供—種方法，其包含使原油進料與— 或多種觸媒接觸以生產含有原油產物的總產物，此方法尚 包括.⑷使該原油產物與該原油進料相同或不同的原油 結合以形成適用於運輸的摻合物；（b)使該原油產物盘該 原油進料相同或不同的原油結合以形成適用於處理設備的 摻合物"0分餾該原油產物；及蜮⑷使該原油產物 分餾成為-或多種餾分，並且由該至少一種餾分生產運輸 用燃料。 於右干具體實例中，本發明與結合本發明之一或多種 方法或組成物者亦提供一種受載觸媒組成物，其：（a)在 每克載體中含有至少0.3克或至少〇·5克的㊀氧化鋁；在 載體中包含δ氧化鋁；（c)在每克載體中含有最多〇1克的 α氧化鋁；（d)具有中位孔徑至少為23〇人的孔徑分佈；（幻 具有該孔徑分佈之孔至少為〇·3 cmVg或至少為〇7 cmVg 的孔體積；（f)具有至少60m2/g或至少9〇m2/g的表面積； (g)包含週期表第7至1〇攔的一或多種金屬，週期表第7 至10攔之一或多種金屬的一或多種化合物，或其混合物； 43 200533737 (h)包含週期表第5 々夕括人p 爛的一或多種金屬，週期表第5欄之 一或多種金屬的一 古締碰由人士 S夕種化合物，或其混合物；（i)在每 克觸媒巾含有（)·〇⑽ 夕播楚ς柄人 至ϋ.6克或0.001至0·3克之：一或 多種弟5攔金屬，— .... ^ Α 或夕種第5攔金屬化合物，或其混合 物，（J)包含週期表m 圳々々々 弟6攔的一或多種金屬，週期表第6 欄之一或夕種金屬的一夕 — > 或夕種化合物，或其混合物；（k)在 每克觸媒中含有〇·〇〇 υί至0·6克或0·001至0·3克之：一 或多種第6攔金屬，_ 一或夕種第6攔金屬化合物，或其混 合物；（1)包含釩，一武炙 A夕種銳化合物，或其混合物；（m)包 含鉬，一或多種鉬化人輪 匕口物’或其混合物；，（n)包含鎢，一 或多種鎢化合物，或i、、曰人 4具此合物；（0)包含鈷，一或多種鈷 化合物，或其混合物· β κ 物’及/或（p)包含鎳，一或多種鎳化 合物，或其混合物。 於若干具體實例中，本發明與結合本發明之一或多種 方法或組成物者亦提供一種原油組成物，其：（a)具有最 多為1，最多為0.5，最多為〇·3，或最多為〇1的TAN ;⑻ 在每克組成物中含有至少〇·_克之沸程分佈在請i Mpa _ 下介於95°C和260°C之間的烴；至少〇 001克，至少〇 〇〇5 克，或至少0.01克之沸程分佈在〇·1〇1 MPa下介於26(rc 和320°C之間的烴；及至少0.001克之沸程分佈在〇.1〇1 Mpa 下介於320°C和650°C之間的烴；（c)在每克組成物中含有 至少0.0005克的鹼性氮；（d)在每克組成物中含有至少 0·001克或至少〇·〇1克的總氮量；及/或（e)在每克組成 物中含有最多0.00005克的總鎳和釩量。 44 200533737 於若干具體實例中，本發明與結合本發明之一或多種 方法或組成物者亦提供一種原油組成物，其包含一或多種 觸媒，該至少一種觸媒：（a)具有中位孔徑至少為i8〇a， 最多為500 A，及/或在90至18〇 A，1〇〇至14〇 A，12〇 至130 A的孔徑分佈；⑻具有至少9〇 A的中位孔徑，該 孔徑分佈中有超過60%的總孔數具有在45人、35入，或乃入 之中位孔徑範圍内的孔徑；⑷具有至少1〇〇至少 "一，或至少22〇Α的表面積；⑷包含載體；該 ㈣含氧化銘、氧化石夕、氧化石夕_氧化紹、氧化鈦、氧化 在口乳化鎮，/弗石，及/或其混合物；⑷包含週期表第5 =〇欄的-或多種金屬，週期表第5至1()欄之一或多種 多種化合物，或其混合物；(…週期表第5 ’週期表·5攔之-或多種金屬的-或 夕種化合物，或其混合物 0.0001克之：一或夕綠笛 在母克觸媒中含有至少 化人物一夕5攔金屬，-或多種第5攔金屬 化“勿，或其混合物；(h)包 屬 金屬，週期表第6欄之一或多種:表第或多種 或其混合物;⑴在每克觸媒中或多種化合物’ 或多種第6欄金屬，—❹種第3二至少_克之、 合物；⑴包含週期表第丨。欄的屬化合物，或其混 10攔之-或多種金屬的種金屬，週期表第 …含週期表第15二種:^ 攔之一或多種元辛的^, 次夕種兀素，週期表第15 在多種化合物，或其混合物。 在進一步的具體實例中，本發明之特定具體實例的特 45 200533737 徵可和本發明之其他具體實例的特徵結合。例如，本發明： 之-具體實例的特徵可和其他具體實例之特徵結合。 在進一步的具體實例中，原油產物可藉由本文中所述 的任一種方法和系統獲得。 在進一步的具體實例中，附加特徵可加入本文中所述 的特定具體實例。 【實施方式】 在此更詳細地敘述本發明的特定具體實例。本文中所 用的術語定義如下。 · ASTM”係指美國材料試驗標準。In some specific examples, the present invention and a combination of one or more methods or compositions of the present invention also provide a method comprising contacting a crude oil feed with one or more catalysts, wherein the pore size distribution of the one or more catalysts Have: (a) at least 60 people, at least $ 90 A, at least 180A, at least 200 people, at least 230 people, at least 30oA, at most 230 people, and at most 500 people, Or a median aperture in the range of 90 to 180 A, 100 to 140 A, 120 to 130 A, 230 to 250 A, 180 to 500 A, 230 to 500 A; or 60 to 300 A; ( b) at least 60% of the total number of pores have a pore size in the range of 45A, 35a, or 25A median pore size; (c) at least 60m2 / g, at least 90 m2 / g, at least 100mvg A surface area of at least 120 m2 / g, at least 150 m2 / g, at least 200 m2 / g, or at least 22 m2 / g; and / or (d) at least 0.3 cm3 / g, at least The total volume of all pore diameters is 0.4 cm3 / g, at least 0.05 cm3 / g 'or at least 0.7 Cm3 / g. 41 200533737 In several specific examples, the present invention and a combination of one or more methods or compositions of the present invention also provide a method comprising contacting a crude oil feed with one or more supported catalysts, in the carrier: ⑷ Contains oxide oxide, silicon oxide 'silica-alumina, titanium oxide, lead oxide, magnesium oxide, or a mixture thereof, and / or zeolite; (b) contains gamma alumina and / or 5 alumina; in a mother gram carrier Contains up to 0.5 grams of gamma oxide; ⑷ contains at least 0.3 grams or at least 0.5 grams of osmium alumina per gram of carrier; ⑷ contains alpha alumina, gamma alumina, delta alumina, Θ alumina, or Its mixture; (f) containing up to 0.1 g of (X alumina) per gram of carrier. In some specific examples, the present invention and one or more methods or compositions of the present invention also provide a vanadium catalyst: (A) A pore size distribution with a median pore diameter of 乂 60A; (b) a carrier containing a θ alumina, and the vanadium catalyst has a pore size distribution with a median pore diameter of at least 60A; One or more metals, block 6 of the periodic table One or more metals, 0 or more compounds, or mixtures thereof; and / or rhenium containing at least 0.001 g per gram of catalyst: one or more metals in column 6 of the periodic table ', column 6 of the periodic table -Or more metals-or more compounds, or mixtures thereof. In some specific examples, the present invention and those combining one or more methods or compositions of the present invention also provide a crude oil product having: ⑷ at most 0.1 — 0.001 to 0.5, 0.01 to 0.2; or 0.05 to 01; () Metal test and soil test metal in the form of a maximum of 9 grams of organic acid metal salt per gram of crude oil product; ⑷ 纟 each The gram crude oil product has a maximum of 0.00002 grams of Ni / V / Fe; and / or (d) at least one catalyst that is greater than 42 200533737 gram, but less than 0.01 gram per gram of crude oil product. Specific examples in Yugan In combination, one or more methods or compositions of the present invention are also provided in combination with one or more metal test salts of organic acids, or one or more earth test metals of organic acids. A salt, or a mixture thereof, wherein: the at least one metal is Bell, sodium, or unloading; and / or (b) the at least one alkaline earth metal is magnesium or calcium. In some specific examples, the present invention and a combination of one or more methods or compositions of the present invention also provide a method, It includes contacting a crude oil feed with one or more catalysts to produce a total product containing crude oil products. The method further includes: combining the crude oil product with crude oils of the same or different crude oil feeds to form a blend suitable for transportation. (B) combining the crude oil product with the same or different crude oil feeds to form a blend suitable for processing equipment " 0 fractionating the crude oil product; and 蜮 ⑷ fractionating the crude oil product into-or A plurality of fractions, and a fuel for transportation is produced from the at least one fraction. In the specific example of the right stem, the present invention and those who combine one or more of the methods or compositions of the present invention also provide a supported catalyst composition, which: (a) contains at least 0.3 g or at least 0. per gram of carrier 5 g of rhenium alumina; δ alumina in the support; (c) up to 0.01 g of α alumina per gram of support; (d) a pore size distribution with a median pore size of at least 230 people; A pore volume having a pore size distribution of at least 0.3 cmVg or at least 0.7 cmVg; (f) having a surface area of at least 60 m2 / g or at least 90 m2 / g; (g) including the seventh to seventh periodic table 100 or more metals, one or more compounds of one or more metals of the Periodic Table 7 to 10, or mixtures thereof; 43 200533737 (h) containing 5 or more of the Periodic Table, including humans and rotten ones or Various metals, one of the five columns of the Periodic Table or one of the metal ’s ancient associations. Compounds, or mixtures thereof; (i) Contains () · 〇⑽ Xibo Chu per person per gram of catalyst towel. To ϋ.6 grams or 0.001 to 0.3 grams: one or more of the 5th metal, — ^ Α or the 5th metallization Substances, or mixtures thereof, (J) containing one or more metals in the Periodic Table 6, one of the columns in the Periodic Table 6 or the metals of the day — > or the compounds, or Mixtures; (k) Containing 〇〇〇υί to 0.6 grams or 0.001 to 0.3 grams per gram of catalyst: one or more 6th metal, one or more 6th metal compound , Or a mixture thereof; (1) containing vanadium, a sulphur compound, or a mixture thereof; (m) containing molybdenum, one or more molybdenum wheels, or a mixture thereof; (n) containing Tungsten, one or more tungsten compounds, or i, or four of these compounds; (0) contains cobalt, one or more cobalt compounds, or mixtures thereof. Β kappa 'and / or (p) contains nickel, a Or several nickel compounds, or mixtures thereof. In several specific examples, the present invention and those combining one or more methods or compositions of the present invention also provide a crude oil composition, which: (a) has a maximum of 1, a maximum of 0.5 , At most 0.3, or at most TAN; 含有 contains at least 0 · _g boiling range distribution per gram of composition in i Mpa _ hydrocarbons between 95 ° C and 260 ° C; a boiling range distribution of at least 0.001 g, at least 0.05 g, or at least 0.01 g between 26 (rc at 0.001 MPa Hydrocarbons between 320 ° C and 320 ° C; and at least 0.001 g of hydrocarbons with a boiling range distribution between 0.1 ° C and 650 ° C at 0.11 Mpa; (c) at least 0.0005 per gram of composition Grams of basic nitrogen; (d) containing at least 0.001 grams or at least 0.001 grams of total nitrogen per gram of composition; and / or (e) containing up to 0.00005 grams of gram per gram of composition Total nickel and vanadium. 44 200533737 In some specific examples, the present invention and a combination of one or more methods or compositions of the present invention also provide a crude oil composition comprising one or more catalysts, the at least one catalyst: (a) has a median The pore size is at least i80a, up to 500A, and / or a pore size distribution between 90 to 180A, 100 to 14A, and 120 to 130A; ⑻ has a median pore size of at least 90A, More than 60% of the total number of pores in the pore size distribution have pore sizes in the range of 45, 35, or even the median pore size; ⑷ has a surface area of at least 100 and at least one, or at least 22A ; ⑷ contains a carrier; the ㈣ contains an oxide, oxidized stone, oxidized stone _ oxide Shao, titanium oxide, oxidized in the mouth emulsification town, / Fu Shi, and / or mixtures thereof; ⑷ contains column 5 = 〇 of the periodic table -Or more metals, one or more compounds in columns 5 to 1 () of the periodic table, or mixtures thereof; (... 5 'of the periodic table · 5 of the-or multiple metal- or evening compounds, Or its mixture 0.0001 g: one or more green flute contains at least one character in the mother gram catalyst 5th metal,-or 5th metallization "Don't, or mixtures thereof; (h) all metals, one or more of column 6 of the periodic table: table or more or mixtures thereof; 或其 per gram of catalyst Medium or multiple compounds' or multiple column 6 metals,-a compound of at least 32 grams of ❹, a compound containing 周期 of the periodic table, or a compound of 10 or more of them , Periodic Table No .... contains two types of the Periodic Table 15: ^ Block one or more of Yuan Xin, ^ Xin Xing Wu Wu, the Periodic Table No. 15 in a variety of compounds, or mixtures thereof. In further specific examples, this The characteristics of the specific embodiment of the invention 45 200533737 may be combined with the characteristics of other specific embodiments of the invention. For example, the invention: The characteristics of the specific embodiments may be combined with the characteristics of other specific embodiments. In a further specific example, crude oil The product can be obtained by any of the methods and systems described herein. In further specific examples, additional features can be added to the specific specific examples described herein. [Embodiment] The specifics of the present invention are described in more detail herein. Examples of the body. As used herein, terms are defined as follows. · ASTM "means American Society for Testing Materials standard.

API比重”係指在15.5。(： （60T)下的API比重。API 比重係藉由ASTM法D6822測定。 原油進料與原油產物的原子氫百分率和原子碳百分率 係藉由ASTM法D5291測定。 除另有說明外，原油進料、總產物，及/或原油產物的 /弗程分佈係藉由ASTM法D5307測定。"API specific gravity" means API specific gravity at 15.5. (: 60T). API specific gravity is determined by ASTM method D6822. The atomic hydrogen percentage and atomic carbon percentage of crude oil feeds and crude products are determined by ASTM method D5291. Unless otherwise stated, crude oil feeds, total products, and / or crude product's / Fruff range are determined by ASTM method D5307.

Cs瀝青質”係指不溶於戊烷的瀝青質。c5瀝青質含量 · 係藉由ASTM法D2007測定。 第X攔金屬，，係指週期表第X攔的一或多種金屬及/ 〆週J表苐X攔之一或多種金屬的一或多種化合物，其中 子應於週期表的搁數（例如1至12)。舉例而言，‘‘第6 ”屬係^曰週期表第6攔的一或多種金屬及/或週期表第 6搁之一或多種金屬的一或多種化合物。 第X攔元素，，係指週期表第X攔的一或多種元素，及 46 200533737 /或週期表第x 中X係對庫^ 或多種元素的一或多種化合物，其 丨”“素；欄數(例如13至18)。舉例而Η 表第15搁之二期表第15搁的一或多種元素及/或週期 1之—或多種元素的一或多種化合物。 金屬的料内，週期表的金屬重量，週期表的 I，週期表的元素重量，或週期表的元素化 口 s係以金屬重量或元素重量計算。舉例而+，： （UW〇3’則該觸媒中銦金屬料^ 量為每克觸媒0.067克。 重 含量”係指以基質總重量計表示成重量分率或重量百 :率2基質(例如原油進料、總產⑯，或原油產物)中的成 为重里。WtpPm’，係指以重量計的百萬分率。 “原油進料/總產物混合物，，係指在處理期間與觸媒接觸 的混合物。 餾分係指沸程分佈在0.10! MPa下介於2〇4它（4〇〇 °F)和3机（650卞）之間的烴。餾分含量係藉由Μ，法 D5307測定。 “雜原子”係指烴分子結構中所含的氧、氮，及/或硫。 雜原子含量係藉由ASTM法對於氧的_，對於總氣的 D5762及對於硫的D4294測定。“鹼性氮總量，，係指具有pKa 小於40的氮化合物。鹼性氮（“bn，，）係藉由astm法d2896 測定。 “氫源”係指氫，及/或化合物及/或當原油進料和觸媒 存在下會反應而對原油進料中的化合物提供氫的化合物。 200533737 氫源可包括，但不限於烴（例 俨、a ^ (例如h至C4的烴，如甲烷、 :: 丁燒)、水，或其混合物。可進行質量均衡以估 汁對原油進料中的化合物所提供的淨氫量。 、 “平板抗碎強度，’係指壓碎觸媒所需的壓縮力。 碎強度係藉由ASTM法D4179測定。 几 LHSV係^日體積液體進料速率/觸媒總體積，其係以 小時㈨·1)表示。觸媒總體積係藉由總和接觸區中的所有 媒體積來計算，如本文中所述者。"Cs asphaltene" means asphaltenes that are insoluble in pentane. C5 Asphaltene content is determined by ASTM method D2007. The Xth metal, refers to one or more metals of the Xth period of the periodic table and / Table 苐 X is one or more compounds of one or more metals, the neutron of which should be the number of the periodic table (for example, 1 to 12). For example, the "sixth" belongs to the sixth table of the periodic table. One or more metals and / or one or more compounds of one or more metals in Period 6 of the Periodic Table. The X-th element refers to one or more elements of the X-th period of the periodic table, and one or more compounds of the X-series to the library ^ or multiple elements in the X-period of the Periodic Table 46200533737 and / or the "prime" column. Number (for example, 13 to 18). By way of example, one or more elements and / or one or more compounds of cycle 1-or one or more elements of table 15 of the second period of the 15th table. In the metal material, the metal weight of the periodic table, I of the periodic table, the element weight of the periodic table, or the elementization of the periodic table s is calculated based on the metal weight or element weight. For example, + ,: (UW〇3 ', the amount of indium metal in the catalyst is 0.067 grams per gram of catalyst. Weight content "refers to the weight fraction or weight percentage based on the total weight of the substrate: 2 substrate (Such as crude oil feed, total production, or crude oil products). WtpPm 'refers to parts per million by weight. "Crude oil feed / total product mixture, refers to contact with The mixture is a mixture which is contacted by a medium. A fraction refers to a hydrocarbon having a boiling range distribution between 0.14 (400 ° F) and 3 (650 ° F) at 0.10! MPa. The fraction content is determined by M, method D5307. Determination. "Heteroatom" refers to the oxygen, nitrogen, and / or sulfur contained in the molecular structure of a hydrocarbon. Heteroatom content is determined by the ASTM method for oxygen, D5762 for total gas, and D4294 for sulfur. " Total basic nitrogen refers to nitrogen compounds with a pKa of less than 40. Basic nitrogen ("bn,") is determined by the astm method d2896. "Hydrogen source" means hydrogen, and / or the compound and / or when A compound that reacts in the presence of a crude oil feed and a catalyst to provide hydrogen to a compound in the crude feed. 200533737 Hydrogen source can include , But not limited to hydrocarbons (eg, 俨, a ^ (such as h to C4 hydrocarbons, such as methane, :: butane), water, or mixtures thereof. Mass balance can be performed to estimate the compounds provided in the crude feed The amount of net hydrogen. "" Flat crushing strength, "refers to the compressive force required to crush the catalyst. The crushing strength is determined by ASTM method D4179. A few LHSV is the daily liquid feed rate / total catalyst volume. , Which is expressed in hours ㈨ · 1). The total volume of the catalyst is calculated by summing all the media volumes in the contact area, as described herein.

“液態混合物”係指包含在標準溫度和壓力(25。。，〇⑻ MPa，後文稱為“STP”)下為液態之一或多種化合物的組成 物’或是包含在STP下為液態的—或多種化合物與在up 下為固態的一或多種化合物之組合的組成物。 週期表係指2003年1丨月由國際純粹與應用化學聯 合會（IUPAC)所規定的週期表。 “有機酸金屬鹽形態的金屬，，係指鹼金屬、鹼土金屬、"Liquid mixture" means a composition containing one or more compounds that are liquid at standard temperature and pressure (25 °, MPa, hereinafter referred to as "STP"), or are contained in a liquid state under STP -A composition of a combination of one or more compounds and one or more compounds that are solid under up. The periodic table refers to the periodic table specified by the International Union of Pure and Applied Chemistry (IUPAC) in January 2003. "Metals in the form of metal salts of organic acids refer to alkali metals, alkaline earth metals,

鋅、砷、鉻，或其組合。有機酸金屬鹽形態的金屬含量係 藉由ASTM法D1318測定。 “微殘留碳”（“MCR”）含量係指在蒸發和熱解基質後留 下的殘留炭量。MCR含量係藉由ASTM法D4530測定。 石腦油係指沸程分佈在〇· 1〇1 MPa下介於38°C (100 °F )和200°C (392°F )之間的烴成分。石腦油含量係藉由 ASTM 法 D5307 測定。 “Ni/V/Fe”係指鎳、釩、鐵，或其組合。 “Ni/V/Fe含量”係指鎳、釩、鐵，或其組合的含量。 48 200533737Zinc, arsenic, chromium, or a combination thereof. The metal content of the organic acid metal salt was determined by ASTM method D1318. The "micro-residual carbon" ("MCR") content refers to the amount of residual carbon left after the substrate is evaporated and pyrolyzed. The MCR content is measured by ASTM method D4530. Naphtha refers to a hydrocarbon component having a boiling range distribution between 38 ° C (100 ° F) and 200 ° C (392 ° F) at 0.101 MPa. The naphtha content is determined by ASTM method D5307. "Ni / V / Fe" means nickel, vanadium, iron, or a combination thereof. "Ni / V / Fe content" refers to the content of nickel, vanadium, iron, or a combination thereof. 48 200533737

Ni/V/Fe含量係藉由ASTM法D5708測定。 “NmVm3”係指每立方米原油進料中的標準立方米氣 體。 “含非羧酸有機氧化合物”係指不含羧基（-C02-)的有機 氧化合物。含非羧酸有機氧化合物包括，但不限於醚、環 醚、醇、芳族醇、酮、醛，或其組合，其不含羧基。 “不可凝氣體”係指在STP下為氣態的成分及/或此等成 分之混合物。 “P (膠溶）值”或“P值”係指表示原油進料中瀝青質絮凝 傾向的數值。P值的測定係由J. J. Heithaus見述於J⑽r/ia/ 〇/ Institute of Petroleum, Vol. 48? Number 458, February 1962, pp. 45-33 的 “Measurement and Significance of Asphaltene Peptization”。 “孔徑”、“中位孔徑”和“孔體積”係指藉由 ASTM法 D4284 (成 140°之接觸角的水銀孔率法）所測定的孔徑、中 位孔徑和孔體積。micromeritics® A9220 儀器（Micromeritics Inc·，Nor cross Georgia，U.S. Α·)可用來測定這些值。 “殘留物”係指具有沸程分佈高於538 °C (1000 °F)的 成分，如ASTM法D53 07所測定者。 “SCFB”係指每桶原油進料中的氣體標準立方呎。 觸媒的“表面積”係藉由ASTM法D3663測定。 “TAN”係指總酸值，以每克（“g”）樣品中的KOH毫克 數（“mg”）表示。TAN係藉由ASTM法D664測定。 “VGO”係指沸程分佈在0.101 MPa下介於343 °C (650 49 200533737 F )和538 C (looo下）之間的烴。vg〇含量係藉由ASTM 法D5307測定。 ‘黏度’’係指在37.8 °C (100 °F)下的 利用ASTM法D445測定 在本申晴案的情況下，應瞭解如果已試驗基質之性質 所得到的數值在試驗方法的限制範圍外時，則可修正及/或 重新校準此試驗方法以測試這類性質。 原油了生產及/或乾德自含有構造物的煙接著使其穩定 化。原油可包含原油。原油通常為固體、半固體，及/或液 體。穩定化可包括，但不限於移除原油中的不可凝氣體、 水、鹽，或其組合以形成穩定原油。這類穩定化通常可能 發生在，或鄰近於生產及/或乾餾場所。 穩定原油典型而言尚未在處理設備中蒸餾及/或分餾以 生產具有特定沸程分佈（例如石腦油、餾分、vg〇，及/或 潤滑:由)的多成分。蒸餾包括，但不限於常壓蒸餾法及/或 減壓瘵餾法。未蒸餾及/或未分餾的穩定原油在每克原油 可能包含數量至少為0.5克的成分之碳數大於4的成分。 穩定原油的實例包括全原油、蒸餘原《由、脫鹽原油、脫_ 蒸餘原油，或其組合。“蒸餘”係指已處理過的原油，因2 已移除至少-部分具有沸點在〇•⑻Mpa下低於Μ “加…5T)的成分。典型而言，蒸餘原油在每 原油中具有含量最多為(Mb最多為QQ5克，或曰夕、：、 〇·〇2克的這類成分。 s 為 若干穩定原油具有可容許稃定肩油M m 原油猎由輪送載具（例如 50 200533737 管線、卡車，或船舶）輪送至習知處理設備的性質。其他原 ： 油具有-或多個使它們不利的不適當性質。劣質原油對於 輸送載具及/或處理設備而言可能是不能接受的，因此會賦 予劣質原油低的經濟價值。此經濟價值可能就像認為内含 劣質原油之容器的生產、輸送及/或處理成本太昂貴。 劣質原油的性質可包括，但不限於：a)至少〇·丨，至 少〇·3的TAN;b)至少1〇cSt的黏度；c)最多為19的Αρι 比重；d)總Ni/V/Fe含量為每克原油中至少有〇 〇〇〇〇2克 或至少有0·0_克的Ni/V/Fe; e)雜原子總含量為每克原籲 油中至少有0.005克的雜原子；f)歹麦留物含量為每克原油 中至少有〇.(H克的殘留物；g)C5瀝青質含量為每克原油 中至少有0.04克的C5瀝青質；h) MCR含量為每克原油中 至少有0.002克的MCR ; i)有機酸金屬鹽形態的金屬含量 為每克原油中至少有0.00001克的金屬；或〗）其組合。於 若干具體實例中，劣質原油在每克劣質原油中可包含至少 0·2克的殘留物，至少〇·3克的殘留物，至少Q 5克的殘留 物’或至少0 · 9克的殘留物。於若干具體實例中，劣質原 ® /由可能具有在0.1或0.3至20，〇·3或〇·5至1〇，或〇·4或 〇·5至5之範圍内的TAN。於特定具體實例中，劣質原油 在每克劣質原油中可能具有至少0_005克，至少〇 〇1克， 或至少0.02克的硫含量。 於若干具體實例中’劣質原油具有包括，但不限於下 列的性質：a)至少0.5的TAN; b)含氧量為每克原油進 料至少有0.005克的氧；c) C5瀝青質含量為每克原油進料 51 200533737 中至少有0·04克的C5瀝青質；d)大於期望黏度（例如對 於具有API比重至少為1〇的原油進料而言> 1〇 cSt) ; e) 有機酸金屬鹽形態的金屬含量為每克原油中至少有〇.〇〇〇〇 J 克的金屬；或f)其組合。 劣質原油在每克劣質原油中可包含：至少0.001克， 至少0.005克，或至少0.01克之沸程分佈在0.101 MPa下 介於90°C和200°C之間的烴；至少0.01克，至少0.005克， 或至少0.001克之沸程分佈在0.101 MPa下介於200°C和300 °C之間的烴；至少0.001克，至少0.005克，或至少0.01 克之沸程分佈在〇·1〇1 MPa下介於300°C和400°C之間的 烴；及至少0.001克，至少0.005克，或至少0_01克之沸 程分佈在0.101 MPa下介於400°C和650°C之間的烴。 劣質原油在每克劣質原油中可包含：至少0.001克， 至少0.005克，或至少0.01克之沸程分佈在0.101 MPa下 最多為100°C的烴；至少0.001克，至少0.005克，或至少 0.01克之沸程分佈在0.101 MPa下介於100°C和200°C之間 的烴；至少0_001克，至少0.005克，或至少0.01克之沸 程分佈在0.101 MPa下介於200°C和300°C之間的烴；至少 0.001克，至少0.005克，或至少〇·〇1克之沸程分佈在0.101 MPa下介於300°C和400°C之間的烴；及至少0.001克，至 少0.005克，或至少0.01克之沸程分佈在〇_ 1〇1 MPa下介 於400°C和650°C之間的烴。 除了較高沸點的成分之外，若干劣質原油在每克劣質 原油中可包含至少0.001克，至少〇·005克，或至少〇·〇1 52 200533737 克之沸程分佈在0.101 MPa下最多為i〇〇°c的烴。典型而 ； 吕’劣質原油在每克劣i原油中具有最多為0.2克或最多 為0 · 1克的這類烴含量。 若干劣質原油在每克劣質原油中可包含至少0.001 克，至少0.005克，或至少0.01克之沸程分佈在o.ioi MPa 下至少為200°C的烴。 若干劣質原油在每克劣質原油中可包含至少0.001 克，至少0.005克，或至少0.01克之沸程分佈至少為65〇 °C的烴。 籲 可使用本文中所述方法處理的劣質原油實例包括，但 不限於來自世界下列地區的原油·· U.S_ Gulf Coast和 southern California > Canada Tar sands > Brazilian Santos andThe Ni / V / Fe content is measured by ASTM method D5708. "NmVm3" refers to standard cubic meters of gas per cubic meter of crude oil feed. The "non-carboxylic acid-containing organic oxygen compound" means an organic oxygen compound containing no carboxyl group (-C02-). Non-carboxylic acid-containing organic oxygen compounds include, but are not limited to, ethers, cyclic ethers, alcohols, aromatic alcohols, ketones, aldehydes, or combinations thereof, which do not contain a carboxyl group. By "non-condensable gas" is meant a component that is gaseous under STP and / or a mixture of these components. "P (peptide) value" or "P value" means a value indicating the tendency of asphaltenes to flocculate in a crude oil feed. The measurement of the P value is described by J. J. Heithaus in "Measurement and Significance of Asphaltene Peptization" described in J⑽r / ia / 〇 / Institute of Petroleum, Vol. 48? Number 458, February 1962, pp. 45-33. "Aperture diameter", "median pore diameter" and "pore volume" refer to the pore diameter, median pore diameter, and pore volume determined by ASTM method D4284 (mercury porosity method at a contact angle of 140 °). A micromeritics® A9220 instrument (Micromeritics Inc., Nor cross Georgia, U.S. A.) can be used to determine these values. "Residue" means a component with a boiling range distribution above 538 ° C (1000 ° F), as determined by ASTM method D53 07. "SCFB" means the standard cubic feet of gas in a barrel of crude oil feed. The "surface area" of the catalyst was measured by ASTM method D3663. "TAN" refers to the total acid value, expressed in milligrams of KOH ("mg") per gram ("g") of the sample. TAN is measured by ASTM method D664. "VGO" refers to hydrocarbons with a boiling range distribution between 343 ° C (650 49 200533737 F) and 538 C (under Looo) at 0.101 MPa. The vg0 content was measured by ASTM method D5307. 'Viscosity' means the measurement by ASTM method D445 at 37.8 ° C (100 ° F). In the case of this application, it should be understood that if the properties of the substrate tested have values outside the limits of the test method This test method can be modified and / or recalibrated to test such properties. Crude oil is produced and / or smoke from the self-contained structures is then stabilized. Crude oil may include crude oil. Crude oil is usually solid, semi-solid, and / or liquid. Stabilization may include, but is not limited to, removing non-condensable gases, water, salts, or a combination thereof in the crude oil to form a stable crude oil. Such stabilization may often occur at or near production and / or retorting sites. Stable crude oils have typically not been distilled and / or fractionated in processing equipment to produce multi-components with specific boiling range distributions (e.g., naphtha, fractions, vg0, and / or lubrication: origin). Distillation includes, but is not limited to, atmospheric distillation and / or vacuum distillation. Undistilled and / or unfractionated stable crude oil may contain components having a carbon number greater than 4 per gram of crude oil. Examples of stabilized crude oils include whole crude oil, distillate crude oil, desalted crude oil, dedistilled crude oil, or a combination thereof. "Distillate residue" refers to processed crude oil, since 2 has been removed at least-partly with components having a boiling point below 0 "⑻Mpa below M" plus ... 5T). Typically, distillate crude oil has The content is at most (Mb is at most QQ5 grams, or xi,…, 〇2. 2 grams of such ingredients. S is a number of stable crude oils with allowable fixed shoulder oil M m crude oil hunting by a carrier (such as 50 200533737 The nature of pipelines, trucks, or ships) that are transported to conventional processing equipment. Other raw materials: Oils have-or more inappropriate properties that make them unfavorable. Poor crude oil may be a transport vehicle and / or processing equipment It is unacceptable and therefore gives a low economic value to inferior crude oil. This economic value may be as if the production, transportation, and / or treatment of a container containing inferior crude oil is considered too expensive. The properties of inferior crude oil may include, but are not limited to: a) a TAN of at least 0, 3; b) a viscosity of at least 10 cSt; c) a specific gravity of at most 19; d) a total Ni / V / Fe content of at least 0 per gram of crude oil 0.002 g or at least 0.0 g of Ni / V / Fe; e) miscellaneous The total content of seeds is at least 0.005 grams of heteroatoms per gram of crude oil; f) the content of oatmeal residue is at least 0. 0 grams of residues per gram of crude oil; g) the content of C5 asphaltenes per gram At least 0.04 grams of C5 asphaltenes in crude oil; h) an MCR content of at least 0.002 grams of MCR per gram of crude oil; i) a metal content in the form of an organic acid metal salt of at least 0.00001 grams of metal per gram of crude oil; or 〖) And its combination. In several specific examples, inferior crude oil may contain at least 0.2 grams of residue, at least 0.3 grams of residue, at least Q 5 grams of residue 'or at least 0 per gram of inferior crude oil. · 9 grams of residue. In several specific examples, inferior raw materials may have a range of 0.1 or 0.3 to 20, 0.3 or 0.5 to 10, or 0.4 or 0.5 to 5. In certain specific examples, inferior crude oil may have a sulfur content of at least 0-005 grams, at least 0.001 grams, or at least 0.02 grams per gram of inferior crude oil. In several specific examples, 'inferior crude oil has included, but Not limited to the following properties: a) TAN of at least 0.5; b) oxygen content per gram of crude oil At least 0.005 grams of oxygen; c) C5 asphaltene content is at least 0.04 grams of C5 asphaltene per gram of crude feed 51 200533737; d) is greater than the desired viscosity (for example, for crude oil with an API specific gravity of at least 10) In terms of feed > 10 cSt); e) metal content in the form of metal salt of organic acid is at least 0.00000 g of metal per gram of crude oil; or f) a combination thereof. Poor crude oil may include: at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams of hydrocarbons having a boiling range distribution between 90 ° C and 200 ° C at 0.101 MPa; at least 0.01 grams, at least 0.005 grams, or at least 0.001 Grams of hydrocarbons with a boiling range between 200 ° C and 300 ° C at 0.101 MPa; at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams with a boiling range at 300 ° C at 0.101 MPa Hydrocarbons between 400 ° C and 400 ° C; and hydrocarbons with a boiling range distribution between 0.1 ° C and 650 ° C at 0.101 MPa of at least 0.001 g, at least 0.005 g, or at least 0_01 g. Inferior crude oil may include per gram of inferior crude oil: at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams of hydrocarbons having a boiling range distribution of up to 100 ° C at 0.101 MPa; at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams. Hydrocarbons with a boiling range distribution between 100 ° C and 200 ° C at 0.101 MPa; at least 0_001 grams, at least 0.005 grams, or at least 0.01 grams, with a boiling range distribution between 200 ° C and 300 ° C at 0.101 MPa At least 0.001 g, at least 0.005 g, or at least 0.001 g of a hydrocarbon having a boiling range distribution between 300 ° C and 400 ° C at 0.101 MPa; and at least 0.001 g, at least 0.005 g, or At least 0.01 g of a hydrocarbon having a boiling range distribution between 400 ° C. and 650 ° C. at 0-10 MPa. In addition to the higher boiling point components, several inferior crudes may contain at least 0.001 grams, at least 0.005 grams, or at least 0.0005 per gram of inferior crude oil at a boiling range distribution of at most 0.101 MPa at 0.10 MPa. 0 ° C hydrocarbons. Typically, Lu 'inferior crude oil has a hydrocarbon content of at most 0.2 grams or at most 0.1 grams per gram of inferior crude oil. Several inferior crudes may contain at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams of hydrocarbons having a boiling range distribution of at least 200 ° C at o.ioi MPa per gram of inferior crude oil. Several inferior crudes may contain at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams of hydrocarbons having a boiling range distribution of at least 65 ° C. per gram of inferior crude oil. Examples of inferior crude oils that can be processed using the methods described herein include, but are not limited to, crude oil from the following regions of the world. U.S. Gulf Coast and southern California > Canada Tar sands > Brazilian Santos and

Campos basins、Egyptian Gulf of Suez、Chad、United Kingdom North Sea、Angola Offshore、Chinese Bohai Bay、 Venezuelan Zulia、Malaysia 及 Indonesia Sumatra。 處理劣質原油可增進劣質原油的性質以便使該原油可 為輸送及/或處理所接受。 參 本文中欲處理的原油及/或劣質原油稱為“原油進料”。 此原油進料可如本文中所述的蒸餘原油。如本文中所述之 由處理原油進料所得的原油產物通常適用於輸送及/或處 理。如本文中所述生產的原油產物性質比原油進料更接近 西德州中級原油的對應性質，或是比原油進料更接近布倫 特（Brent)原油的對應性質，藉此提高原油進料的經濟價 值。這類原油產物可用較少或不用預處理精煉，藉此提高 53 200533737 精煉效率。預處理可包括脫硫、脫金屬及/或常壓蒸餾 除雜質。 、根據本發明處理原油進料可包括在接觸區及/或結合兩 個或更多個接觸區中使原油進料與觸媒接觸。在接觸區 中，f油進料的至少一種性質與該原油進料的同樣性質相 比可藉由該原油進料與一或多種觸媒的接觸而改變。於若 干八體貫例中’在氫源存在下進行接觸。於若干具體實例 中氫源為在特定接觸條件下反應而對原油進料中的化合 物提供相當少量氫的一或多種烴。 口 圖1為接觸系統1 〇〇的簡圖，其包含接觸區丨〇2。原 油進料、、二由導管1 04進入接觸區丨〇2。接觸區可為反應器、 反應器之一部分、反應器之多個部分，或其組合。接觸區 的實例包括堆疊床反應器、固定床反應器、沸騰床反應器、 連續攪拌槽式反應器（“CSTR”）、流化床反應器、喷霧反應 器，及液/液接觸器。於特定具體實例中，接觸系統係位於 或連接到近海設備。在接觸系統100中，原油進料與觸媒 的接觸可為連續或分批法。 此接觸區可包含一或多種觸媒（例如兩種觸媒）。於若 干具體實例中，原油進料與兩種觸媒之第一種觸媒的接觸 可減少該原油進料的TAN。已減少TAN的原油進料與第 二種觸媒的後續接觸係減少雜原子含量並增加API比重。 在其他具體實例中，在原油進料與一或多種觸媒接觸之 後，原油進料之TAN、黏度、Ni/V/Fe含量、雜原子含量、 殘留物含量、API比重，或是這些性質的組合與該原油進 54 200533737 料的同樣性質相比會改變至少ίο%。 ； 於特疋具體實例中，接觸區中的觸媒體積在1 〇至00 體積20至50體積％，或3〇至4〇體積％之接觸區中原 油進料總體積的範圍内。於若干具體實例中，觸媒和原油 進料的裝液在接觸區的# 100克原油進料中可包含0.001 至10克’ 0.005至5克，或〇 〇1至3克的觸媒。 接觸區中的接觸條件可包括，但不限於溫度、壓力、 氫源動原油進料流動，或其組合。控制若干具體實例 中的接觸條件以生產具有特性的原油產物。接觸區中的溫 _ 度 T 刀佈在 50 至 5〇〇〇c，60 至 440〇C，70 至 430°C，或 80 至420 C的範圍。接觸區中的壓力可分佈在〇· 1至別MPa， 1至12 MPa，4至l〇 MPa，或ό至8 MPa的範圍。原油進 料的LHSV通常分佈在〇 1至％ h_i，〇」至Μ h·1，1至20 •5至15h ，或2至1〇 h-1的範圍。於若干具體實例 中’ LHSV至少為5 ^，至少為11 h·1，至少為15 h-i，或 至少為20 Ir1。 在氫源以氣體（例如氫氣）供應的具體實例中，氣態氫 · 源和原油進料的比率典型而言分佈在〇.丨至1 〇〇,〇〇〇 Nm /m3’ 〇.5 至 10，_ Nm3/m3, 1 至 8,0〇〇 Nm3/m3,2 至 5,000Campos basins, Egyptian Gulf of Suez, Chad, United Kingdom North Sea, Angola Offshore, Chinese Bohai Bay, Venezuelan Zulia, Malaysia, and Indonesia Sumatra. Processing of poor quality crude oil can enhance the properties of the poor quality crude oil so that the crude oil is acceptable for transportation and / or processing. The crude oil and / or inferior crude oil to be processed is referred to herein as the "crude feed". This crude feed can be a distillate crude as described herein. Crude products derived from processing crude feeds as described herein are generally suitable for transportation and / or processing. The properties of crude oil products produced as described herein are closer to the corresponding properties of West Texas Intermediate crude oil than the crude oil feed, or closer to the corresponding properties of Brent crude oil than the crude oil feed, thereby improving the crude oil feed Economic Value. This type of crude oil product can be refined with little or no pretreatment, thereby improving the refining efficiency of 53 200533737. Pretreatment may include desulfurization, demetallization, and / or atmospheric distillation to remove impurities. 2. Processing a crude oil feed according to the present invention may include contacting the crude oil feed with a catalyst in a contact zone and / or a combination of two or more contact zones. In the contact zone, at least one property of the f oil feed compared to the same property of the crude feed can be changed by contacting the crude feed with one or more catalysts. In several examples of the octagonal body, the contact is made in the presence of a hydrogen source. In several specific examples, the hydrogen source is one or more hydrocarbons that provide a relatively small amount of hydrogen to the compounds in the crude feed in order to react under specific contact conditions.口 Figure 1 is a simplified diagram of the contact system 100, which includes a contact area 〇2. Crude oil feed, and two enter the contact zone through the conduit 104. The contact zone may be a reactor, a portion of a reactor, multiple portions of a reactor, or a combination thereof. Examples of contact zones include stacked bed reactors, fixed bed reactors, ebullated bed reactors, continuous stirred tank reactors ("CSTR"), fluidized bed reactors, spray reactors, and liquid / liquid contactors. In a specific embodiment, the contact system is located at or connected to offshore equipment. In the contact system 100, the contact of the crude feed with the catalyst may be a continuous or batch process. This contact area may contain one or more catalysts (eg, two catalysts). In several specific examples, contacting the crude feed with the first catalyst of the two catalysts can reduce the TAN of the crude feed. Subsequent contact of the TAN-reduced crude oil feed with the second catalyst reduces heteroatom content and increases API specific gravity. In other specific examples, the TAN, viscosity, Ni / V / Fe content, heteroatom content, residue content, API gravity, or these properties of the crude oil feed after contacting the crude oil feed with one or more catalysts. The combination will change by at least ίο% compared to the same properties of this crude oil feed. In a specific example, the volume of the contact medium in the contact zone is within the range of 10 to 00 vol. 20 to 50 vol.%, Or 30 to 40 vol.% Of the total crude oil feed volume in the contact zone. In some specific examples, the loading liquid of the catalyst and the crude oil feed may contain 0.001 to 10 grams of the '0.005 to 5 grams, or 0.01 to 3 grams of the catalyst in the # 100 grams of crude oil feed in the contact zone. The contact conditions in the contact zone may include, but are not limited to, temperature, pressure, hydrogen source moving crude oil feed flow, or a combination thereof. The contact conditions in several specific examples are controlled to produce characteristic crude oil products. The temperature T in the contact area is in the range of 50 to 50000c, 60 to 4400 ° C, 70 to 430 ° C, or 80 to 420 ° C. The pressure in the contact zone may be in the range of 0.1 to 12 MPa, 1 to 12 MPa, 4 to 10 MPa, or 6 to 8 MPa. The LHSV of the crude oil feed is usually distributed in the range of 01 to% h_i, 0 ″ to M h · 1, 1 to 20 • 5 to 15 h, or 2 to 10 h-1. In several specific examples, the LHSV is at least 5 ^, at least 11 h · 1, at least 15 h-i, or at least 20 Ir1. In the specific example where the hydrogen source is supplied as a gas (such as hydrogen), the ratio of the gaseous hydrogen · source to the crude oil feed is typically distributed in the range of 0.1 to 10,000,000 Nm / m3 ', 0.5 to 10 _ Nm3 / m3, 1 to 8,00 Nm3 / m3, 2 to 5,000

Nm3/m3，5 至 3,000 Nm3/m3，或 10 至 800 Nm3/m3 與觸媒 接觸的範圍。此氫源於若干具體實例中係與載送氣體結合 並且再循環通過接觸區。載送氣體可例如為氮、氦，及/或 氮。載送氣體可促進接觸區中的原油進料流動及/或氫源流 動。載送氣體亦可增進接觸區中的混合作用。於若干具體 55 200533737 實例中，氫源（例如氫、 L 或乙烷）可用來作Λ恭s々诚 並且再循環通過接觸區。 乍為裁达風體 風源可舆導營丨士 中的原油進料並流或經由導瞢 分別進入接觸區1〇2。 由導e 106 的接觸传產生八古 區1〇2中’原油進料與觸媒 :接觸係產生含有原油產物，而在若干具體實例 體的總產物。於若干且，眘 ；' 右干具體實例中，载送氣體係 及/或在導管106中盥气、后从人 尽，由進# 中/、虱源纟。合。總產物可離開接觸區1〇2 !由導官110進入分離區108。 於分離區1〇8中，片、、由甚必$ a触 r原油產物和軋體可使用一般已知的 分離技術，例如ϋ _、為八M ^ '、狄 乳/夜刀離，自總產物分離。原油產物可經 由導g 112離開分離區1〇8，接著輸送到輸送載具、管線、 啫存谷态/精煉廠、其他處理區，或其組合。氣體可包括 處理期間所生成的氣體(例如硫化氫、二氧化碳，及/或一 氧化反）過里氣恶氳源，及/或載送氣體。過量氣體可再 循環至接觸系、、统⑽，可純化，輸送到其他處理區、儲存 容器，或其組合。 於若干具體實例中，使原油進料與觸媒接觸以生產總 產物係於兩個或更多個接觸區内進行。可分離該總產物以 生成原油產物和氣體。 圖2至3為包含兩個或三個接觸區的接觸系統1 〇 〇之 具體實例的簡圖。在圖2A和2B中，接觸系統1〇〇包含接 觸區102和114。圖3 A和3B包含。接觸區1 〇2、114、11 6。 在圖2A和3A中，接觸區102、114、116係描繪成在一個 反應器中的個別接觸區。原油進料係經由導管1 進入接 56 200533737 觸區102。 於若干具體實例中，載送氣體在導管丨〇6中與氫源社 合並且以混合物的形式導入接觸區。於特定且體實例中 如圖1、3A和3B所示者，氫源及/或載送氣體可經由導管 106及/或經由如導管1〇6’以原油進料流動相反的方向’= 原油進料分別進入一或多個接觸區。與原油進料流動反向 添加氫源及/或載送氣體可增進原油進料與觸媒的混合及\ 或接觸。 在接觸區102中，原油進料與觸媒的接觸會生成原料 _ 流。此原料流係由接觸區102流到接觸區114。在圖3八和 3 B中，原料流係由接觸區114流到接觸區116。 接觸區1〇2、114、116可包含一或多種觸媒。如圖2b 所示，原料流係經由導管118離開接觸區1〇2而進入接觸 區114。如® 3B所*，原料流係經由導管118離開接觸區 1 1 4而進入接觸區1 1 6。 、原料流可在接觸區114及/或接觸區116與附加觸媒接 觸以生^總產物。總產物離開接觸區114及/或接觸區鲁 、工由導S "0進入分離區1〇8。原油產物及/或氣體係分離 自總產物。原油產物係經由導管112離開分離區108。 〇圖4為分離區在接觸系統1GG上游之具體實例的簡圖。 名貝原油(蒸餘或非蒸餘者)係經由導管122進入分離區 Z在分離區120中，至少一部分的劣質原油係使用該 决甚Γ已知的技術（例如喷佈、薄膜分離、減壓）分離以Nm3 / m3, 5 to 3,000 Nm3 / m3, or 10 to 800 Nm3 / m3 in contact with the catalyst. This hydrogen originates from several specific examples in combination with a carrier gas and recycled through the contact zone. The carrier gas may be, for example, nitrogen, helium, and / or nitrogen. The carrier gas can facilitate the flow of crude oil feed and / or hydrogen source in the contact zone. The carrier gas can also enhance mixing in the contact zone. In several specific 55 200533737 examples, a hydrogen source (such as hydrogen, L, or ethane) can be used as a sacrifice and recycled through the contact zone. At first glance, the wind source can feed crude oil from the pilot camp and enter the contact area 102 respectively through the co-current flow or via the guide. The contact transmission of e 106 produces the crude oil feed and catalyst in the Baku area 102: the contact system produces the total product containing crude oil products, but in several specific examples. In a number of, and cautious; in the specific example of the right stem, the air-carrying system and / or the gas in the catheter 106 are exhausted from the person, and then enter the center and the lice source. Together. The total product can leave the contact zone 102 and enter the separation zone 108 by the guide 110. In the separation zone 108, the flakes, crude oil products, and rolling stocks that must be contacted with each other can use commonly known separation techniques, such as ϋ 为, MM ^ ', Diru / Night Knife, The total product was isolated. The crude product may leave the separation zone 108 via the guide 112, and then be transported to a conveyance vehicle, a pipeline, a storage valley / refinery, other processing zones, or a combination thereof. Gases may include gases (e.g., hydrogen sulfide, carbon dioxide, and / or reverse monoxide) generated during processing, and / or carrier gases. Excess gas can be recycled to the contact system, system, and purified, and transferred to other processing areas, storage containers, or a combination thereof. In several specific examples, contacting a crude feed with a catalyst to produce a total product is performed in two or more contact zones. This total product can be separated to produce crude oil products and gases. Figures 2 to 3 are simplified diagrams of specific examples of a contact system 100 including two or three contact zones. In Figures 2A and 2B, the contact system 100 includes contact areas 102 and 114. Figures 3 A and 3B contain. The contact areas 1 02, 114, 116. In Figures 2A and 3A, the contact areas 102, 114, 116 are depicted as individual contact areas in a reactor. The crude oil feed enters contact zone 102 through conduit 1 2005200533737. In several specific examples, the carrier gas is incorporated in the conduit with the hydrogen source and introduced into the contact zone as a mixture. In specific examples, as shown in Figures 1, 3A, and 3B, the hydrogen source and / or carrier gas may flow through the conduit 106 and / or via the conduit 1 06 'in the opposite direction as the crude oil feed flow' = crude The feed enters one or more contact zones, respectively. Reverse the flow of crude oil feed The addition of a hydrogen source and / or carrier gas can enhance the mixing and / or contact of the crude oil feed and the catalyst. In the contact zone 102, contact of the crude oil feed with the catalyst generates a raw material stream. This raw material stream flows from the contact zone 102 to the contact zone 114. In FIGS. 3A and 3B, the feed stream flows from the contact zone 114 to the contact zone 116. The contact areas 102, 114, 116 may include one or more catalysts. As shown in FIG. 2b, the feed stream leaves the contact zone 102 via the conduit 118 and enters the contact zone 114. As indicated by ® 3B *, the feed stream leaves contact zone 1 1 4 via conduit 118 and enters contact zone 1 1 6. The raw material stream may be contacted with additional catalyst in the contact zone 114 and / or the contact zone 116 to produce a total product. The total product leaves the contacting zone 114 and / or the contacting zone and enters the separation zone 108. Crude products and / or gas systems are separated from the total products. The crude product exits the separation zone 108 via a conduit 112. Figure 4 is a simplified diagram of a specific example of the separation zone upstream of the contact system 1GG. Mingbei crude oil (distilled or non-distilled) enters the separation zone Z through the conduit 122. In the separation zone 120, at least a part of the inferior crude oil is using a technique known by this method (such as spraying, membrane separation, Pressure

生產原油進料。與A 牛例而言，水可從劣質原油中至少部分分 57 200533737 離。於另一實例中，具有沸程分佈低於95它或低於1 〇〇〇c 的成分可從劣質原油中至少部分分離以生產原油進料。於 右干具體貫例中’至少一部分的石腦油及比石腦油更具揮 發性的化合物係從劣質原油中分離。於若干具體實例中， 至少一部分經過分離的成分係經由導管1 24離開分離區 120 ° 由分離區120所得到的原油進料於若干具體實例中係 包含沸程分佈至少為1〇〇它，或於若干具體實例中，沸程 分佈至少為120°C之成分的混合物。典型而言，經過分離 _ 的原油進料包含沸程分佈介於100至1000 °c，120至900 C或2⑽至8 0 0 c之成分的混合物。至少一部分的原油 進料經由導管126離開分離區120進入接觸系統1〇〇 (參見 如圖1至3中的接觸區）以進一步處理生成原油產物。於若 干具體實例中，分離區12〇可位於脫鹽單元的上游或下游。 處理之後，原油產物係經由導管i 12離開接觸系統1〇〇。 於若干具體實例中，使原油產物與原油進料相同或不 同的原油摻合。舉例而言，原油產物可與具有不同黏度# · 原油結合，藉此產生具有黏度介於該原油產物黏度與該原 油黏度之間的摻合產品。於另一實例中，原油產物可與具 有不同TAN的原油摻合，藉此產生具有TAN介於該原油 產物與該原油TAN之間的產品。此摻合產品可適用=輸送 及/或處理。 管 如圖5所示，於特定具體實例中，原油進料係經由導 1〇4進入接觸系統1〇〇,而至少一部分的原油產物經由 58 200533737 導管128離開接觸系統100導入摻合區13〇。於摻合區i3〇 中，使至少一部分的原油產物與一或多個工業生產液流（例 如烴流，如分離一或多種原油進料所產生的石腦油）、原油、 原油進料，或其混合物結合以產生摻合產品。將工業生產 液流、原油進料、原油，或其混合物經由導管丨32直接導 入摻合區130或這類摻合區的上游。混合系統可位於或接 近摻合區130。摻合產品可符合精煉廠及/或輸送載具所指 定的產品規格。產品規格包括，但不限於Αρι比重、tan、 黏度，或其組合的範圍或限制。摻合產品係經由導管ΐ34 離開摻合區130以進行輸送或處理。 在圖6中，劣質原油係通過導管ι22進入分離區ι2〇， 如先前所述使劣質原油分離以生成原油進料。原油進料接 著通過導官1 26進入接觸系統1 〇〇。該劣質原油的至少若 干成分係經由導管124離開分離區i 2〇。至少一部分的原 油產物係經由導管128離開接觸系統100進入摻合區13〇。 其他工業生產液流及/或原油係直接或經由導管1 3 2進入摻 a區1 3 0與原油產物結合生成摻合產品。摻合產品係經由 導管134離開摻合區130。 於若干具體實例中，原油產物及/或摻合產品係輸送到 精煉廠及/或處理設備。原油產物及/或摻合產品可加工以 生產工業產品，如運輸用燃料、加熱用燃料、潤滑油或化 學品。加工可包括蒸餾及/或分餾原油產物及/或摻合產品 以產生一或多種餾分。於若干具體實例中，原油產物、摻 合產品，及/或一或多種餾分可加氫處理。 59 200533737 於若干具體實例中，原油產物具有TAN最多為9〇〇/， 取多為50〇/〇,最多為3〇%，或最多$ 1〇%之原油進料的 TAN。於若干具體實例中，原油產物具有tan在工至， 20至70%，30至60%，或40至5〇%之原油進料的丁an之 耗圍内。於特定具體實例中，原油產物具有最多為1，最 多為〇·5 ’最多為〇·3，最多為〇·2，最多為〇1，或最多為 〇·〇5的TAN。原油產物的ΤΑΝ通常至少為〇 〇〇〇ι，更常 見者，至少為0.001。於若干具體實例中，原油產物的ταν 可在0.001至〇·5，〇.01至〇 2，或〇 〇5至〇」的範圍内。 於若干具體實例中，原油產物具有總Ni/V/Fe含量最 夕為90 /〇，隶多為50%，最多為ι〇〇/〇，最多為5%，或最 多為3%之原油進料的Ni/V/Fe含量。此原油產物於若干具 體實例中具有總Ni/V/Fe含量在i至80%，10至7〇%，2〇 至60%’或30至50%之原油進料的Ni/V/Fe含量之範圍内。 於特定具體實例中，原油產物在每克原油產物中具有在i χ 10 7 克至 5 χ 1〇-5 克，3 χ 1〇-7 克至 2 χ 1〇·5 克，或 i χ 1〇_6 克至1 X 10克之範圍内的總Ni/v/Fe含量。於特定具體實 例中’此原油含有最多為2 x 1〇-5克的Ni/V/Fe。於若干具 體貫例中’原油產物的總Ni/V/Fe含量為70至130%，80 至120%或90至11〇%之原油進料的Ni/V/Fe含量。 於若干具體實例中，原油產物具有有機酸金屬鹽形態 的金屬總含量最多為90%，最多為50%，最多為10%，或 最多為5%之原油進料中有機酸金屬鹽形態的金屬總含量。 於特定具體實例中，原油產物具有有機酸金屬鹽形態的金 200533737 屬總含量在1至80%，10至70%，20至60%，或3〇至50% 之原油進料中有機酸金屬鹽形態的金屬總含量之範圍内。 常用來生成金屬鹽的有機酸包括，但不限於羧酸、硫醇、 亞胺、磺酸和磺酸鹽。羧酸的實例包括，但不限於環烷酸、 菲酸和苯甲酸。金屬鹽的金屬部分可包括鹼金屬（例如鋰、 鈉和鉀），鹼土金屬（例如鎂、鈣和鋇），第12欄金屬（例如 辞和鎘），第15欄金屬（例如砷），第6攔金屬（例如鉻），或 其混合物。Production of crude feed. In the case of A cattle, water can be at least partially separated from inferior crude oil. In another example, components with a boiling range distribution below 95 or below 1000c can be at least partially separated from a poor quality crude to produce a crude feed. In the concrete example of the right stem, at least part of the naphtha and compounds more volatile than naphtha were separated from the inferior crude oil. In some specific examples, at least a portion of the separated components leave the separation zone 120 through the conduit 1 24. The crude oil feed obtained from the separation zone 120 contains, in some specific examples, a boiling range distribution of at least 100, or In certain embodiments, a mixture of ingredients having a boiling range distribution of at least 120 ° C. Typically, the separated crude oil feed comprises a mixture of components having a boiling range distribution between 100 to 1000 ° C, 120 to 900 C, or 2 to 800 C. At least a portion of the crude oil feed leaves separation zone 120 via conduit 126 and enters contact system 100 (see contact zone as in Figures 1-3) for further processing to produce crude oil products. In some embodiments, the separation zone 120 may be located upstream or downstream of the desalination unit. After processing, the crude product exited the contact system 100 via conduit i 12. In several specific examples, the crude product is blended with the same or different crude oil feeds. For example, crude oil products can be combined with crude oils with different viscosities #, thereby producing a blended product with a viscosity between the viscosity of the crude oil product and the viscosity of the crude oil. In another example, a crude product may be blended with a crude oil having a different TAN, thereby producing a product having a TAN between the crude product and the crude TAN. This blended product may be suitable = conveyed and / or handled. The tube is shown in FIG. 5. In a specific embodiment, the crude oil feed enters the contact system 100 via the guide 104, and at least a portion of the crude product leaves the contact system 100 via the 58 200533737 conduit 128 and is introduced into the blending zone 13 . In the blending zone i30, at least a portion of the crude oil product is combined with one or more industrial production streams (eg, hydrocarbon streams, such as naphtha produced by separating one or more crude feeds), crude oil, crude feed, Or a mixture thereof to produce a blended product. Industrial production streams, crude oil feeds, crude oil, or mixtures thereof are directed via conduits 32 to the blending zone 130 or upstream of such blending zones. The mixing system may be located at or near the blending zone 130. The blended product can meet the product specifications specified by the refinery and / or conveyor. Product specifications include, but are not limited to, the range or limitation of Aρι specific gravity, tan, viscosity, or a combination thereof. The blended product leaves the blending zone 130 for delivery or processing via the catheter ΐ34. In FIG. 6, the inferior crude oil enters the separation zone ι20 through the conduit ι22, and the inferior crude oil is separated to generate a crude oil feed as previously described. The crude feed then enters the contact system 100 through the pilot 126. At least some of the components of the inferior crude oil leave the separation zone i 2O via the conduit 124. At least a portion of the crude oil product exits the contact system 100 via the conduit 128 and enters the blending zone 130. Other industrial production streams and / or crude oils enter the a-doped zone 1 30 directly or via the conduits 1 2 3 and combine with the crude product to form a blended product. The blended product exits the blending zone 130 via a conduit 134. In several specific examples, the crude product and / or blended product is delivered to a refinery and / or processing facility. Crude products and / or blended products can be processed to produce industrial products such as transportation fuels, heating fuels, lubricants or chemicals. Processing may include distilling and / or fractionating the crude product and / or blending the product to produce one or more fractions. In several specific examples, crude oil products, blended products, and / or one or more fractions may be hydrotreated. 59 200533737 In several specific examples, the crude oil product has a TAN of up to 900 /, a maximum of 50 //, a maximum of 30%, or a TAN of crude oil feed of up to $ 10%. In certain specific examples, the crude oil product has tan within the consumption range of 20 to 70%, 30 to 60%, or 40 to 50% of the crude oil feed. In certain specific examples, the crude oil product has a TAN of at most 1, at most 0.5 ', at most 0.3, at most 0.2, at most 01, or at most 0.05. The TAN of the crude product is usually at least 100,000, and more often, at least 0.001. In several specific examples, the ταν of the crude oil product may be in a range of 0.001 to 0.5, 0.01 to 0.2, or 0.05 to 0 ". In some specific examples, the crude oil product has a total Ni / V / Fe content of 90 / 〇 at most, 50% at most, ι〇〇 / 〇 at most, 5% at most, or 3% at most. Ni / V / Fe content of the material. This crude oil product has, in several specific examples, a total Ni / V / Fe content of i to 80%, 10 to 70%, 20 to 60% ', or 30 to 50% of the Ni / V / Fe content of the crude oil feed. Within range. In a specific embodiment, the crude oil product has a range of i χ 10 7 g to 5 χ 1 0-5 g, 3 χ 1 0-7 g to 2 χ 10.5 g, or i χ 1 per gram of crude product. Total Ni / v / Fe content in the range of 0-6 grams to 1 X 10 grams. In a specific embodiment, this crude oil contains up to 2 x 10-5 grams of Ni / V / Fe. In several specific examples, the 'crude oil product has a total Ni / V / Fe content of 70 to 130%, 80 to 120%, or 90 to 110% of the Ni / V / Fe content of the crude oil feed. In some specific examples, the crude product has a total metal content of organic acid metal salt form of up to 90%, a maximum of 50%, a maximum of 10%, or a maximum of 5% of the metal in the form of an organic acid metal salt in the crude oil feed. Total content. In specific examples, the crude oil product has the form of an organic acid metal salt 200533737. The total content of the metal is 1 to 80%, 10 to 70%, 20 to 60%, or 30 to 50% of the organic acid metal in the crude oil feed. Within the total metal content of the salt form. Organic acids commonly used to form metal salts include, but are not limited to, carboxylic acids, thiols, imines, sulfonic acids, and sulfonates. Examples of carboxylic acids include, but are not limited to, naphthenic acid, phenanthronic acid, and benzoic acid. The metal portion of the metal salt may include alkali metals (such as lithium, sodium, and potassium), alkaline earth metals (such as magnesium, calcium, and barium), column 12 metals (such as Ci and Cd), column 15 metals (such as arsenic), and 6 metal (such as chromium), or a mixture thereof.

於特定具體實例中，原油產物在每克原油產物中具有 有機酸金屬鹽形態的金屬總含量為在每克原油產物=有 0-0000001 克至 0_00005 克，〇 〇〇〇〇〇〇3 克至 〇 克， 或0.000001克至0·00001克的有機酸金屬鹽形態之金屬的 範圍内。於若干具體實例中，原油產物之有機酸金屬鹽形 態的金屬總含量為70至130%，》0至120%，或90至110% 之原油進料中有機酸金屬鹽形態的金屬總含量。 〇In a specific embodiment, the total metal content of the crude oil product in the form of an organic acid metal salt per gram of crude oil product is between 0-0000001 grams to 0-00005 grams per gram of crude oil products, and 0 g, or 0.00001 g to 0.0001 g of metal in the form of a metal salt of an organic acid. In some specific examples, the total metal content of the organic acid metal salt form of the crude oil product is 70 to 130%, 0 to 120%, or 90 to 110% of the total metal content of the organic acid metal salt form in the crude oil feed. 〇

於特定具體實例中，在接觸條件下原油進料與觸媒接 觸所生產的原油產物之ΑΡΙ比重為7〇至13〇%，8〇至 咖/。，90至110%，或1〇〇至13〇%之原油進料的Αρι比 重。於特定具體實例中’原油產物的API比重為14至4〇, 15 至 3〇，或 16 至 25。 ^於特定具體實例中，原油產物具有黏度最多為州 取二為80%，或最多& 70%之原油進料的黏度。於若干 體實例中’原油產物具有黏度在1〇 i 6〇%，2〇至州 或30至40%之原油進料的黏度之範圍内。於若干具體 61 200533737 例中’原油產物的考占声县 日度取夕為90%之原油進料的黏度，同 日守此原油產物㈤API比重為7〇至13〇%， ^ 90至110%之原油進料的Ambp 或 於若干具體f你丨+ 、j中，原油產物具有雜原子總含量最$ 為90%，最多為50。/ 旦a 。各里取夕 最多為1〇%，或最多為5%之原油 進料的雜原子總含量。於 ’、 於特疋具體實例中，原油產物且 雜原子總含量至少為〗0/ /、 夕為i/。，至少為30%，至少為8〇%， 至少為99%之原油進料的雜原子總含量。 一 於若干具體實例中’原油產物的含硫量可能最多為 9〇〇/。，最多為50%，最多為 夕馬 夕马10/。，或最多為5%之原油產物 的含硫量。於特定具體實例 彳中原/由產物具有含硫量至少 為1/)，至》為30¾，至少袁^ . 夕為80/〇，或至少為99%之原油 進料的含硫量。於若千呈鱗念，丨丄 ^ 右干具體實例中，原油產物的含硫量為 70 至 130%’ 80 至 12〇%，^ 主i20/。，或90至11〇%之原油進料的含 石荒量0 於若干具體實例中，；§、丄4 ^ ^ ^ ^ ^ 原油產物的總含氮量可能最多In a specific embodiment, the API ratio of the crude oil product produced by the contact between the crude oil feed and the catalyst under contact conditions is 70 to 130%, 80 to 80%. , 90 to 110%, or 100 to 130% of the crude APF ratio of crude oil feed. In a specific embodiment, the API gravity of the 'crude oil product is 14 to 40, 15 to 30, or 16 to 25. ^ In specific examples, crude oil products have a viscosity of up to 80%, or up to & 70% of the viscosity of the crude oil feed. In several instances, the 'crude oil product has a viscosity in the range of 10 to 60%, 20 to 40%, or 30 to 40% of the viscosity of the crude feed. In some specific 61 200533737 cases, the 'crude oil product's investigation accounted for 90% of the crude oil feed viscosity in Shengxian County. On the same day, the crude oil product's API ratio was 70 to 13%, ^ 90 to 110% Ambp of the crude oil feed or in several specific processes, crude oil products have a total heteroatom content of at most 90% and at most 50. / Once a. The maximum heteroatom content of each crude oil feed is 10% or 5% of the crude oil feed. In the specific example of ′, in the specific example, the crude product has a total heteroatom content of at least 0 // and i /. The total heteroatom content of the crude oil feed is at least 30%, at least 80%, and at least 99%. The sulfur content of the 'crude oil product may be up to 900 /, in several specific examples. , Up to 50% and up to Xi Ma Xi Ma 10 /. , Or sulfur content of up to 5% of crude oil products. In a specific specific example, the raw material of Zhongyuan / Yuan has a sulfur content of at least 1 /), ≧ 30¾, at least RMB ^. Xi is 80 / 〇, or at least 99% of the sulfur content of the crude oil feed. Yu Ruoqian said, in the specific example on the right, the sulfur content of crude oil products is 70 to 130% '80 to 120%, ^ main i20 /. , Or 90 to 110% of the crude rock content of crude oil feed 0 in some specific examples; §, 丄 4 ^ ^ ^ ^ ^ The total nitrogen content of crude oil products may be the most

90%，最多為80%，最多為】 々县夕达 取夕馬10%，或最多為5%之原油進〗 的總含氮量。於特定具體會么丨士 広、L女w ，、股貫例中，原油產物具有總含氮: 至少為1 乂，至少為30% ’ s 7丨、或只1,. 主 > 為80%，或至少為99%: 原油進料的總含氮量。 於若干具體貫例中，原油產物的驗性氮含量可能最多 為95%，最多為9G%，最多為駡，最多為1()%，或最多 為5%之原油進料的驗性氮含量。於特定具體實例中，原 油產物具有驗性氮含量至少》1%，至少&鳩，至少為 62 200533737 8〇%，或至少為99%之原油進料的驗性氮含量。 於若干具體實例中， 9〇%，最多為5〇%，畀夕劣 古虱里J犯取多為 5〇/ m 夕為30% ’最多為10%，或最多為 。之原油進料的含氧量。 且 有含氧量至少4 1%，至小泛 I〗中屑W由產物具 為9 v為30%，至少為80%，或至少 為9/°之原油進料的含氧量。於若干具體實例中，々、、“ 物的含氧量在丨至8QQ/，1Λ 胺貫例f原油產 ςΛ0/ 〇 0 至 70%，20 至 60% ,或 30 至 50 /〇之原油進料的含氧 原油產物的竣酸化人二：圍内。於若干具體實例中， 5〇m 含量可能最多為90%，最多為 物含旦牲1G/° ’或最多為5%之原油進料中的m酸化合 定具體實例中，原油產物具有㈣化合物總 *、，、 ％，至少為3〇0/。，至少為80%，或至少為99〇/ 之原油，料中的缓酸化合物總含量。 戈至 化人1若干具體實例中，可還原原油進料中的選定有機氧 张鉍祕女 實例中，㈣及7或«金屬鹽可在含 非竣敲有機氧化合物之前 酸與非_的有機氧化合一還 紅外線分析、質砸八妨爲 又已知的光譜法（例如 產物而鑑別。…’或乳相層析法)藉由分析原油 90%此最原Λ產物於特定具體實例中具有含氧量最多為 料的人氧1 ’最多為7G%，或最多&观之原油進 70。/二二而此原油產物的TAN最多為9〇%，最多為 特二’或最多為40%之原油進料的tan。於 ，、體實例中，原油產物具有含氧量至少為1%，至少 63 200533737 為30%，至少為80%，或 而此原油產物具有Tan 80%，或至少為99%之原 至少為99%之原油 至少為1 %，至少 油進料的TAN。 進料的含氧量， 為30%，至少為 βθ夂及/或羧酸 曰 油進料最多為90%，最多為 现s ΐ佔原 0 取多為5 00乂，+ nr 概，含非羧酸有機氧化合物的含 “多為 至120%，或90至11〇%之原油進 至，80 合物的範目@。 、 3非羧酸有機氧化 於若干具體實例中，用油方从Μ #90%, up to 80%, up to] Xixian Xida takes 10% of Xima, or up to 5% of the total nitrogen content of crude oil. In a specific specific meeting, Shi Jie, L N W, and the stock examples, the crude product has a total nitrogen content: at least 1%, at least 30% 's 7 丨, or only 1, the main> 80 %, Or at least 99%: The total nitrogen content of the crude feed. In certain specific examples, the test nitrogen content of crude oil products may be at most 95%, at most 9G%, at most curse, at most 1 ()%, or at most 5% of the crude nitrogen input of the crude feed. . In a specific embodiment, the crude oil product has a test nitrogen content of at least 1%, at least & dove, at least 62 200533737 80%, or at least 99% test oil content of crude oil feed. In some specific examples, 90%, the maximum is 50%, and the maximum number of J offenders in ancient louse is 50 / m, and 30% is the maximum, and the maximum is 10%. The oxygen content of the crude oil feed. And there is oxygen content of at least 41%, to small pan I, the crumb W from the product has 9 v is 30%, at least 80%, or at least 9 / ° of the crude oil feed oxygen content. In some specific examples, the oxygen content of 々, “, and“ is between 8 and 8 QQ /, and the crude oil produced by the crude oil is Λ0 / 〇0 to 70%, 20 to 60%, or 30 to 50 / 〇 crude oil. Complete acidification of oxygenated crude products of raw materials: within the enclosure. In some specific examples, the content of 50m may be up to 90%, the maximum is 1G / ° 'or 5% of crude oil feed. In the specific example of the m acid compound in the crude oil product, the crude oil product has a total of ㈣ compounds *, ,, and%, at least 300 /%, at least 80%, or at least 990 /% of crude oil. Total content: In several specific examples of Gezhihuaren 1, selected organic oxygen bismuth in the example of reducible crude oil feed, 7 and «metal salts can be acid and non- Organic oxidation combined with infrared analysis and mass spectrometry may also be known by spectrometry (such as product identification ... 'or milk chromatography) by analyzing 90% of the crude crude product in a specific specific In the example, the oxygen content with the most oxygen content 1 'is at most 7G%, or at most 70% of crude oil. Second, the TAN of this crude oil product is at most 90%, the maximum is at least two or 40% of the tan of the crude oil feed. In the example, the crude oil product has an oxygen content of at least 1%, at least 63 200533737 is 30%, at least 80%, or the crude oil product has Tan 80%, or at least 99% of the original at least 99% of the crude oil is at least 1%, at least the TAN of the oil feed. Oxygen in the feed The amount is 30%, at least βθ 夂 and / or carboxylic acid. The oil feed is at most 90%, the most current is 现 ΐ accounts for the original 0, which is more than 5 00 乂, + nr, containing non-carboxylic organic oxygen compounds. The crude oil containing "up to 120%, or 90 to 11% of crude oil, reached 80% of the compound @. , 3 non-carboxylic acid organic oxidation In several specific examples, use oil side from M #

“ Τ原、油產物於其分子結構中包含名 克原油產物有0.05至0.15克或〇〇 … 見的氣。此7? 油產物於其分子結構中可包含各古 ^ 匕3母克原油產物有0.8至〇 克或0.82至0.88克的碳。肩、、士吝％ 反原油產物之原子氫和原子碳白? 比（Η/C)可在70至130%，8〇至12〇%，或9〇至ιι〇%之肩 油進料的原子H/C比之範圍内。纟1〇i3G%之原油進申 的原子H/C比之範圍内的原油產物之原子H/c比係顯示庄 在過程中吸取及/或消耗的氫相當地少，及/或氫係現場生"The crude oil product contains gram crude oil in the molecular structure of 0.05 to 0.15 grams or 0 .... See this. The 7? Oil product may contain various crude oil products in its molecular structure. There are 0.8 to 0 g or 0.82 to 0.88 g of carbon. The ratio of atomic hydrogen and atomic carbon white (肩 / C) of the anti-crude product of anti-crude oil can be 70 to 130%, 80 to 120%, Or 90% to 100% of the atomic H / C ratio of the shoulder oil feed. 〇 10i3G% of the crude oil product within the range of the atomic H / C ratio of the atomic H / c ratio of the crude oil product is It shows that the hydrogen absorbed and / or consumed by Zhuang in the process is relatively small, and / or the hydrogen is generated on site.

產。 原油產物包含某個沸點範圍内的成分。於若干具體實 例中，原油產物在每克原油產物中包含··至少〇 〇〇 i克， 或0.001至〇·5克之沸程分佈在〇·ΐ〇ι MPa下最多為1〇〇 °c 的烴；至少0.001克，或0.001至〇·5克之沸程分佈在0·101 MPa下介於i〇〇°C和200°C之間的烴；至少〇_〇〇ι克，或〇·〇〇ι 至〇·5克之沸程分佈在0.101 MPa下介於200°C和300°C之 間的烴；至少0.001克，或0.001至0.5克之沸程分佈在〇· 101 64 200533737 MPa下介於300°c和40(TC之間的烴；及至少0.001克，或 〇·001至〇·5克之沸程分佈在0.101 MPa下介於400°c和538 °C之間的烴。 於若干具體實例中，原油產物在每克原油產物中包含 至少0.001克之沸程分佈在〇 1〇1 MPa下最多為i〇〇t的烴 及/或至少0·001克之沸程分佈在0.101 MPa下介於i〇〇°c 和200 C之間的煙。 於若干具體實例中，原油產物在每克原油產物中可含 有至少0.001克，或至少〇〇1克的石腦油。在其他具體實修 例中’原油產物可具有石腦油含量為每克原油產物中最多 0.6克，或最多〇·8克。 於若干具體實例中，原油產物具有餾分含量為至 13 0% ’ 80至120%，或90至110%之原油進料的餾分含量。 原油產物的餾分含量於每克原油產物中可在〇 〇〇〇〇1至〇.5 克’ 0.001至〇·3克，或〇·〇〇2克至0.2的範圍内。 於特定具體實例中，原油產物具有VGO含量為7〇至 130%，80至120%，或90至U0%之原油進料的vg◦含馨 量。於若干具體實例中，原油產物在每克原油產物中具有 0.00001 至 0_8 克，0_001 至 0.5 克，或 0.002 至 〇 4 克了或 0.001至0.3克之範圍内的VGO含量。 於若干具體實例中，原油產物具有殘留物含量為70至 130%，80至120%，或90至110%之斤油推粗从& 尽/由進枓的殘留物含 量。此原油產物可在每克原油產物中具有〇〇〇〇〇1至〇 8 克，0.0001 至 0.5 克，0.0005 至 0.4 克，〇 〇(H 至 〇 3 克·， 65 200533737 0.005 至 0.2 克，或 〇 〇1 至 〇 於特定呈髀杳 靶圍内的殘留物含量。 、特疋，、體霄例中，原油產 ⑽，心啊，或90至含量為70至 # , n ^ U〇/°之原油進料的MCR含 里，此原油產物具有c5瀝青質含量最多為州p 為8〇%，或最多為50%之原油進料的主併入旦0夕 定具體實例中’原油進料 5 :：里於特 少Α 6Π。/ -+· . 5歷月貝含1至少為10%，至 時原，由產。物二少為70%之原油進料的C5瀝青質含量，同Production. Crude products contain components in a range of boiling points. In several specific examples, the crude oil product contains at least 100,000 grams per gram of crude oil product, or a boiling range distribution of 0.001 to 0.5 grams at a maximum of 100 ° C at 0.001 MPa. Hydrocarbons; at least 0.001 grams, or 0.001 to 0.5 grams of boiling range distribution hydrocarbons between 0 ° C and 200 ° C at 0.101 MPa; at least 0,00 grams, or 0. 〇ι to 0.5 grams of hydrocarbons with a boiling range distribution between 0.1 ° C and 300 ° C at 0.101 MPa; at least 0.001 grams, or 0.001 to 0.5 grams of boiling range distributions between .101 64 200533737 MPa Hydrocarbons between 300 ° C and 40 ° C; and at least 0.001 grams, or 0.0001 to 0.5 grams of hydrocarbons with a boiling range distribution between 0.101 MPa and 400 ° c and 538 ° C. In several specific In the example, the crude oil product contains at least 0.001 grams of a boiling range distribution of hydrocarbons of up to 100 tons at 0.001 MPa per gram of crude product and / or a boiling range distribution of at least 0.001 grams of between 0.101 MPa Smoke between 100 ° C and 200 C. In several specific examples, the crude oil product may contain at least 0.001 grams, or at least 0.001 grams of naphtha per gram of crude oil product. In other specific practical examples, 'crude oil products may have a naphtha content of up to 0.6 grams, or up to 0.8 grams per gram of crude oil products. In several specific examples, crude oil products have a distillate content of up to 130%' Distillate content of 80 to 120%, or 90 to 110% of crude oil feed. Distillate content of crude oil products can range from 0.001 to 0.5 grams per gram of crude oil products, from 0.001 to 0.3 grams, Or in the range of 0.002 g to 0.2. In a specific embodiment, the crude oil product has vg of 70 to 130%, 80 to 120%, or 90 to U0% of the crude oil feed vg. In several specific examples, the crude oil product has a VGO content in the range of 0.00001 to 0_8 grams, 0_001 to 0.5 grams, or 0.002 to 0.04 grams or 0.001 to 0.3 grams per gram of crude oil products. In several specific examples The crude oil product has a residue content of 70 to 130%, 80 to 120%, or 90 to 110% of the crude oil. The residue content is as low as possible. This crude oil product can be produced per gram of crude oil product. In the range of 0.0001 to 08 g, 0.0001 to 0.5 g, 0.0005 to 0.4 Gram, 〇〇 (H to 〇3 grams ·, 65 200533737 0.005 to 0.2 gram, or 0.001 to 〇 within a specific range of the target content of residues. In particular, crude oil production, crude oil production Alas, heart, or 90 to the MCR content of a crude oil feed with a content of 70 to #, n ^ U0 / °, this crude product has a c5 asphaltene content of up to 80%, or a maximum of 50 % Of the crude oil feed master is incorporated into the specific example of the crude oil feed 'Crude oil feed 5 :: Li Yute Shao A 6Π. /-+ ·. 5 calendar month shellfish contains 1 at least 10%, to the time of origin, produced. C5 asphaltene content of crude oil feed with less than 70%

含:之矿圍内MCR含量在10至30%之原油進料的MCR 青；於若干具想實例中，減少原油進料… :二1 保持相對穩定的MCR含量可增加原油進 枓/、、、心產物混合物的穩定度。 旦於若干具體實例中’可結合c5瀝青質含量和MCR含 :以產生與原油進料中的高黏度成分相比介於原油產物的 :黏度成刀之間的數學關係。舉例而言，原油進料之q瀝 :質含量和原油進料之MCR含量的和可表示為s。原油產 勿之C5遞青質含量和原油產物之MCR含量的和可表示為Contains: MCR green of crude oil feed with MCR content of 10 to 30% in the mine; in several contrived examples, reducing crude oil feed ...: 2 1 Maintaining a relatively stable MCR content can increase crude oil feed, , The stability of the heart product mixture. In several specific examples, 'c5 asphaltene content and MCR content can be combined to produce a mathematical relationship between the viscosity of the crude product and the viscosity of the crude product compared to the high viscosity components in the crude feed. For example, the sum of the mass ratio of the crude oil feed and the MCR content of the crude oil feed can be expressed as s. The sum of the C5 cyanide content of crude oil products and the MCR content of crude oil products can be expressed as

::可比曰較這些和(S，與S)以估算原油進料中高黏度成分的 甲減少量。原油產物的S，可在i至99%，10至9〇%，或2〇 八 之S的範圍内。於若干具體實例中，原油產物之mcr 各里和C：5遞青質含量的比在1〇至3 〇，1_2至2 〇，或1·3 至1 · 9的範圍内。 於特疋具體實例中，原油產物具有MCR含量最多為 90%’最多為80%，最多為50%或最多為1〇%之原油進料 的MCR含量。於若干具體實例中，原油產物具有mcr含 66 200533737 量在1至80%，10至70%，20至60%，或30至5〇%之原 油進料的MCR含量之範圍内。原油產物於若干具體實例 中在每克原油產物中含有0.0001至0·1克，0.005至〇 〇8 克，或0.01至0.05克的MCR。 於若干具體實例中，原油產物在每克原油產物中包含 大於0克，但小於0.01克，0.000001至0·001克，或〇 〇〇〇〇1 至0 · 0 0 0 1克的觸媒總篁。觸媒在輸送及/或處理期間可幫 助使原油產物穩定化。觸媒可抑制腐蝕，抑制摩擦，及/或 提升原油產物的分水能力。可配置本文中所述的方法在處 _ 理期間將本文中所述的一或多種觸媒添加至原油產物。 與接觸系統100接觸所產生的原油產物具有和原油進 料性質不同的性質。這類性質可包括，但不限於：a)降低 TAN ; b)降低黏度；c)降低的總Ni/V/Fe含量；d)降低 的石氧、氮，或其組合之含篁，e)降低的殘留物含量； 0降低的Cs瀝青質含量；g)降低的MCR含量；h)增加 的API比重；i)降低的有機酸金屬鹽形態之金屬含量；或 j)其組合。於若干具體實例中，原油產物的一或多種性質 _ 與原油進料相比可選擇性地改變，而其他性質並沒有同樣 夕的改變或者實質上未改變。舉例而言，可能希望只選擇 性地減少原油進料中的TAN而不會顯著地改變其他成分 (例如硫、殘留物、Ni/V/Fe，或VG〇)的量。用這種方式， 接觸期間的氫吸取可依TAN的減少而被“濃縮，，，而不會作 用在其他成分的減少。因此，雖然使用較少的氫，但仍可 減v原油進料的TAN，因為較少量的這類氮同樣會用來減 67 200533737 少原油進料中的其他成分。舉例而言，如果劣質原油具有 高TAN，但含硫量為符合處理及/或輸送規格所能接受者， 則這類原油進料可更有效地處理以減少TAN而不需同樣也 減少硫。 本發明之一或多個具體實例中所用的觸媒可包含一或 多種塊狀金屬及/或載體上的一或多種金屬。該金屬可呈元 素形態或呈金屬化合物形態。本文中所述的觸媒可以前驅 物的形式導入接觸區，然後在接觸區中變成具有活性的觸 媒（舉例而言當硫及/或含硫的原油進料與前驅物接觸時）。 如本文敘述所使用的觸媒或觸媒組合可能是或可能不是商 品觸媒。涵蓋本文敘述所使用的商品觸媒實例包括HDS3 ; HDS22 ； HDN60 ； C234 ； C311 ； C344 ； C411 ； C424 ； C344 ； C444 ； C447 ； C454 ； C448 ； C524 ； C534 ； DN110 ； DN120 ； DN130； DN140； DN190； DN200； DN800； DN2118； DN2318 ； DN3100 ； DN3110 ； DN3300 ； DN3310 ； RC400 ； RC410 ； RN412 ； RN400 ； RN420 ； RN440 ； RN450 ； RN650 ； RN5210 ； RN5610 ； RN5650 ； RM430 ； RM5030 ； Z603 ； Z623 ； Z673 ； Z703; Z71 3; Z723; Z753;和 Z763,其可得自 CRI International，:: Comparatively, these sums (S, and S) are compared to estimate the reduction in A of the high viscosity components in the crude feed. The S of the crude product may be in the range of i to 99%, 10 to 90%, or S of 208. In several specific examples, the ratio of mcr to C: 5 diazine content of the crude oil product ranges from 10 to 30, 1_2 to 20, or 1.3 to 1.9. In a specific example, the crude oil product has an MCR content of a crude oil feed with a MCR content of at most 90% ', a maximum of 80%, a maximum of 50%, or a maximum of 10%. In some specific examples, the crude oil product has a mcr content of 66 200533737 ranging from 1 to 80%, 10 to 70%, 20 to 60%, or 30 to 50% of the MCR content of the crude oil feed. The crude product contains, in several specific examples, 0.0001 to 0.1 g, 0.005 to 2008 g, or 0.01 to 0.05 g of MCR per gram of crude product. In several specific examples, the crude oil product contains more than 0 grams, but less than 0.01 grams, 0.000001 to 0.001 grams, or 0.00000 to 0. 0 0.01 grams of catalyst per gram of crude oil product. bamboo grove. Catalysts can help stabilize crude oil products during transportation and / or processing. Catalysts can inhibit corrosion, inhibit friction, and / or increase the water-separation capacity of crude oil products. The methods described herein can be configured to add one or more of the catalysts described herein to crude oil products during processing. The crude oil product produced by contacting the contact system 100 has properties different from those of the crude oil feed. Such properties may include, but are not limited to: a) reduced TAN; b) reduced viscosity; c) reduced total Ni / V / Fe content; d) reduced stone oxygen, nitrogen, or thorium content in combination, e) Reduced residue content; 0 reduced Cs asphaltene content; g) reduced MCR content; h) increased API specific gravity; i) reduced metal content in organic acid metal salt form; or j) combinations thereof. In several specific examples, one or more properties of the crude product may be selectively changed compared to the crude feed, while other properties are not changed or substantially unchanged. For example, it may be desirable to selectively reduce only the TAN in a crude oil feed without significantly altering the amount of other components such as sulfur, residues, Ni / V / Fe, or VG0. In this way, the hydrogen uptake during the contact can be "concentrated" according to the reduction of TAN, without affecting the reduction of other components. Therefore, although less hydrogen is used, the v TAN, because a smaller amount of this nitrogen will also be used to reduce other components in the crude oil feed. 67 200533737 For example, if inferior crude oil has a high TAN, but the sulfur content is in line with the processing and / or transportation specifications. Acceptable, such crude oil feeds can be processed more effectively to reduce TAN without also reducing sulfur. The catalyst used in one or more specific examples of the present invention may include one or more bulk metals and / Or one or more metals on the carrier. The metal can be in the form of an element or a metal compound. The catalyst described herein can be introduced into the contact zone as a precursor, and then becomes an active catalyst in the contact zone (for example When sulfur and / or sulfur-containing crude oil feeds are in contact with precursors). The catalyst or catalyst combination used as described herein may or may not be a commodity catalyst. It covers the commodity catalysts used in this description. Examples of media include HDS3; HDS22; HDN60; C234; C311; C344; C411; C424; C344; C444; C447; C454; C448; C524; C534; DN110; DN120; DN130; DN140; DN190; DN18; DN800; DN800; DN3100; DN3110; DN3300; DN3310; RC400; RC410; RN412; RN400; RN420; RN440; RN450; RN650; RN5210; RN5610; RN5650; RM430; RM5030; Z; Z603 And Z763, which is available from CRI International,

Inc. (Houston，Texas，U.S.A·) 〇 於若干具體實例中，用來改變原油進料性質的觸媒包 含載體上的一或多種第5至10欄金屬。第5至10欄金屬 包括，但不限於飢、鉻、翻、鶴、锰、錯、銖、鐵、鈷、 鎳、釕、把、姥、锇、銀、鈾，或其混合物。該觸媒在每 克觸媒中可具有至少〇·〇〇〇1克，至少0.001克，至少0·01 68 200533737 克或是在0.0001至0_6克，0.005至0.3克，0.001至〇」 ' 克，或0.01至〇·〇8克的第5至10搁金屬總含量。於若干 具體實例中，該觸媒除了第5至10攔金屬之外，還包含 第1 5欄元素。第1 5攔元素的實例包括磷。該觸媒可具有 第15攔元素的總含量在每克觸媒中為〇·〇〇〇〇〇 1至〇1克， 0.00001 至 0.06 克，〇·00005 至 〇.〇3 克，或 0·0001 至 〇 〇〇1 克的範圍内。 於特定具體實例中，觸媒包含第6欄金屬。該觸媒在 每克觸媒中可具有至少0.0001克，至少0 01克，至少〇 〇2 # 克及/或在0.0001至0·6克，0.001至0.3克，〇 005至〇」 克，或0·01至0.08克的第6攔金屬總含量。於若干具體 實例中，觸媒在每克觸媒中包含0·0001至〇 〇6克的第6 攔金屬。於若干具體實例中，觸媒除了第6欄金屬之外， 還包含第1 5攔元素。 於若干具體實例中，觸媒包含第6攔金屬與第5欄及/ 或第7至1〇欄之一或多種金屬的組合。第6攔金屬與第5 欄金屬的莫耳比可在（Μ至2〇，丨至1〇，或2至5的範圍參 内。第6攔金屬與第7至1〇攔金屬的莫耳比可在〇1至π， 1至/〇 ’或2至5的範圍内。於若干具體實例巾，觸媒除 了第6欄金屬與第5欄及/或第7至1〇攔之一或多種金屬 的組合之外，€包含帛15_元素。於其他具體實例中， 觸媒包含第6攔金屬和第10攔金屬。觸媒中第10欄金屬 總量與第6攔金屬總量的莫耳比可在i至1〇,或2至$的 範圍内。於特定具體實例中，觸媒包含第5攔金屬和第1〇 69 200533737 欄金屬。觸媒中第10攔金屬總量與第5攔金屬總量的莫 耳比可在1至10，或2至5的範圍内。 於若干具體實例中，第5至1〇欄金屬係併入或沈積於 載體上以形成觸媒。在某些具體實例中，第5至1〇攔金 屬與第15攔元素之組合被併入或沉積在載體上以形成觸 媒。於金屬及/或元素受載的具體實例中，觸媒的重量包括 所有載體，所有金屬和所有元素。該載體可為多孔性而且 可匕括耐火性氧化物，多孔性碳基材料，沸石，或其組合。 耐火性氧化物可包括，但不限於氧化鋁、氧化矽、氧化矽_ :化鋁、氧化鈦、氧化鍅、氧化鎂，或其混合物。載體可 ^ ^ t t it ^ ^ Criterion Catalysts and Technologies LP (Houston, Texas，US A)。多孔性碳基材料包括，但不 限於活性碳及/或多孔石墨。沸石的實例包括Y沸石、p沸 :、絲光滞石、ZSM_5沸石和鎮鹼沸石。 章 製造商，例如Zeolyst(Vallevp p 業 y (Valley Forge, Pennsylvania, U S A )〇 於若干㈣實財係製備_讀使輯料有至少 體實例中至少170入’或至少180 A的平均孔徑。於特定且 ㈣:中，載體係藉由形成载體的水漿而製備。於若干且 體貫例中’將酸添加至衆料以促進聚干-的酸係以所需要的量i葬 水和稀釋 擠出浆料期望的柄…^ 加，以提供可 酉文、硫酸和鹽酸。 丨民於硝酸、乙 漿料可使用一般已知的觸媒擠出法 出和切割以形成擠出物。嗲棬*从〜 琛切打法擠 ®物錢A物可在5至26 70 200533737 至235 t：之範圍内的溫度下熱處理—段時間（例如〇·5至8 小時）及/或直到擠出物的濕度達到期望值為止。埶處理過 的擠出物可在800至〖200。(：或900至11〇〇之範圍内Inc. (Houston, Texas, U.S.A.). In several specific examples, the catalyst used to modify the properties of the crude oil feed contains one or more of the columns 5 to 10 metals on the support. Columns 5-10 include, but are not limited to, hungry, chromium, iron, crane, manganese, iron, baht, iron, cobalt, nickel, ruthenium, barium, thorium, thorium, silver, uranium, or mixtures thereof. The catalyst may have at least 0.0001 grams, at least 0.001 grams, at least 0.016 200533737 grams per gram of catalyst, or 0.0001 to 0-6 grams, 0.005 to 0.3 grams, and 0.001 to 0 grams. , Or 0.01 to 0.08 grams of the total metal content from 5th to 10th. In several specific examples, the catalyst contains elements in columns 15 in addition to the 5th to 10th metal. Examples of the 15th element include phosphorus. The catalyst may have a total content of the 15th element in the catalyst of 0.0000 to 0.01 g per gram of catalyst, 0.00001 to 0.06 g, 0.0005 to 0.03 g, or 0.05 g In the range of 0001 to 0.0001 grams. In a specific embodiment, the catalyst includes a column 6 metal. The catalyst may have at least 0.0001 grams, at least 0.01 grams, at least 0.002 grams per gram of catalyst and / or between 0.0001 to 0.6 grams, 0.001 to 0.3 grams, 0.005 to 0.005 grams, or The total content of the 6th metal from 0.01 to 0.08 grams. In a few specific examples, the catalyst contains from 0.0001 to 0.006 grams of the 6th metal per gram of catalyst. In some specific examples, the catalyst contains elements 15 to 15 in addition to the metal in column 6. In some specific examples, the catalyst comprises a combination of metal 6 and one or more metals in columns 5 and / or columns 7-10. The molar ratios of the 6th metal to the 5th metal can be in the range of (M to 20, 1 to 10, or 2 to 5). The 6th metal to the 7th to 10th metal. The ratio can be in the range of 〇1 to π, 1 to / 〇 ′ or 2 to 5. In some specific examples, the catalyst except one of the metal in column 6 and one of column 5 and / or 7 to 10 or In addition to the combination of various metals, the europium contains 15 elements. In other specific examples, the catalyst includes the 6th metal and the 10th metal. The total amount of metal in column 10 and the 6th metal in the catalyst Morse ratio can be in the range of i to 10, or 2 to $. In a specific specific example, the catalyst includes the 5th metal and the 1069 200533737 metal. The total amount of the 10th metal in the catalyst and The molar ratio of the total amount of the fifth metal can be in the range of 1 to 10, or 2 to 5. In some specific examples, the metal systems of columns 5 to 10 are incorporated or deposited on the carrier to form a catalyst. In some specific examples, the combination of the 5th to 10th metal and the 15th element is incorporated or deposited on the carrier to form a catalyst. In the specific example of the metal and / or element supported, the catalyst's weight The amount includes all supports, all metals and all elements. The support may be porous and may include refractory oxides, porous carbon-based materials, zeolites, or combinations thereof. Refractory oxides may include, but are not limited to, alumina , Silicon oxide, silicon oxide: aluminum oxide, titanium oxide, hafnium oxide, magnesium oxide, or a mixture thereof. The carrier can be ^ ^ tt it ^ ^ Criterion Catalysts and Technologies LP (Houston, Texas, US A). Porous carbon-based Materials include, but are not limited to, activated carbon and / or porous graphite. Examples of zeolites include Y zeolite, zeolite, mordenite, ZSM_5 zeolite, and soda zeolite. Manufacturers, such as Zeolyst (Vallevp y (Valley Forge (Pennsylvania, Pennsylvania, USA). Prepared in several financial institutions, the reading material has an average pore size of at least 170 in or at least 180 A. In specific and ㈣ :, the carrier is formed by the formation of the carrier. Water slurry is prepared. In several examples, the acid is added to the crowd to promote the polymerization of the acid-based system in the required amount of water and dilute the desired handle of the extruded slurry ... ^ to provide Available in obituary, sulfuric acid and Acid. 丨 The nitric acid and B slurry can be extruded and cut to form an extrudate using commonly known catalyst extrusion methods. 70 200533737 to 235 t: heat treatment at a temperature in the range—for a period of time (for example, 0.5 to 8 hours) and / or until the humidity of the extrudate reaches the desired value. The treated extrudate can be between 800 and 〖 200. (: or within the range of 900 to 1100

的溫度下進一步熱處理以形成具有平均孔徑至少為i5〇A 的載體。 ^ 於特定具體實例中，載體包含γ氧化鋁、θ氧化鋁、§氧 化鋁、α氧化鋁，或其混合物。γ氧化鋁、δ氧化鋁、α氧化 鋁，或其混合物的量於每克觸媒載體中可在〇〇〇〇1至〇 99Further heat treatment at a temperature of 50 ° C. to form a support having an average pore size of at least i50A. ^ In a specific embodiment, the support comprises gamma alumina, theta alumina, § alumina, alpha alumina, or a mixture thereof. The amount of γ alumina, δ alumina, α alumina, or a mixture thereof may be between 0.001 and 0.999 per gram of the catalyst carrier.

克，0.001至0.5克’ 0.01至ο」克的範圍内，或最多為〇 克，其藉由X射線繞射測定。於若干具體實例中，載體夺 單獨含有或結合其他形態的氧化鋁，θ氧化鋁含量於每身 ，體中在（Μ至0.99克，〇·5至〇·9克，或〇6至〇8克^ 範圍内，其藉由X射線繞射測定。於若干具體實例中，韋 體可含有至少0.1克，至少0.3克，至少〇 5克，或至少〇 克的Θ氧化鋁’其藉由χ射線繞射測定。Gram, in the range of 0.001 to 0.5 gram '0.01 to 0 gram, or at most 0 gram, which is measured by X-ray diffraction. In some specific examples, the carrier alone or in combination with other forms of alumina, theta alumina content in each body, in the body (M to 0.99 g, 0.5 to 0.9 g, or 〇6 to 〇8 It is measured by X-ray diffraction in the range of gram ^. In some specific examples, the Weiwei body may contain at least 0.1 grams, at least 0.3 grams, at least 0.05 grams, or at least 0 grams of Θ alumina. Diffraction measurement.

受載觸媒可使用一般已知的觸媒製備技術製備。觸媒 製備法的實例係見述於頒予Gabriel〇v等人的美國專利案 唬 6,218,333 ;頒予 Gabrielov 等人的 6,29〇 841 ;頒予 B〇〇n 等人的5,744,025，及頒予Bhan的美國專利申請案公告案 號 20030111391 。 於若干具體實例中，載體可用金屬浸潰以形成觸媒。 於特疋具體實例中，在浸潰金屬之前，使載體於4〇〇至 C，450至1000 °c，或6〇〇至9〇〇之範圍内的溫度下 進仃熱處理。於若干具體實例中，浸潰助劑可在製備觸媒 71 200533737 期間使用。浸潰助劑 酸（贿A)、氨，或其混合^括摔樣酸成分、乙二胺四乙 於特定具體實例中， 加或換入已熱處理二觸：可藉由將第…。棚金屬添 ρ , ^ ^ 成形的载體混合物（“覆蓋，，）而形成。在 已熱處理成形的载體頂 Λ, ^ . . 上覆盍金屬以具有實質或相對均 ^ /辰度的金屬通常會 ^ w 、予觸媒有利的催化性質。在每次覆 皿孟屬後熱處理已忐 &你田资— ^的载體會有改善觸媒催化活性的傾 向。使用覆蓋法製借鎚册k A 觸某的方法係見述於頒予Bhan的美The supported catalyst can be prepared using generally known catalyst preparation techniques. Examples of catalyst preparation methods are described in U.S. Patent No. 6,218,333 issued to Gabrielov et al .; 6,29,841 issued to Gabrielov et al .; 5,744,025 issued to Bonon et al., And Bhan's U.S. Patent Application Publication No. 20030111391. In several specific examples, the carrier can be impregnated with a metal to form a catalyst. In a specific example, before the metal is impregnated, the support is subjected to a heat treatment at a temperature in the range of 400 to C, 450 to 1000 ° C, or 600 to 900. In several specific examples, the impregnation aid can be used during the preparation of the catalyst 71 200533737. Impregnation aids Acid (Brilliance A), ammonia, or a mixture thereof including stilbene-like acid components, ethylenediamine tetraethyl. In specific examples, it can be added or replaced by a heat-treated two-touch method. Shed metal is formed by adding ρ, ^ ^ formed carrier mixture ("covering ,,). The top of heat-treated formed carrier Λ, ^... Is covered with rhenium metal to have a substantially or relatively uniform metal Generally, the catalyst has favorable catalytic properties. After each coating, the heat treatment has been performed on the carrier, and the carrier will have a tendency to improve the catalytic activity of the catalyst. The overlay method is used to make a hammer book. A method of touching something is described in the beauty awarded to Bhan

卜月节A。案垅2〇〇3〇111391。 苐5至1〇棚么愿』 忐筮 、’和載體可用適當的混合設備混合以形 成弟5至1〇攔金属/ 、、B ^ "载體混合物。第5至10攔金屬/載體 混合物可使用適當的、、曰 勺k 、吞炫 、此6设備混合。適當的混合設備實例 匕枯淚筒、固定殼或描 々、,· < 9、研磨混合機（例如分批式或連續 式）、衝擊式混人她 轉、B入& ° 、’以及能適當形成第5至10欄金屬/載 體〜合物的任何i仙— '、—叙已知混合器，或一般已知裝置。 %将疋具體實例中January Festival A. Case 垅 200301111391.苐 5 to 10 sheds? 愿, ’, and the carrier can be mixed with a suitable mixing device to form a 5 to 10 metal /, and B ^ carrier mixture. The 5th to 10th metal / carrier mixtures can be mixed using the appropriate equipment. Examples of suitable mixing equipment: daggers, fixed shells or traces, < 9, grinding mixers (e.g. batch or continuous), impact mixers, B into & Any suitable mixer capable of forming metals / supports in columns 5 to 10-',-known mixers, or generally known devices. % Will be in the specific example

^ 使材料混合直到第5至10攔金屬實 貝上均勻分散在載體中為止。 於若干具體實例中，在結合载體與金屬之後，使觸媒 在 150 至 7SΠ °n 〇至740 °c，或400至730 °C的潘 度下進行熱處理。 ;干〆、體實例中，觸媒可在熱空氣及/或富氧空氣存 =下’於介於400 t和咖。c之範圍内的溫度下進行熱 捫八/移除揮發性物f，以便使至少—部分的第5至1〇 攔金屬轉化成對應的金屬氧化物。 72 200533737 然而在其他具體實例中，觸媒可在空氣存在下於35至 ' 500 C (例如低於300 °C，低於4〇〇或低於5〇〇艺）之 範圍内的溫度下熱處理達丨至3小時之範圍内的一段時 間，以移除大多數的揮發性物質而不會使第5至ι〇欄金 屬轉化成金屬氧化物。藉由此種方法所製備的觸媒通常稱 為“未煅燒過的，，觸媒。當以這種方式結合形成硫化物法製 備觸媒時，活性金屬實質上可分散在載體中。這類觸媒的 製備係見述於頒予Gabrielov等人的美國專利案號 6,218,333，及頒予 Gabrielov 等人的 6,29〇,841。 籲 於特定具體實例中，θ氧化銘載體可結合第5至1〇欄 金屬以形成Θ氧化鋁載體/第5至1〇欄金屬混合物。❸氧化 鋁載體/第5至1〇攔金屬混合物可在至少4〇〇。〇的溫度下 熱處理以形成具有中位孔徑至少$ 23g Α之孔徑分佈的觸 媒。典型而言，這類熱處理在最高為12〇〇 的溫度下進 行〇^ The materials are mixed until the metal shells 5 to 10 are evenly dispersed in the carrier. In some specific examples, after the carrier and the metal are combined, the catalyst is heat-treated at a temperature of 150 to 7 °, 0 to 740 ° c, or 400 to 730 ° C. In dry and bulk examples, the catalyst can be stored in hot air and / or oxygen-enriched air at a temperature between 400 t and ca. Thermal treatment is performed at a temperature in the range c to remove / remove volatiles f in order to convert at least part of the 5th to 10th metal to the corresponding metal oxide. 72 200533737 However, in other specific examples, the catalyst can be heat treated in the presence of air at a temperature in the range of 35 to '500 C (for example, less than 300 ° C, less than 400 or less than 500 ° C). For a period of time ranging from 3 to 3 hours to remove most of the volatiles without converting the 5th to 5th column metals into metal oxides. The catalysts prepared by this method are commonly referred to as "uncalcined, catalysts. When combined in this way to form catalysts, the active metal can be substantially dispersed in the carrier. This type of catalyst The preparation of the catalyst is described in U.S. Patent No. 6,218,333 issued to Gabrielov et al. And 6,29〇, 841 issued to Gabrielov et al. In specific examples, the theta oxide carrier can be combined with 10 bars of metal to form a Θ alumina support / 5 to 10 metal mixtures. ❸ alumina support / 5 to 10 metal mixtures can be heat treated at a temperature of at least 400. Catalysts with a pore size distribution of at least $ 23g A. Typically, this type of heat treatment is performed at a temperature of up to 1200.

於若干具體實例中，載體（商品載體或如本文敘述所 莆之載體）可與X載觸媒及/或塊狀金屬觸媒結合。於若 具體實例中，受載觸媒可包含第15襴金屬。舉例而言 文載觸媒及/或塊狀金屬觸媒可壓碎成平均粒徑為i至 微米，2至45微米，…4〇微米的粉末。該粉末可 載體結合以形成埋人金屬觸媒。於若干具體實例中，粉 可與载體結合’然後使用標準技術擠出，以形成具有中 孔徑在80至200 Λ戎90 $ λ 忒川至180人，或120至130 Λ的 圍内之孔徑分佈的觸媒。 73 200533737 使觸媒與載體接觸於若干具體實例中可容許至少一部 分的金屬存在於埋入金屬觸媒表面下方（例如埋入載體 :)’而導致在表面上比用其他方法存在於未埋人金屬觸媒 者有更少的金屬。於若干具體實例中，在觸媒表面上具有 較少金屬者會由於在使用期間容許至少一部分的金屬移到 觸媒表面而延長觸媒的壽命及/或催化活性。金屬可藉由觸 媒與原油進料接觸期間觸媒表面的侵蝕而移到觸媒表曰面。In some specific examples, the carrier (commercial carrier or carrier as described herein) may be combined with an X-loaded catalyst and / or a bulk metal catalyst. In a specific example, the supported catalyst may include a 15th metal. For example, the text catalyst and / or bulk metal catalyst can be crushed into powders with an average particle size of i to micron, 2 to 45 micron, ... 40 micron. The powder can be combined with a carrier to form a buried metal catalyst. In several specific examples, the powder can be combined with a carrier 'and then extruded using standard techniques to form a pore size with a mesopore size ranging from 80 to 200 Λ Rong 90 $ λ Xichuan to 180 people, or 120 to 130 Λ Distributed catalyst. 73 200533737 Contacting the catalyst with the carrier in several specific examples may allow at least a portion of the metal to exist below the surface of the buried metal catalyst (eg, the carrier is buried): 'which results in the surface being present in the unburied person by other methods Metal catalysts have less metal. In some specific examples, those with less metal on the catalyst surface will extend the life and / or catalytic activity of the catalyst by allowing at least a portion of the metal to move to the catalyst surface during use. Metals can be moved to the surface of the catalyst by erosion of the catalyst surface during contact between the catalyst and the crude feed.

夾雜及/或混合觸媒成分於若干具體實例中會使第6棚 氧化物晶體結構中帛6欄金屬的結構順序變成埋入觸媒晶 體結構中帛6欄金屬的實質隨機順序。第6攔金屬的順序 可使用粉I X射、線繞射法決定。與金屬氧化物中金屬元素 的順序相比，觸媒中金屬元素的順序可藉由比較第6攔氧 化物之X射線繞射光譜中第6攔金屬波峰的順序和觸媒之 X射線繞射光譜中帛6攔金屬波峰的順序而決^。從與X 射線繞射光譜中第6攔金屬有關的圖案增寬及/或無圖案來 看可估异在晶體結構中實質上無規排列的第6欄金屬。 化鋁/第6欄二氧化物混合物可在至少5 3 8乞（1⑻〇卞）的 溫度下熱處理以產生在χ射線繞射光譜中不會顯示出二氧 化鉬圖案（例如沒有D⑽波峰）的觸媒。 於若干具體實例中’觸媒的特徵可能是孔隙結構。各 種孔隙結構的參數包括，但不限於孔徑、孔體積、表面積， 舉例而言，三氧化鉬與具有中位孔徑至少為18〇 A的 氧化鋁载體可結合形成氧化鋁/三氧化鉬混合物。三氧化鉬 具有明確圖案（例如明確的D㈣、及/或D3。。波峰）。氧 74 200533737 或其組合。觸媒可具有與孔徑相對的孔徑總量分佈。孔徑' 分佈的中位孔徑可在30至iOOO A、50至500 A，或60至 300 A的範圍内。於若干具體實例中，每克觸媒中包含至 乂 0.5克γ氧化鋁的觸媒具有中位孔徑在6〇至2〇〇 A ; 9〇 至180 A，100至140入，或⑶至13〇人之範圍内的孔徑 分佈。於其他具體實例中’每克觸媒中包含至少〇1克_ 化鋁的觸媒具有中位孔徑在18〇至5〇〇 A，2〇〇至3〇〇人， 或230至250 A之範圍内的孔徑分佈。於若干具體實例中， 孔徑分佈的中位孔徑至少為12〇人，至少為15〇人至少為籲 ⑽A’至少為200 A，至少為220 A，至少為23〇 A，或 至少為300 A。這類中位孔徑典型而言最多為1〇〇〇A。 觸媒可具有中位孔徑至少為60 A或至少為9〇 A的孔 徑分佈。於若干具體實例中，觸媒具有中位孔徑在9〇至18〇 A，100至140人，或120至130 A之範圍内的孔徑分佈， 該孔徑分佈中至少60%的總孔數具有在45人、35人，或25人 之中位孔徑範圍内的孔徑。於特定具體實例中，觸媒具有 中位孔徑在70至180 A之範圍内的孔徑分佈，該孔徑分佈 _ 中至少60%的總孔數具有在45 A、35人，或25人之中位 孔徑範圍内的孔徑。 於孔徑分佈之中位孔徑至少為丨80 A，至少為2〇〇人， 或至少為230 A的具體實例中，該孔徑分佈中有超過6〇% 的總孔數具有在50 Λ、70 A，或90 A之中位孔徑範圍内 的孔徑。於若干具體實例中，觸媒具有中位孔徑在1 至 500 A，200 至 400 A，或 230 至 300 A 之誌问〜h x Λ <乾圍内的孔徑分 75 200533737 佈，該孔徑分佈中至少6()%的總孔數具有在5q α、a， 或90 A之中位孔徑範圍内的孔徑。 於若干具體實例中，孔的孔體積可為至少G 3⑽3/g、 至4 〇·7 cm3/g或至少為0·9 cm3/g。於特定具體實例中， 孔的孔體積可在〇.3至0.99cmVg，〇4至〇8cm3/g，或〇5 至0.7 cm3/g的範圍内。 具有中位孔徑在90至18G A之範圍内的孔徑分佈之觸 媒於若干具體實例中可具有至少為1〇〇m2/g，至少為12〇 m /g，至少為no m2/g，至少為22〇或至少為2川w化φ 的表面積。這類表面積可在1〇〇至3〇〇 mVg，丨2〇至27〇 m2/g，130 至 250 m2/g，或 170 至 22〇 m2/g 的範圍内。 於特定具體實例中，具有中位孔徑在18〇至3〇〇人之 範圍内的孔徑分佈之觸媒可具有至少為6〇m2/g，至少為 m化，至少為100 m2/g，至少為120 m2/g，或至少為27〇 的表面積。這類表面積可在6〇至3〇〇 mVg，9〇至28〇 η%， 1〇〇 至 270 m2/g ’ 或 120 至 250 m2/g 的範圍内。 於特定具體實例中，觸媒係以成形形態，例如片粒狀、魯 圓桎狀，及/或擠出物存在。該觸媒典型而言具有在5〇至 5〇〇 Ν/cm，60 至 400 N/cm，100 至 350 N/cm，200 至 300 cm，或220至280N/cm之範圍内的平板抗碎強度。 於若干具體實例中，觸媒及/或觸媒前驅物係使用該項 技術中已知的技術（例如ACTICATTM法，CRI Internati〇nal， nc·)琉化以形成金屬硫化物（在使用之前）。於若干具體實 中觸媒可乾燥然後使其硫化。或者，觸媒可藉由觸媒 76 200533737 :包含含，化合物之原油進料的接觸而在現場硫化。現場 &化可在虱存在下使用氣態硫化氫，或液相硫化劑，例如 錢硫化合物（包括院基硫、多硫化合物、硫醇和亞楓）。 %外硫化法係見述於 、頒予Seamans等人的美國專利案號 5,468,372 ’ 及頒予 Seamans 等人的 5,688,736。 、：特定具體實例中’第一類觸媒（“第一種觸媒，，）包含 與載體結合的第5 i 10攔金屬，且具有中位孔徑在150 至/50A之範圍内的孔徑分佈。第_種觸媒可具有至少1〇〇 :’g的表面積。第一種觸媒的孔體積可至少為0」cm3/g。 · 第種觸媒可具有γ氧化铭含量在每克的第一種觸媒中至少 ，〇·5克的γ氧化銘，典型而言最多為〇·9999克的丫氧化鋁。 第種觸媒於若干具體實例中在每克觸媒中具有OOOW至 •1克之範圍内的第6攔金屬總含量。第一種觸媒能移除 原油進料中的一部分Ni/V/Fe，移除造成原油進料之TAN 的一部分成分，移除原油進料中至少一部分的c5瀝青質， 、示原油進料中至少一部分的有機酸金屬鹽形態之金屬， 或其組合。當原油進料與第一種觸媒接觸時，其他性質（例 _ 如含硫量、VG0含量、API比重、殘留物含量，或其組合） 可能只表現出相當少量的變化。能選擇性地改變原油進料 的丨生貝而同時只相當少量地改變其他性質可容許原油進料 進行更有效地處理。於若干具體實例中，一或多種第一種 觸媒可以任意順序使用。 於特定具體實例中，第二類觸媒（“第二種觸媒，，）包含 /、载體結合的第5至10欄金屬，具有中位孔徑在9〇至1 8〇 77 200533737 A之範圍内的孔徑分佈。該第：種觸媒的孔徑 60%的總孔數具有在45 A 夕 T I札從靶圍内的。 當接觸條件下原油進料斑第— ^在適 逆t十興弟一種觸媒的接觸可生 進料的同樣性質相比，且有顯荖 屋/、原油 二η H 改變之選定性質（例如ΤΑΝ) 而同日守其他性質只有少量改變的 3夕里汉爻的原油產物。於若干且 例中，在接觸期間可存在氫源。 /、 、第二種觸媒可減少造成原油進料之TAN的至少八 成分，造成相對高黏度的至少一 刀 铷夕=丨 I刀成刀，及減少原油產 物之至V-部分的Nl/V/Fe含量。此外，原油進料鱼第二 種觸媒的接觸可生產與原油進料的含硫量相比， ::::量改變的原油產物。舉例而言，原油產物；具；： 至13G%之原油進料的含硫量。該原油產物與 之由進枓相比，在館分含量、VG0含量，和殘留物含量方 ，也可能只表現出相當少量的變化。 人旦於若干具體實例中，原油進料可具有相對低的而職 :里(例如最多為5〇 wtppm)，但相對高的TAN、瀝青質含 :有機酸金屬鹽形態的金屬含量。相對高的UN、(例 夕為0.3的TAN)可能使得原油進料為輸送及/或精煉 所不能接受。具有相對高〜歷青質含量的劣質原油在處理 月門”具有相對低Cs瀝青質含量的其他原油相比，可能會 表現出較低的穩定性。原油進料與第二種觸媒的接觸可移 除原油進料中造成TAN的酸性成分及/或c5瀝青質。於若 、「-實例中，減少cs瀝青質及/或造成TAN的成分與原 油進料的黏度相比，可能會降低原油進料/總產物混合物的 78 200533737 黏度。於特定具體實例中，第二種觸媒的—或多種組合當 :來：理本文中所述的原油進料時，可提高總產物/原油產 ?混5物的穩定性，增加觸媒壽命，提供原油進料之复的 彔小淨吸取。 於若干具體實例中，第三類觸媒（“第三種觸媒，，）可藉 =使載體與第6攔金屬結合產生觸媒前驅物而獲得。觸媒 河驅物可在-或多種含硫化合物的存在下在低me (例如低於482 〇C ί西降πτ丄& L )的服度下加熱一段相當短的時間以生成 未煅t過的第二種觸媒。典型而言，觸媒前驅物係加埶到 =100。°達2小時。於特定具體實例中，第三種觸媒在 母克觸媒中可具有0.001至0.03克，〇 〇〇5至〇 〇2克或 0.008至CMH克之範圍内的第15欄元素含 當用=理本文中所述的原油進料時，可表現出顯著的^ !生和穩疋性。於若干具體實例中’觸媒前驅物係於—或多 種硫，合物的存在下在低於_ t的溫度下加熱。 第三種觸媒可減少造成原油進料之TAN的至少一部分 成分’減少至少-部分的有機酸金屬鹽形態之金屬，心 原油產物的Ni/V/Fe含量，及降低原油產物的黏度。此外， 原油進料與第二種觸媒的接觸可生產與原油進料的含硫量 ^目比:其含硫量相當少量改變及具有原油進料之氫的相對 旦平吸取的原油產物。舉例而言，原油產物可具有含硫 為70%至130%之原油進料的含硫量。使用第三種觸媒 :生產的原油產物與原油進料相比，纟Αρι比重、餾分含 VGO含里，和殘留物含量方面，也可能只表現出相當 79 200533737 少量的變化。降低原油進料& TAN、有機酸金屬鹽形能之 金屬、Nl/V/Fe含量，及黏度且同時只少量改變Αρι比=、 餾分含量、VGO含量’和殘留物含量的能力可容許原油產 物為各種處理設備所使用。 / .第三種觸媒於若干具體實例中可降低原油進料之至少 -部分的MCR含量，而同時保持原油進料/總產物的穩定 性。於特定具體實例中，第三種觸媒在每克觸媒中W有 在 0.0001 至 0.1 克，0·005 至 0.05 克，或 〇 〇〇1 至"i 克 之範圍内的第6攔金屬含量以及在0._至㈣5克，〇〇〇5 至0.03克，或〇 〇〇1至〇 〇1吉 益 旦 i兑之乾圍内的第10欄金屬含 里。第6和1〇攔金屬觸媒可促使減少至少一 至_。〇或⑽i 450 t之範圍内的溫度和^在至1〇 :m8MPa，或2至5MPa之範圍内的壓力下造成 原/由進料中之MCR的成分。 於特定具體實例中’第四類觸媒（“第四種觸媒，，）包含 ^乳化I呂載體結合的帛5攔金屬。第四種觸媒具有中位 :至少A180A的孔徑分佈。於若干具體實例中，第四 =某的中位孔經可至少為220A，至少為230人，至少為 〇 A，或至少為300 A〇該恭骋士 載體在母克載體中可包含至少 鋁〜至夕〇·5克’至少0·8克，或至少0.9克的Θ氧化 為。細種觸媒於若干具體實例中可包含每克㈣中最多 笛克的第5攔金屬’且每克觸媒中至少為克的 搁金屬。於特定具體實例中，第5搁金屬為飢。 於若干具體實例中，在與第四種觸媒接觸之後，原油 80 200533737 進㈣附加觸媒接觸。該附加觸媒可為下 者·第一種觸媒、第二種觸媒、第三種觸媒、第^夕 弟五種觸媒、弟六種觸媒、第七種觸★某、 ： 品觸媒，或其組合。 中所述的商 於右干具體實例中，氫可在原油進料與第 觸期間於_至彻。c，32u彻。C，或咖至^ 的溫度下產生。由這類接觸所生產的原油產物可具有T聽 最多為90〇/。，最多為80%，最多為50%，或最多為贈 原油進料的TAN。氫氣發生可在U5〇Nm3/m3, ι〇至The inclusion and / or mixing of the catalyst components in several specific examples will cause the structural sequence of the 帛 6 column metal in the 6th shed oxide crystal structure to become a substantially random order of the 帛 6 column metal embedded in the catalyst crystal structure. The order of the 6th metal can be determined by powder I X-ray and wire diffraction methods. Compared with the order of the metal elements in the metal oxide, the order of the metal elements in the catalyst can be compared by comparing the order of the 6th metal peak in the X-ray diffraction spectrum of the 6th oxide and the X-ray diffraction of the catalyst. The order of 帛 6 metal peaks in the spectrum depends on ^. From the pattern widening and / or non-patterning related to the sixth metal in the X-ray diffraction spectrum, it can be estimated that the metal in the sixth column is substantially randomly arranged in the crystal structure. Aluminium / column 6 dioxide mixtures can be heat treated at a temperature of at least 5 3 8 (1⑻〇 卞) to produce a material that does not show a molybdenum dioxide pattern in the X-ray diffraction spectrum (for example, without D⑽ peaks). catalyst. In several specific examples, the catalyst may be characterized by a pore structure. Various pore structure parameters include, but are not limited to, pore size, pore volume, and surface area. For example, molybdenum trioxide can be combined with an alumina support having a median pore size of at least 180 A to form an alumina / molybdenum trioxide mixture. Molybdenum trioxide has a well-defined pattern (such as well-defined D㈣, and / or D3 ... wave peak). Oxygen 74 200533737 or a combination thereof. The catalyst may have a total pore size distribution as opposed to a pore size. Aperture 'distributions can have median pore sizes ranging from 30 to 10,000 A, 50 to 500 A, or 60 to 300 A. In some specific examples, the catalyst containing 0.5 g of gamma alumina per gram of catalyst has a median pore size of 60 to 2000 A; 90 to 180 A, 100 to 140 A, or ⑶ to 13 Pore size distribution in the range of 〇 person. In other specific examples, the catalyst containing at least 0.01 g aluminum oxide per gram of catalyst has a median pore size of 180 to 500 A, 200 to 300 people, or 230 to 250 A. Aperture distribution in the range. In several specific examples, the median pore size of the pore size distribution is at least 120 people, at least 150 people, at least 200 A, at least 200 A, at least 220 A, at least 23 A, or at least 300 A. Such median pore sizes are typically up to 1000 A. The catalyst may have a pore size distribution with a median pore size of at least 60 A or at least 90 A. In several specific examples, the catalyst has a pore size distribution with a median pore size in the range of 90 to 180 A, 100 to 140 people, or 120 to 130 A. At least 60% of the total number of pores in the pore size distribution has Apertures in the median aperture range of 45, 35, or 25 people. In a specific embodiment, the catalyst has a pore size distribution with a median pore size in the range of 70 to 180 A, and at least 60% of the pore size distribution_ has a total pore size of 45 A, 35 people, or 25 people Aperture within the aperture range. The median pore size in the pore size distribution is at least 80 A, at least 200 people, or at least 230 A. In the specific example of the pore size distribution, more than 60% of the total number of pores has 50 Λ, 70 A , Or an aperture in the 90 A median aperture range. In some specific examples, the catalyst has a median pore diameter of 1 to 500 A, 200 to 400 A, or 230 to 300 A ~ hx Λ < Aperture within the dry wall is divided into 75 200533737 cloth. At least 6 ()% of the total number of pores have a pore size in the 5q α, a, or 90 A median pore size range. In some specific examples, the pore volume of the pores may be at least G3⑽3 / g, to 40.7 cm3 / g, or at least 0.9 cm3 / g. In specific embodiments, the pore volume of the pores may be in the range of 0.3 to 0.99 cmVg, 0.4 to 0.8 cm 3 / g, or 0.05 to 0.7 cm 3 / g. A catalyst having a pore size distribution with a median pore size in the range of 90 to 18 G A may have at least 100 m2 / g, at least 120 m / g, at least no m2 / g, at least A surface area of 22 or more. Such surface areas can range from 100 to 300 mVg, 20 to 2700 m2 / g, 130 to 250 m2 / g, or 170 to 2200 m2 / g. In a specific embodiment, a catalyst having a pore size distribution with a median pore size in the range of 180 to 300 people can have at least 60 m2 / g, at least m, at least 100 m2 / g, at least A surface area of 120 m2 / g, or at least 270. Such surface areas can range from 60 to 300 mVg, 90 to 28 η%, 100 to 270 m2 / g ', or 120 to 250 m2 / g. In a specific embodiment, the catalyst exists in a shaped form, such as a pellet shape, a round shape, and / or an extrudate. The catalyst typically has flat shatter resistance in the range of 50 to 500 N / cm, 60 to 400 N / cm, 100 to 350 N / cm, 200 to 300 cm, or 220 to 280 N / cm. strength. In several specific examples, catalysts and / or catalyst precursors are chemically transformed to form metal sulfides using techniques known in the art (eg, ACTICATTM method, CRI International, nc ·) (before use) . The catalyst can be dried and then vulcanized in several specific applications. Alternatively, the catalyst can be vulcanized in situ by contacting Catalyst 76 200533737: a crude oil feed containing a compound. On-site & chemical can use gaseous hydrogen sulfide in the presence of lice, or liquid sulfiding agents, such as sulphur compounds (including sulphur, polysulfides, thiols, and maple). % The external vulcanization method is described in U.S. Patent No. 5,468,372 'issued to Seamans et al. And 5,688,736 issued to Seamans et al. :: In a specific specific example, the first type of catalyst ("the first type of catalyst,") contains a 5 i to 10 metal bonded to the carrier, and has a pore size distribution with a median pore size in the range of 150 to / 50A The first catalyst may have a surface area of at least 100: g. The pore volume of the first catalyst may be at least 0 "cm3 / g. · The first catalyst may have a gamma oxide content of at least 0.5 grams of gamma oxide per gram of the first catalyst, and typically a maximum of 0.999 grams of alumina. The first catalyst has a total sixth metal content in the range of OOOW to • 1 gram per gram of catalyst in several specific examples. The first catalyst can remove a part of Ni / V / Fe in the crude oil feed, remove a part of the TAN that caused the crude oil feed, and remove at least a part of the c5 asphaltene in the crude oil feed. At least a part of the metal in the form of a metal salt of an organic acid, or a combination thereof. When the crude feed is in contact with the first catalyst, other properties (such as sulphur content, VG0 content, API specific gravity, residue content, or a combination thereof) may show only relatively small changes. The ability to selectively change the raw scallops of the crude oil feed, while changing other properties only in relatively small amounts, allows the crude oil feed to be processed more efficiently. In several specific examples, one or more of the first catalysts can be used in any order. In a specific specific example, the second type of catalyst ("the second type of catalyst,") includes metal in columns 5 to 10 of the carrier combination, and has a median pore diameter of 90 to 1807. The pore size distribution within the range. The number: 60% of the total pore number of the catalyst has a target range of 45 Å at the TI range. When the crude oil is fed under contact conditions, the first ^ is at the inverse t The contact with a catalyst can compare the same properties of raw feed, and there are significant changes in selected properties of crude oil / crude oil η H (such as TAN), while other properties of the same day have changed only slightly. Product. In several examples, there may be a hydrogen source during the contact. /,, The second catalyst can reduce at least eight components of the TAN that causes crude oil feed, resulting in at least one knife of relatively high viscosity. Into a knife, and reduce the Nl / V / Fe content of the crude product to the V-part. In addition, the contact of the second catalyst of the crude feed fish can produce a sulfur content compared to the crude feed, :::: Crude oil products with varying amounts. For example, crude oil products; with: to 13G% of crude oil feed Compared with the crude oil product, the crude oil product may also show only a small amount of changes in the content of the content, VG0 content, and residue content. In some specific examples, the crude oil feed may have Relatively low job: li (for example, up to 50wtppm), but relatively high TAN, asphaltenes: metal content in the form of metal salts of organic acids. Relatively high UN, (such as 0.3 TAN) may make Crude oil feed is unacceptable for transportation and / or refining. Inferior crude oils with relatively high to high blue content may show lower stability when compared to other crude oils with relatively low Cs asphaltene content Sex. The contact of the crude feed with the second catalyst can remove the acidic components of the TAN and / or c5 asphaltenes from the crude feed. In the case of "-", the reduction of cs asphaltenes and / or the constituents that cause TAN may reduce the viscosity of the crude feed / total product mixture by 78 200533737 compared to the viscosity of the crude feed. In certain specific examples, the Two kinds of catalysts—or a combination of them: When: Coming from the crude oil feed described in this article, it can improve the stability of the total product / crude oil mixture, increase the life of the catalyst, and provide the recovery of crude oil feed. In some specific examples, the third type of catalyst ("the third type of catalyst,") can be obtained by combining the carrier with the sixth metal to generate a catalyst precursor. The catalyst river flooding substance can be heated in the presence of-or multiple sulfur compounds at a low me (e.g., less than 482 ° C ί 西 降 πτ 丄 & L) for a relatively short period of time to generate uncalcined t Passed the second catalyst. Typically, the catalyst precursors increase to 埶 100. ° for 2 hours. In a specific embodiment, the third catalyst may have 0.001 to 0.03 grams, 0.05 to 0.02 grams, or 0.008 to CMH grams in the mother gram catalyst. The crude oil described in this article can exhibit significant growth and stability. In several specific examples, the 'catalyst precursor is based on-or multiple sulfur compounds, and is heated at a temperature below _t in the presence of a sulphur compound. The third catalyst can reduce at least a portion of the constituents of the TAN of the crude oil feed ′, reduce at least a portion of the metal in the form of a metal salt of an organic acid, reduce the Ni / V / Fe content of the crude oil product, and reduce the viscosity of the crude oil product. In addition, the contact of the crude oil feed with the second catalyst can produce a sulfur content of the crude oil feed, which is a relatively small amount of sulfur content and a crude oil product that has a relatively small amount of hydrogen absorbed by the crude oil feed. For example, a crude oil product may have a sulfur content of a crude oil feed having a sulfur content of 70% to 130%. Using a third catalyst: Compared with crude oil feed, the crude oil product produced, the specific gravity of ιΑρι, the fraction containing VGO, and the residue content may also show only small changes in 79 200533737. The ability to reduce crude oil feed & TAN, metals of organic acid metal salt form, Nl / V / Fe content, and viscosity while only slightly changing Αρι ratio =, fraction content, VGO content 'and residue content allows crude oil The product is used by various processing equipment. The third catalyst can reduce the MCR content of at least-part of the crude oil feed in several specific examples, while maintaining the stability of the crude oil feed / total product. In certain specific examples, the third catalyst has a sixth metal content in the range of 0.0001 to 0.1 g, 0.005 to 0.05 g, or 0.0001 to " i gram per gram of catalyst. And the metal column in the tenth column within the range of 0. to 5 grams, 005 to 0.03 grams, or 001 to 001 Jiyidan. The 6th and 10th metal catalysts can contribute to a reduction of at least one to _. Temperatures in the range of 0 or ⑽ 450 t and pressures in the range of 10: m8 MPa, or 2 to 5 MPa cause the components of the original / derived MCR in the feed. In a specific specific example, the fourth type of catalyst ("the fourth type of catalyst,") contains 乳化 emulsions, which are combined with a metal carrier. The fourth type of catalyst has a median: pore size distribution of at least A180A. In some specific examples, the fourth = a certain median pore can be at least 220A, at least 230 people, at least 0A, or at least 300 A. The Christine carrier can contain at least aluminum in the mother gram carrier ~ Up to 0.5 grams' at least 0.8 grams, or at least 0.9 grams of Θ oxidized to. Fine catalysts in several specific examples may include the 5th metal block with the most flute gram per gram, and per gram of contact The metal in the medium is at least grams of metal. In certain specific examples, the fifth metal is hungry. In several specific examples, after contact with the fourth catalyst, crude oil 80 200533737 is brought into additional catalyst contact. The additional The catalyst can be the following: the first catalyst, the second catalyst, the third catalyst, the fifth catalyst, the sixth catalyst, the seventh catalyst Medium, or a combination of them. In the specific example described in the right hand example, hydrogen can .C, 32u through .c, or coffee to ^. The crude oil products produced by this type of contact can have a maximum of 90%, a maximum of 80%, a maximum of 50%, or a maximum of TAN for crude oil feed. Hydrogen generation can range from U50Nm3 / m3,

NmVm3’或15至25 NmVm3的範圍内。原油產物可具有 總Ni/V/Fe含量最多為9〇%，最多為8〇%，最多為_， 最多為5〇%，最多為10%，或至少為1%之原油進料㈣ Ni/V/Fe 含量。 於特定具體實例中，第五類觸媒（“第五種觸媒，，）包含 與Θ氧化鋁載體結合的第6欄金屬。第五種觸媒具有中2 孔徑至少為180 A，至少為220 Λ，至少為23〇 A，至少為 250 A，至少為300 A，或最多為500 A的孔徑分佈。該載 體在母克載體中可包含至少0.1克，至少〇·5克，或至少 0.999克的θ氧化鋁。於若干具體實例中，載體具有α氧化 銘含量為每克觸媒中有低於0· 1克的α氧化鋁。該觸媒於若 干具體實例中係包含每克觸媒中最多為〇 · 1克的第6搁金 屬，且每克觸媒中至少為0.0001克的第6欄金屬。於若干 具體實例中，第6攔金屬為鉬及/或鎢。 於特定具體實例中，當原油進料與第五種觸媒在3 ! 〇 81 200533737 至 400 °c，320 至 37〇 ^ 芏370 C，或330至360 t的溫 觸時，原油進料之氕从w η 之氧的甲吸取可能相當地低（例如〇 〇1至 100 Nm3/m3，1 j sn Μ 3, ^ 80 Nm /m，5 至 50 Nm3/m3，或 1()至 3〇NmVm3 'or 15 to 25 NmVm3. Crude products can have a total Ni / V / Fe content of up to 90%, up to 80%, up to _, up to 50%, up to 10%, or at least 1% of crude oil feed ㈣ Ni / V / Fe content. In a specific embodiment, the fifth type of catalyst ("the fifth catalyst,") includes the sixth column of metal combined with a Θ alumina support. The fifth catalyst has a meso2 pore size of at least 180 A, at least Pore size distribution of 220 Λ, at least 23 OA, at least 250 A, at least 300 A, or at most 500 A. The carrier may contain at least 0.1 g, at least 0.5 g, or at least 0.999 in the mother gram carrier Grams of θ alumina. In some specific examples, the carrier has an alpha oxide content of less than 0.1 grams of α alumina per gram of catalyst. The catalyst contains per gram of catalyst in several specific examples. The maximum amount is 0.1 g of the 6th metal, and each gram of the catalyst is at least 0.0001 g of the 6th metal. In some specific examples, the 6th metal is molybdenum and / or tungsten. In specific examples In the middle, when the crude oil feed and the fifth catalyst are at a temperature of 3 〇81 200533737 to 400 ° C, 320 to 37〇 芏 370 C, or 330 to 360 t, the crude oil feed 氕 from w η The oxygen uptake of oxygen may be quite low (for example, 0.001 to 100 Nm3 / m3, 1 j sn Μ 3, ^ 80 Nm / m, 5 to 50 Nm3 / m3 , Or 1 () to 3〇

Nm3/m3)。原油進料夕气 一， 琨抖之虱的净吸取於若干具體實例中可在丄 至2〇馳3/11；3,2至15_、3，或3至10他3/1113的範圍 内由原油進料與第五種觸媒接觸所生產的原油產物可具 有則最多為9〇%，最多為80%，最多為5〇%，或最多為 10%之原油進料㈤TAN。原油產物的TAN可在至〇」，Nm3 / m3). For crude oil feed, the net intake of trembling lice can be in the range of 丄 to 202 3/11; 3, 2 to 15_, 3, or 3 to 10 他 3/1113 in some specific examples. The crude oil product produced by contacting the crude oil feed with the fifth catalyst may have a maximum of 90%, a maximum of 80%, a maximum of 50%, or a maximum of 10% crude oil feed ㈤TAN. The TAN of crude oil products can be as low as 0 ",

〇·〇3至〇.〇5，或〇 〇2至〇 〇3的範圍内。 广於特疋具體實例中，第六類觸媒（“第六種觸媒”）包含 ’、Θ氧化鋁載體結合的帛5欄金屬和第6欄金屬。第六種 :媒具有中位孔徑至少& 180 A的孔徑分佈。於若干具體 2例中，孔徑分佈的中位孔徑可至少為22〇 A，至少為 、為5〇 A ’至少為3〇〇 a ’或最多為5〇〇 a。該 =在母克載體中可包含至少〇1克，至少〇·5克，至少。·8In the range of 0.03 to 0.05, or 0.002 to 0.003. In the specific examples that are broader than the special ones, the sixth type of catalyst ("the sixth type of catalyst") includes 包含, Column 5 metal and Column 6 metal combined with Θ alumina support. Sixth: The medium has a pore size distribution with a median pore size of at least & 180 A. In some specific 2 cases, the median pore size of the pore size distribution can be at least 22 A, at least 50 A ', at least 300 a', or at most 500 a. The = may contain at least 0.01 g, at least 0.5 g, at least in a mother gram carrier. ·8

^ 夕〇·9克’或最多為〇·99克的Θ氧化鋁。該載體於 右干具體實例中可包含每克觸媒中最多為0·1 1之第5攔 ^ 欄金屬的總量，且每克觸媒中至少為0.0001克 ^ 襴金屬和第6攔金屬的總量。於若干具體實例中， ]金屬總量與第5攔金屬總量的莫耳比可在〇· 1至20， 1至1 〇，十 金、或2至5的範圍内。於特定具體實例中，第5欄 王屬為釩而第6攔金屬為鉬及/或鎢。 〇c 田眾〉'由進料與第六種觸媒在310至400 °c，320至370 〆 〇至360 C的溫度下接觸時，原油進料之氫的淨 82 200533737 吸取可在」0 Nm3/m3 至 20 Nm3/m3，-7 Nm3/m3 至 1〇 ΝΐΏ /1Ώ ’或-5 Nm3/m3至5 Nm3/m3的範圍内。氫的負值淨 吸取為虱在現場產生的跡象。由原油進料與第六種觸媒接 觸:生產的原油產物可具有TAN最多為90%，最多為8〇%， 最夕為50/。’最多為1〇%，或至少為1%之原油進料的tan。 原油產物的TAN可在〇·〇1至0.1，0·02至0.05，或〇 〇3 至〇.〇4的範圍内。 〆· 产在原油進料與第四種、第五種，或第六種觸媒接觸期 的夕、里/爭吸取會減少在生產輸送及/或處理可接受之原 油f :的加工期間氫的總需求。由於生產及/或輸送氫的成 本叩貴，因此使製程中氫的使用減至最小量會降低加工總 成本。 於特定具體實例中，第七類觸媒（“第七種 第㈣金屬總含量在每克觸媒中有。.嶋至。：2第有6 攔金屬的範圍内。帛6欄金屬為翻及/或鶴。第七種觸媒係 有利於生產具有TAN最多為9〇%之原油進料的Tan之原 油產物。 —第一種、第二種、第三種、第四種、第五種、第六種 和第七種觸媒的其他具體實例也可像本文中另外敘述一樣 地製造及/或使用。 選擇本申請案之觸媒及控制操作條件可容許生產具有 與原油進料相比改變的TAN及/或選定性質而同時原油進 料的其他性質沒有顯著改變的原油產物。所得原油產物與 原油進料相比可能會具有強化性質，因此更為輸送及/或精 83 200533737 煉所能接受。 按選擇順序配置兩種或更多種觸媒可控制原油進料的 性質改善順序。舉例而言，原油進料中的丁AN、API比重、 至少一部分的Cs瀝青質、至少一部分的鐵、至少一部分的 鎳，及/或至少一部分的釩能在減少原油進料中至少一部分 的雜原子之前減少。 配置及/或選擇觸媒於若干具體實例中可提高觸媒壽命 及/或原油進料/總產物混合物的穩定性。在加工期間提高 觸媒壽命及/或原油進料/總產物混合物的穩定性可容許接 觸系統在不更換接觸區中觸媒的情況下，運轉至少3個月， 至少6個月，或至少丨年。 結合選定觸媒可在原油進料的其他性質改變之前，使 j油進料中至少—部分的Ni/V/Fe，至少-部分的C5瀝青 =，至少一部分的有機酸金屬鹽形態之金屬，至少一部分 :成TAN的成分，至少一部分的殘留物，或其組合減少， ^且同時在加工期間保持原油進料/總產物混合物的穩定性 (列如保持高於1 · 5的原油逸料^ 0.9 g 'or Θ alumina up to 0.99 g. In the specific example of the right carrier, the carrier may include the total amount of the fifth bar ^ metal of up to 0.11 per gram of the catalyst, and at least 0.0001 g ^ metal and the sixth bar of metal per gram of the catalyst. Of the total. In several specific examples, the molar ratio of the total amount of metal to the total amount of the fifth metal may be in the range of 0.1 to 20, 1 to 10, ten gold, or 2 to 5. In a specific embodiment, the queen of the fifth column is vanadium and the sixth metal is molybdenum and / or tungsten. 〇c Tianzhong> 'When the feed is in contact with the sixth catalyst at a temperature of 310 to 400 ° C, 320 to 370 ° C to 360 C, the net hydrogen absorption of the crude oil feed can be as low as 0,200,533,737. Nm3 / m3 to 20 Nm3 / m3, -7 Nm3 / m3 to 10NΐΏ / 1/1 'or -5 Nm3 / m3 to 5 Nm3 / m3. Negative net uptake of hydrogen is a sign of lice in the field. The crude oil feed is in contact with the sixth catalyst: the crude oil product produced can have a TAN of up to 90%, up to 80%, and up to 50 /. 'Is at most 10%, or at least 1% of the tan of the crude feed. The TAN of the crude product may be in the range of 0.001 to 0.1, 0.02 to 0.05, or 0.003 to 0.04. 〆 · Produced during the contact period between the crude oil feed and the fourth, fifth, or sixth catalyst will reduce the hydrogen during processing and / or processing of acceptable crude oil f: Total demand. Because the cost of producing and / or transporting hydrogen is expensive, minimizing the amount of hydrogen used in the process will reduce the overall processing cost. In a specific specific example, the seventh type of catalyst ("the total content of the seventh type VII metal is in each gram of the catalyst .. 嶋 to.: 2 to the 6th metal range. 帛 6 column metal is a turn And / or cranes. The seventh catalyst is a crude oil product that is favorable for the production of Tan with a TAN crude oil feed of up to 90%.-The first, second, third, fourth, fifth Other specific examples of the first, sixth, and seventh catalysts can also be manufactured and / or used as described elsewhere herein. Selecting the catalyst and controlling the operating conditions of this application may allow production to have a phase similar to crude oil feeds. Crude products that have a significantly lower than the changed TAN and / or selected properties while other properties of the crude feed are not significantly changed. The resulting crude oil products may have enhanced properties compared to the crude feed and are therefore more transported and / or refined. Acceptable. Configuring two or more catalysts in a selected order can control the order of improving the properties of the crude oil feed. For example, Ding AN in the crude oil feed, API specific gravity, at least a portion of Cs asphaltenes, at least a portion Iron, at least part of Nickel, and / or at least a portion of vanadium can be reduced before reducing at least a portion of the heteroatoms in the crude oil feed. Configuring and / or selecting the catalyst in several specific examples can increase the catalyst life and / or crude oil feed / total product Stability of the mixture. Increasing the catalyst life and / or the stability of the crude feed / total product mixture during processing allows the contact system to operate for at least 3 months without changing the catalyst in the contact zone, at least 6 Month, or at least 丨 years. Combined with the selected catalyst, at least-part of Ni / V / Fe, at least-part of C5 asphalt =, at least part of organic Metals in the form of acid metal salts, at least a part: TAN-forming ingredients, at least a part of the residues, or a combination thereof are reduced, while maintaining the stability of the crude oil feed / total product mixture during processing (listed to remain above 1 5 crude oil escapes

π原油進科P值）。或者，c5瀝青質、丁AN / API比重可藉由原油進料與選定觸媒的接觸而逐漸減 夕。漸進式及/或選擇性改變原油進料性質的能力可容許在 工期間保持原油進料/總產物混合物的穩定性。 連串總干八體實例中，第一種觸媒（上述者）可配置在一 旦一 裡觸媒的此種配置可容許移除高分 里’亏染物、金屬污毕物，芬/ 甘B门 木物及/或有機酸金屬鹽形態之金屬， 亚且同時保持原油進 丁十~屋物混合物的穩定性。 84 200533737 -種觸媒於若干具时財係料移W油進料中 广部分的Nl/V/Fe’移除酸性成分，移除造成系統中 :、他觸媒壽命減短的成分，或其組合。舉例而t，與原油π crude oil into the P value). Alternatively, the specific gravity of c5 asphaltenes and D / AN can be gradually reduced by the contact of crude oil feed with selected catalysts. The ability to incrementally and / or selectively change the properties of the crude feed can allow the stability of the crude feed / total product mixture to be maintained during the process. In a series of examples of total stem octapods, the first catalyst (the above) can be arranged once. This configuration of the catalyst can allow the removal of 'defectives, metallic contaminated materials, and fen / gan B in high scores. Metals in the form of wood and / or organic acid metal salts, while maintaining the stability of the crude oil into the house mixture. 84 200533737-A type of catalyst removes acidic components from a large portion of Nl / V / Fe 'in the oil feed of certain time-based materials, removing components that cause the system to shorten its catalyst life, or Its combination. For example, t, with crude oil

進料相比，減少原油進料/總產物混合物中至少一部分的、C 瀝青質會抑制配置於下游之其他觸媒的堵塞，因此;增力C口5 接觸系統在沒有補充觸媒的情況下仍可運轉的持續σ 移除原油進料中至少一部分# N1/V/Fe於若干具體實^ 可9加配置在第一種觸媒後面之一或多種觸媒的壽命。 卜第一種觸媒及/或第三種觸媒可配置在第一種觸媒的下 、原油進料/總產物混合物與第二種觸媒及/或第三種觸 媒的進一步接觸可進一步降低TAN，降低Ni/V/Fe含量， 降低& &里，降低含氧量，及/或降低有機酸金屬鹽形態的 金屬含量。 於若干具體實例中，原油進料與第二種觸媒及/或第三 種觸媒的接觸可生產原油進料/總產物混合物，與原油進= 的個別性質相tb，其具有降低# tan，降低的含硫量，降 低的含氧量，降低的有機酸金屬鹽形態之金屬含量，降低 的瀝青質含量，降低的黏度，或其組合，1同時在加工期 =保持原油進料/總產物混合物的穩定性。第二種觸媒可並 耳外配置，第二種觸媒係位於第三種觸媒上游，或者反過來 也可以。 使氣輪送至特定接觸區的能力會傾向於使接觸期間氫 、用減至最小畺。結合在接觸期間促使氫氣發生的觸媒 〃在接觸期間吸取相當少量氫氣的觸媒可用來改變與原油 85 200533737 進料的同樣性質相比之下原油產物的選定性質。舉例而 〉 言，第四種觸媒可與第一種觸媒、第二種觸媒、第三種觸 媒、第五種觸媒、第六種觸媒，及/或第七種觸媒合併使用 以改變原油進料的選定性質，而同時只有選擇量地改變原 2進料的其他性質，及/或同時保持原油進料/總產物的穩 定性。可選擇觸媒的順序及/或數目使氫的淨吸取減至最小 量，同時保持原油進料/總產物的穩定性。氫的最小淨吸取 係使原油進料的殘留物含量、VG〇含量、餾分含量、A?工 比重，或其組合保持在20%的原油進料之個別性質的範圍修 内’而原油產物的TAN及/或黏度最多為9〇%之原油進料 的TAN及/或黏度。 由進料之氫的淨吸取可生產具有與原油進申 彿點分佈類似料程分佈，與原油進料之TAN相比释 TAN的原油產物。々、、由甚 ^由產物的原子Η/C也可只比原油遠 的原子H/C有相當少量的改變。Compared with the feed, reducing at least a part of the crude oil feed / total product mixture, C asphaltenes will inhibit the clogging of other catalysts arranged downstream, therefore; the booster C port 5 contact system without supplementary catalyst Continued operation to remove at least a part of the crude oil feed # N1 / V / Fe for a number of specific applications ^ can be configured behind the life of one or more catalysts behind the first catalyst. The first catalyst and / or the third catalyst may be arranged under the first catalyst, and further contact between the crude oil feed / total product mixture and the second catalyst and / or the third catalyst may be Further reducing TAN, reducing Ni / V / Fe content, reducing & & reducing oxygen content, and / or reducing metal content in the form of metal salt of organic acid. In several specific examples, the contact of the crude oil feed with the second catalyst and / or the third catalyst can produce a crude oil feed / total product mixture, with the individual properties of crude oil feed = tb, which has a reduced # tan , Reduced sulfur content, reduced oxygen content, reduced metal content in the form of metal salts of organic acids, reduced asphaltene content, reduced viscosity, or a combination thereof, 1 at the same time during processing = maintaining crude oil feed / total Product mixture stability. The second catalyst can be configured outside the ear, the second catalyst is located upstream of the third catalyst, or vice versa. The ability to get the gas wheel to a specific contact zone tends to minimize hydrogen use during contact. In combination with a catalyst that promotes the occurrence of hydrogen during the contact, a catalyst that absorbs a relatively small amount of hydrogen during the contact can be used to change the selected properties of the crude oil product compared to the same properties of the crude oil 85 200533737 feed. For example, the fourth catalyst can be combined with the first catalyst, the second catalyst, the third catalyst, the fifth catalyst, the sixth catalyst, and / or the seventh catalyst. Used in combination to change selected properties of the crude feed, while only changing the other properties of the original 2 feed in a selected amount, and / or while maintaining the stability of the crude feed / total product. The sequence and / or number of catalysts can be selected to minimize the net uptake of hydrogen while maintaining the stability of the crude feed / total product. The minimum net hydrogen uptake is to keep the residual content, VG0 content, distillate content, A? Work gravity, or a combination thereof of the crude oil feed within the range of the individual properties of the crude oil feed of 20%. TAN and / or viscosity TAN and / or viscosity of crude oil feeds up to 90%. The net uptake of hydrogen from the feed can produce a crude product with a similar distribution to the feed point distribution of crude oil and a TAN release compared to the TAN of the crude feed. The atomic Η / C of the product can be changed only slightly compared to the atomic H / C of the crude oil.

二定接觸區"氯氣發生可容許氨選擇性添加至其 實例中，第四種觸媒： f。於若干具 游、 '、°配置在本文中所述的附加觸媒 子、下办或介於其間。鈐 ^ ^ Π ^ ^ β在原油進料與第四種觸媒接 ^間發生，可將氫輪 〃卞设; ,, 、匕3附加觸媒的接觸區。氫的4 < j興原油進料的流動 送可盥原、、由進# Μ ώ ;右干具體實例中，氫的4 /、原油進枓的流動同向。 舉例而言，在堆最 %π^ ^ 隹隹且結構中（參見如圖2Β)，氳可在接 4間於-接觸區中(例如 "τ在㈣ 口 2Β中的接觸區102)生成，氫月 86 200533737 以原油進料流動相反的方向輸送至附加接觸區（例如圖2B 中的接觸【114)。於若干具體實例中，氫流動可與原油進 料的流動同向。或者，在堆疊結構中(參見如圖3B)，氫可 在接觸期間於-接觸區中(例如圖3B中的接觸區1〇2)生 成。氨源可以原油進料流動相反的方向輸送至第-附加接 觸區（例如在β 3B中，使氫經由導管1〇6，添加至接觸區 Η4)，以原油進料流動相同的方向輸送至第二附加接觸區 (例如在Η 3Β中’使氫經由導# 1〇6，添加至接觸區116)。 ;右干具體實例中，第四種觸媒與第六種觸媒係並聯 φ 制，第四種觸媒係位於第六種觸媒上游，或者反過來也 :以。結合第四種觸媒與附加觸媒可在原油進料之氯的少 量淨吸取的情況下’降低TAN，降低Ni/V/Fe含量，及/或 降低有機酸金屬鹽形態的金屬含量。氫的少量淨吸取可容 〇午原油產物的其他性質與原油進料的同樣性質相比之下只 有少量改變。 ;右干具體實例中，兩種不同❸第七種觸媒可合併使 用。在上游所用的第七種觸媒而非下游的第七種觸媒在每 克觸媒中可具有0.0001至〇·〇6克之範圍内的第6攔金屬 總含量。下游的第七種觸媒在每克下游的第七種觸媒中可 八有等於或大於上游的第七種觸媒中第6攔金屬總含量， :每克觸媒中至少0.02克之第6攔金屬的第六欄金屬總含 置。於若干具體實例中’上游的第七種觸媒和下游的第七 種觸媒可顛倒過來。於下游的第七種觸媒中使用相當少量 之催化活性金屬的能力可容許原油產物的其他性質與原油 87 200533737 進料的同樣性質相比之下只 -比重、殘留物含量、VG0含量二，含量、 改變）。 里^組合的相當少量 原t進料與上游和下游的第七種觸媒之接觸可 、TAN最多為9〇%，最多為8〇%，最多為50%，最多；、 或至少為1 〇/ 4広》 夕為10 % ’ :至：為“之原油進料的TAN之原油產物。 貫例中，原油進料的TAN藉 接觸而逐漸降低(例如，原油進料與觸媒的接觸以生成 ”原油進料相比具有改變性質的初原油產#，接著初原油 產物與附加觸媒的接觸係 ， W·併Μ = 度王/、初原油產物相比具有改變 :貝的原油產物)。漸進式降低ΤΑΝ的能力可在加工期間 襄助保持原油進料/總產物混合物的穩定性。 於若干具體實例中，觸媒選擇及/或觸 ⑽原油進料流率)的結合可幫助= ''之氫的吸取’在加工期間幫助保持原油進料人總產物 混合物的穩定性，並且與原油進料的個別性質相比，改變 原產物的或夕種性質。原油進料/總產物混合物的穩定 ί·生可月《3會受到來自原油進料/總產物混合物之各種相分離的 影響。相分離可能由例如原油進料/總產物混合物中原油進 料及/或原油產物的不溶性，原油進料/總產物混合物之遞 青質的絮凝’原油進料/總產物混合物之成分的沈澱，或其 組合所導致。 在接觸期間的一定次數下，原油進料/總產物混合物中 原油進料及/或總產物的濃度可能會改變。當原油進料/總 88 200533737 產物此合物中的總產物濃度因為生成原油產物而改變時， 原油進料/總產物混合物中原油進料成分及/或總產物成分 的溶解度會有改變的傾向。舉例而言，原油進料可能含= 於加工-開始可溶於原油進料的成分。當原油進料的性質 _口、TAN、MCR、C5〉歷青質、p值，或其組合）改變時，、 k 一成刀可月b會有變得較不易溶於原油進料/總產物混合物 W貝向&右干實例中’原油進料和總產物可能會形成兩 相及/或變成彼此不溶。溶解度改變也可能導致原油進料/ 總產物混合物形成兩個或更多個相。由於瀝青質的絮凝， 原油進料和總產物濃度的改變，及/或成分的沈殿而形成兩 4 :傾向於減紐一或多種觸媒的壽命。此外，製程效率也 可能會降低。舉例而言，可能需要重複處 物混合物以生產具有期望性質的原油產物。 4、·心產 、在加工#月間，彳監測原油進料/總產物混合物的P值， I二估^、原油進料，及/或原油進料/總產物混合物的 =!·生。典型而言，最多為i5 & p值係表示原油進料之 遞月質的絮凝通常會發生。如果p值一開始至少為Μ， 而此等P值在接觸期間會增加或相當穩定 =料在接觸期間相當穩定。原油進料/總產物混合二： 二$遅如J值所評估者，可藉由控制接觸條件，藉由觸媒 此由觸媒的選擇性排序，或其組合而加以控制。 =控：接觸條件可包括…請、溫度、麼力、氯的 及取、原油進料流率，或其組合。 ' 、體實例中，@制接觸溫度以便移㉟q瀝青質 89 200533737 及/或其他遞青質，计 山尸 、W冋守保持原油進料的MCR含量。葬 由虱的吸取及/或軔古从 里 耩 回的接觸溫度降低MCR含量可能合導 致形成兩相，其可能合隊“ 各里“匕會導 性及/或—ρ括θ ♦低原〉由進料/總產物、混合物的穩定 社人J 5夕觸媒的壽命。控制接觸溫度和氫的吸取並 結r文中所述的觸媒可容許降低。5瀝青質而同時= 少量地改變原油進料的MCR含量。 于、相田 於若干具體實例中，批 控制接觸條件以便使一或多個接 觸區中的溫度可為相里者 ，、者不同溫度下的操作可容許選擇 性改變原油進料性暂而π主 、 貝而同時保持原油進料/總產物混合物的 穩定性。原油進料在製程開始時進入第一接觸區。第 觸溫度為第一接觸區中的溫度。其他接觸溫度(例如第二溫 度、第三溫度、第四溫度等)為配置在第一接觸區後面之： 觸區中的溫度。第一垃鎚、、西Γ ^ 罘接觸/皿度可在1 00至420。(：的範圍内， 第二接觸溫度可在與第一接觸溫度相差20至1〇〇 t，3〇 至90。(：，或40至60 t的範圍内。於若干具體實例中， 第二接觸溫度大於第一接觸溫度。具有不同的接觸溫度可 使原油產物中的TAN及/或q瀝青質含量與原油進料的 TAN及/或（：5瀝青質含量相比之下降低至比，如果有的話， 在第一和第二接觸溫度彼此相同或相差為1〇它以内時的 TAN及/或C5瀝青質減少量更大的程度。 舉例而言，第一接觸區可包含第一種觸媒及/或第四種 觸媒，而第二接觸區可包含本文中所述的其他觸媒。第一 接觸溫度可為350。(：，第二接觸溫度可為3〇〇它。原油 進料在第一接觸區中與第一種觸媒的接觸及/或在與第二接 200533737 觸區中與其他觸媒接觸之前於較高溫度下與第四種觸媒的 ， 接觸可導致在原油進料中，與在第一和第二接觸溫度相差 為10 °C以内時相同原油進料中TAN及/或c5瀝青質的減 少相比，有更多TAN及/或C5瀝青質的減少。 實施例 以下提出載體製備、觸媒製備，及具有選定觸媒配置 與控制接觸條件之系統的非限定實施例。 例1.___U希觸嫫載艚二 載體係利用585克的水和8克的冰硝酸將576克的氧籲 化鋁（Criterion Catalysts and Techn〇1〇gies LP，MichigailThe second contact zone " chlorine generation allows selective addition of ammonia to its example, the fourth catalyst: f. The additional catalysts described in this article are deployed in several games, ', °, or in between.钤 ^ ^ Π ^ ^ β occurs between the crude oil feed and the fourth catalyst, and a hydrogen wheel can be set up; In the specific example of hydrogen, the flow of hydrogen and crude oil feed in the same direction. For example, in the structure with the highest% π ^ ^ 隹 隹 and the structure (see Figure 2B), 氲 can be generated in the 4 contact-contact areas (for example, " τ in the contact area 102 in port 2B). , Hydrogen month 86 200533737 was transported to the additional contact zone in the opposite direction of the crude oil feed flow (eg contact [114] in Figure 2B). In several specific examples, the hydrogen flow may be in the same direction as the flow of the crude oil feed. Alternatively, in a stacked structure (see Fig. 3B), hydrogen may be generated in the -contact region (e.g., contact region 102 in Fig. 3B) during the contact. The ammonia source can be transported to the first additional contact zone in the opposite direction of the crude oil feed flow (for example, in β 3B, hydrogen is added to the contact zone Η4 through the conduit 106), and the crude feed stream is transferred to the first Two additional contact regions (for example, in '3B' to allow hydrogen to be added to the contact region 116 via conduction # 106). ; In the specific example of the right stem, the fourth catalyst is connected in parallel with the sixth catalyst system, and the fourth catalyst system is located upstream of the sixth catalyst, or vice versa:. Combining the fourth catalyst with the additional catalyst can reduce the TAN, reduce the Ni / V / Fe content, and / or reduce the metal content of the organic acid metal salt in the case of a small net uptake of chlorine in the crude oil feed. The small net uptake of hydrogen can tolerate other properties of the crude oil product with only minor changes compared to the same properties of the crude feed. ; In the specific example of the right stem, two different ❸ seventh catalysts can be used in combination. The seventh catalyst used upstream, rather than the seventh catalyst downstream, may have a total sixth metal content in the range of 0.0001 to 0.06 grams per gram of catalyst. The seventh catalyst in the downstream may have eight or more of the total metal content in the seventh catalyst in the downstream of the seventh catalyst in the downstream, at least 0.02 g of the sixth in each gram of the catalyst. The sixth column of metal is always contained. In several specific examples, the seventh catalyst upstream and the seventh catalyst downstream can be reversed. The ability to use a relatively small amount of catalytically active metal in the seventh catalyst downstream can allow other properties of the crude oil product to be comparable to the same properties of the crude oil 87 200533737 feed only-specific gravity, residue content, VG0 content, Content, change). The contact of a relatively small amount of the raw t feed with the seventh and upstream catalysts can be up to 90%, up to 80%, up to 50%, and up to 10%. / 4 広 ”Evening is 10% ': to: is the crude product of TAN of the crude oil feed. In the conventional example, the TAN of the crude oil feed is gradually reduced by contact (for example, the contact between the crude oil feed and the catalyst is "Crude crude oil production # with altered properties compared to the crude oil feed, followed by the contact system between the crude oil product and the additional catalyst, W · M = degree king /, compared with the crude oil product: the crude oil product) . The ability to progressively reduce TAN can help maintain the stability of the crude feed / total product mixture during processing. In a few specific examples, the combination of catalyst selection and / or contact with the crude oil feed flow rate) can help = `` hydrogen uptake '' to help maintain the stability of the total product mixture of the crude oil feed during processing, and Compared to the individual properties of the crude oil feed, the properties of the original product are changed. Stability of crude oil feed / total product mixtures. 生 可 受到 3 is affected by various phase separations from the crude oil feed / total product mixtures. Phase separation may be caused by, for example, the insolubility of the crude oil feed and / or crude oil product in the crude oil feed / total product mixture, precipitation of components of the crude oil feed / total product mixture, cyanogenic flocculation, crude oil feed / total product mixture, Or a combination thereof. At certain times during the contact, the concentration of the crude feed and / or total product in the crude feed / total product mixture may change. When the crude product feed / total 88 200533737 product total product concentration changes due to the formation of crude oil products, the solubility of the crude feed component and / or the total product component in the crude feed / total product mixture will tend to change . For example, a crude oil feed may contain ingredients that are soluble in the crude feed at the beginning of processing. When the nature of the crude oil feed_mouth, TAN, MCR, C5> calendar quality, p-value, or a combination thereof) is changed, k is equal to $ 10, and b will become less soluble in the crude oil feed / total In the product mixture & right dry example, the crude oil feed and the total product may form two phases and / or become insoluble with each other. Changes in solubility may also cause the crude feed / total product mixture to form two or more phases. Due to the flocculation of asphaltenes, changes in the crude oil feed and total product concentration, and / or the composition of the Shen Dian 4: tend to reduce the life of one or more catalysts. In addition, process efficiency may be reduced. For example, it may be necessary to repeat the process mixture to produce a crude product with desired properties. 4. Heart production During the month of processing, 值 monitor the P value of the crude oil feed / total product mixture, I estimate, crude oil feed, and / or crude oil feed / total product mixture =! Typically, up to i5 & p values indicate that the flocculation of crude oil feeds usually occurs. If the p-value is at least M initially, these P-values will increase or be fairly stable during the contact = the material is quite stable during the contact. Crude oil feed / total product mix 2: As estimated by the J value, it can be controlled by controlling the contact conditions, by the catalyst, by the selective ordering of the catalyst, or by a combination thereof. Control: The contact conditions may include: please, temperature, melamine, chlorine and extraction, crude oil feed flow rate, or a combination thereof. In the example, the @ contact temperature is used to transfer the q asphaltenes 89 200533737 and / or other green substances, and it is assumed that the MCR content of the crude oil feed is maintained by the corpse and W. The reduction in MCR content caused by the absorption of lice and / or the reduction in contact temperature from ancient times may lead to the formation of two phases, which may form a "group" that is conductive and / or-ρ encompassing θ ♦ Low origin> The life of the catalyst is based on the stability of the feedstock / total product and the mixture of J5. Control of contact temperature and hydrogen uptake and the catalyst described in the text may allow reduction. 5 asphaltenes at the same time = slightly change the MCR content of the crude feed. In some specific examples, Yu Xiangtian, batch control the contact conditions so that the temperature in one or more contact zones can be in the phase, or the operation at different temperatures can allow selective changes in crude oil feedability temporarily π main , While maintaining the stability of the crude feed / total product mixture. The crude feed enters the first contact zone at the beginning of the process. The contact temperature is the temperature in the first contact zone. Other contact temperatures (e.g., second temperature, third temperature, fourth temperature, etc.) are the temperatures in the contact area disposed behind the first contact area. The first contact of the hammer and the bridge can be between 100 and 420. In the range of :, the second contact temperature may be 20 to 100 t, 30 to 90 different from the first contact temperature. (:, Or 40 to 60 t. In some specific examples, the second The contact temperature is greater than the first contact temperature. Having different contact temperatures can reduce the TAN and / or q asphaltene content in crude oil products to the ratio of TAN and / or (: 5 asphaltene content in crude oil feeds, If any, the TAN and / or C5 asphaltenes are reduced to a greater extent when the first and second contact temperatures are the same or differ by less than 10 degrees. For example, the first contact zone may include the first Catalyst and / or fourth catalyst, and the second contact zone may contain other catalysts described herein. The first contact temperature may be 350. (:, the second contact temperature may be 300 ° C. The contact of crude oil feed with the first catalyst in the first contact zone and / or with the fourth catalyst at a higher temperature before contact with other catalysts in the second contact 200533737 contact zone may be As a result, in the crude oil feed, the same principle as when the difference between the first and second contact temperature is within 10 ° C Compared with the reduction of TAN and / or c5 asphaltenes in the feed, there is more reduction of TAN and / or C5 asphaltenes. Examples The following proposes carrier preparation, catalyst preparation, and the selection of catalyst configuration and control contact conditions. Non-limiting example of the system. Example 1. ___ U ’s second carrier system uses 585 grams of water and 8 grams of glacial nitric acid to 576 grams of aluminum oxide (Criterion Catalysts and Technogies LP, Michigangail

City，Michigan，U.S.Α·)研磨35分鐘製備。所得到的研磨 混合物係透過1.3 Tril〇beTM模板擠出，於9〇至125之 間乾燥，接著在918 t：下煅燒，得到65〇克具有中位孔徑 為I82 A的煅燒載體。將此煅燒載體放入Lindberg爐中。 使爐溫於1.5小時過程中升到1 〇〇〇至n 〇〇它，然後保持 在此乾圍内2小時以生產載體。此載體在每克載體中包含 〇·〇〇〇3克的γ氧化鋁，0·00〇8克的α氧化鋁，〇〇2〇8克的δ · 氧化銘，和0.9781克的θ氧化銘，其藉由叉射線繞射測定。 此載體具有llOmVg的表面積和〇·821 cmVg的總孔體積。 此載體具有中位孔徑為232 A的孔徑分佈，該孔徑分佈中 有66.7%的總孔數具有在85人之中位孔徑範圍内的孔徑。 此實施例說明如何製備具有孔徑分佈至少為18〇人且 包含至少0.1克Θ氧化鋁的載體。City, Michigan, U.S.A.) was prepared by milling for 35 minutes. The resulting milled mixture was extruded through a 1.3 TrilObeTM template, dried between 90 and 125, and then calcined at 918 t: to obtain 650 g of a calcined support having a median pore size of I82A. This calcined support was placed in a Lindberg furnace. The temperature of the furnace was raised to 1,000 to 2000 in the course of 1.5 hours, and then kept in this dry area for 2 hours to produce a carrier. This carrier contained 0.0003 g of gamma alumina, 0.0008 g of alpha alumina, 0.0008 g of δ · oxide, and 0.9781 g of theta oxide per gram of carrier. , Which is measured by cross-ray diffraction. This support has a surface area of 110 mVg and a total pore volume of 0.82 cmVg. This carrier had a pore size distribution with a median pore size of 232 A, and 66.7% of the total number of pores in the pore size distribution had a pore size in the range of 85 people. This example illustrates how to prepare a support having a pore size distribution of at least 180 persons and containing at least 0.1 g of Θ alumina.

91 200533737 tJL飢觸嫫。 釩觸媒係以下列方式製備。由實施例1所述之方法製 備的氧化鋁載體用釩浸潰溶液浸潰，其藉由結合7.69克的 v〇S〇4與82克的去離子水而製備。該溶液的pH值為2 27。 氧化鋁載體（100 g)係利用釩浸潰溶液浸潰，以偶然攪 動老凡化2小時，於125 °C下乾燥數小時，接著在480。(： 下ife燒2小時。所得觸媒在每克觸媒中含有〇 〇4克的釩， 其餘。卩分為載體。此釩觸媒具有中位孔徑為35〇人的孔徑 分佈，0.69Cm3/g的孔體積，和n〇m2/g的表面積。此外， 釩觸媒的孔徑分佈中有66·7〇/〇的總孔數具有在70人之中位 孔徑範圍内的孔徑。 此實施例說明製備具有中位孔徑至少為23〇 Α之孔徑 分佈的第5攔觸媒。 例3·~~裝備具有中位孔徑趸少為230 A之孔徑分 佈的鉬觸媒。 翻觸媒係以下列方式製備。由實施例1所述之方法製 備的氧化紹載體用翻浸潰溶液浸潰。此鉬浸潰溶液係藉由 結合 4.26 克的（ΝΗ4)2Μ〇2〇7、6·38 克的 Μο03、1·12 克的 30% Η2〇2、〇·27克的單乙醇胺（ΜΕΑ)，與6.51克的去離子水形 成漿液而製備。此漿液係加熱至65 °C直到固體溶解為止。 使加熱溶液冷卻至室溫。該溶液的pH值為5.36。用離子 水將溶液體積調整至82 mL。91 200533737 tJL was hungry. The vanadium catalyst is prepared in the following manner. The alumina support prepared by the method described in Example 1 was impregnated with a vanadium impregnation solution, which was prepared by combining 7.69 g of VOSO4 and 82 g of deionized water. The pH of this solution was 2-27. The alumina support (100 g) was impregnated with a vanadium impregnation solution, aged by accident for 2 hours, dried at 125 ° C for several hours, and then at 480. (: Burn under ife for 2 hours. The catalyst obtained contains 0.004 grams of vanadium in each gram of catalyst, and the rest is divided into carriers. This vanadium catalyst has a pore size distribution with a median pore size of 350,000 people, 0.69 Cm3 pore volume / g, and a surface area of nom2 / g. In addition, the pore size distribution of the vanadium catalyst has a total pore number of 66 · 70 / 〇 with a pore size in the range of 70 people's median pore size. This implementation The example illustrates the preparation of a fifth catalyst with a pore size distribution with a median pore size of at least 23〇A. Example 3 · ~~ Equipped with a molybdenum catalyst with a pore size distribution with a median pore size of less than 230 A. The following catalysts are used: Prepared in a row manner. The oxide support prepared by the method described in Example 1 was impregnated with an impregnation solution. This molybdenum impregnation solution was obtained by combining 4.26 g of (ΝΗ4) 2MO207 and 6.38 g. Mο03, 1.12 grams of 30% Η202, 〇27 grams of monoethanolamine (MEA), and 6.51 grams of deionized water were prepared as a slurry. This slurry was heated to 65 ° C until the solids dissolved. The heated solution was allowed to cool to room temperature. The pH of the solution was 5.36. The volume of the solution was adjusted to 82 mL with ionized water.

氧化銘載體（10 0克）係利用錮浸潰溶液浸潰，以偶然挽 動老化2小時，於12 5 °C下乾燥數小時，接著在4 8 0 °C 92 200533737 下煅燒2小時。所得觸媒在每克觸媒中含有〇〇4克的钥， ，、餘邛刀為載體。此鉬觸媒具有中位孔徑為人的孔徑 刀佈0.77 cm /g的孔體積，和116 m2/g的表面積。此外， 銦觸媒的孔徑分佈中有67 7%的總孔數具有在％ A之中位 孔徑範圍内的孔徑。 此實施例說明製備具有中位孔徑至少為23〇 A之孔徑 分佈的第6攔觸媒。 复施例上~氫具有中每徑至少為230 A之孔徑分 #的鉬/釩觸媼。 鉬/釩觸媒係以下列方式製備。由實施例丨所述之方法 製備的氧化鋁載體用如下製備的鉬/釩浸潰溶液浸潰。第一 種/合液係藉由結合2.14克的（NH4)2Mo2〇7、3.21克的Mo03、 0.56克的30%過氧化氫（Η"2)、〇14克的單乙醇胺（MEA)， 與3.28克的去離子水形成漿液而製造。此漿液係加熱至65 C直到固體溶解為止。使加熱溶液冷卻至室溫。 第二種溶液係藉由結合3.57克的V0S04與40克的去 離子水而製造。使第一種溶液和第二種溶液結合，添加足 夠的去離子水使結合溶液的體積達到8 2 ml以產生銦/飢浸 潰溶液。將氧化鋁用鉬/釩浸潰溶液浸潰，以偶然攪動老化 2小時，於125 °C下乾燥數小時，接著在480 °C下煅燒2 小時。所得觸媒在每克觸媒中含有〇·〇2克的釩和〇 〇2克 的鉬，其餘部分為載體。此鉬/釩觸媒具有中位孔徑為300人 的孔徑分佈。 此實施例說明製備具有中位孔徑至少為230 Α之孔徑 200533737 分佈的第6欄金屬和第5攔金屬觸媒。 ， 例5·~~三種觸嬅的接觸。 在中央配置有測溫插套的管式反應器係配備熱電偶以 測量整個觸媒床的溫度。此觸媒床係藉由在測溫插套和内 壁之間的空間填充觸媒和碳化矽（2〇_grid，stanf〇u Materials; AHso Viej0, CA)而形成。咸信此種碳化矽如果 有的話，在本文中所述的操作條件下具有低的催化性質。 在將混合物放入反應器的接觸區部位之前，使所有觸媒與 等體積量的碳化石夕摻合。 φ 反應器的原《由進料流動係由反應器的頂部至反應器的 底部。碳化石夕係配置在反應器的底部作為底部載體。底部 的觸媒/碳化矽混合物（42 cm3)係配置在該碳化矽上方以形 成底部接觸區。底部觸媒具有中位孔徑為77 A的孔徑分 佈，该孔徑分佈中有66 7%的總孔數具有在2〇 A之中位孔 徑範圍内的孔徑。該底部觸媒在每克觸媒中含有〇 〇95克 的錮和0.G25克的^，其餘部分為氧化紹載體。 中間的觸媒/碳化石夕混合物（56 cm3)係配置在底部接觸 · 區上方以形成中間接觸區。令間觸媒具有中位孔徑為98 A 的孔徑分佈，該孔徑分佈中冑66 7%的總孔數具有在Μ A 之中位孔徑範圍内的孔徑。該中間觸媒在每克觸媒中含有 〇.〇2克的鎳和0.08克的鉬，其餘部分為氧化鋁載體。 品頂邛的觸媒/碳化矽混合物（42 cm3)係配置在中間接觸 區上方以形成頂部接觸區。頂部觸媒具有中位孔徑為192入 的孔徑分佈，在每克觸媒中含有〇·〇4克的鉬，其餘部分主 94 200533737 要為γ氧化鋁載體。 碳化石夕係配置在頂部接觸區上方以填充空位並且作為 預熱區。觸媒床係裝入Lindberg爐，其包括對應於預熱區、 頂部、中間’和底部接觸區，及底部載體的五個加熱區。 觸媒係藉由將5體積％硫化氫和95體積％氫氣的氣態 混合物以每單位體積（mL)觸媒總量（碳化矽並不視為觸媒的 體積部分）1.5升之氣態混合物的速率導入接觸區而形成硫 化物。接觸區的溫度於i小時過程中提高到2〇4(4〇〇。^ ) 並且保持在204 °C下2小時。保持在204 °C下之後，接 觸區以每小時10 。〇 (50 T)的速率逐漸提高到316 (600 F )。使接觸區保持在3丨6它下一小時，於}小時過 程中逐漸升到370。<： (700卞）並且保持在37〇下兩小 日守。使接觸區冷卻至周圍溫度。 過濾Gulf of Mexico中Mars鑽臺的原油，接著在93艺The oxidized carrier (100 g) was impregnated with a samarium immersion solution, aged by accident for 2 hours, dried at 12 5 ° C for several hours, and then calcined at 4 80 ° C 92 200533737 for 2 hours. The obtained catalyst contained 004 grams of key in each gram of catalyst, and Yu and Dao were used as carriers. This molybdenum catalyst has a pore volume with a median pore diameter of 0.77 cm / g, and a surface area of 116 m2 / g. In addition, 67.7% of the total pore number in the pore size distribution of the indium catalyst has a pore size within the median pore size range of% A. This example illustrates the preparation of a sixth catalyst having a pore size distribution with a median pore size of at least 230 A. In the re-application example, hydrogen has a molybdenum / vanadium contact with a pore size of at least 230 A in each diameter. The molybdenum / vanadium catalyst was prepared in the following manner. The alumina support prepared by the method described in Example 丨 was impregnated with a molybdenum / vanadium impregnation solution prepared as follows. The first type is a combination of 2.14 grams of (NH4) 2Mo2 07, 3.21 grams of Mo03, 0.56 grams of 30% hydrogen peroxide (Η " 2), 014 grams of monoethanolamine (MEA), and 3.28 grams of deionized water is made into a slurry. This slurry was heated to 65 C until the solids were dissolved. The heating solution was allowed to cool to room temperature. The second solution was made by combining 3.57 grams of VOS04 with 40 grams of deionized water. The first solution was combined with the second solution, and sufficient deionized water was added to bring the volume of the combined solution to 8 2 ml to produce an indium / starved solution. The alumina was impregnated with a molybdenum / vanadium impregnation solution, aged by accidental agitation for 2 hours, dried at 125 ° C for several hours, and then calcined at 480 ° C for 2 hours. The obtained catalyst contained 0.02 g of vanadium and 0.02 g of molybdenum per gram of the catalyst, and the remainder was a carrier. This molybdenum / vanadium catalyst has a pore size distribution with a median pore size of 300 people. This example illustrates the preparation of a column 6 metal and a column 5 metal catalyst with a pore size 200533737 distribution with a median pore size of at least 230 A. , Example 5 · ~~ Three types of contact. A tubular reactor with a temperature-measuring insert in the center is equipped with a thermocouple to measure the temperature of the entire catalyst bed. The catalyst bed is formed by filling the space between the temperature measuring sleeve and the inner wall with catalyst and silicon carbide (20_grid, stanfou materials; AHso Viej0, CA). It is believed that this silicon carbide, if any, has low catalytic properties under the operating conditions described herein. Prior to placing the mixture in the contact zone of the reactor, all catalysts were blended with an equal volume of carbides. The original φ reactor from the feed flow system from the top of the reactor to the bottom of the reactor. The carbonized fossils are arranged at the bottom of the reactor as a bottom carrier. A catalyst / silicon carbide mixture (42 cm3) at the bottom is placed above the silicon carbide to form the bottom contact area. The bottom catalyst has a pore size distribution with a median pore size of 77 A. In this pore size distribution, 66 7% of the total number of pores have a pore size in the range of 20 A. The bottom catalyst contained 0.995 g of gadolinium and 0. G of 25 g per g of the catalyst, and the remainder was an oxide carrier. The middle catalyst / carbon fossil evening mixture (56 cm3) is arranged above the bottom contact area to form the middle contact area. Let the intercatalyst have a pore size distribution with a median pore size of 98 A. In this pore size distribution, 胄 66 7% of the total number of pores have a pore size within the range of the median pore size of M A. The intermediate catalyst contained 0.02 g of nickel and 0.08 g of molybdenum per gram of catalyst, and the remainder was an alumina carrier. The catalyst / Silicon Carbide (42 cm3) of Pingdingyu is placed above the middle contact area to form the top contact area. The top catalyst has a pore size distribution with a median pore diameter of 192 in. It contains 0.04 g of molybdenum per gram of catalyst, and the remaining part is mainly alumina support. The carbide fossils are arranged above the top contact area to fill the vacancies and serve as a preheating area. The catalyst bed is loaded into a Lindberg furnace and includes five heating zones corresponding to the preheating zone, the top, middle 'and bottom contact zones, and the bottom carrier. The catalyst is a rate of 1.5 liters of a gaseous mixture per unit volume (mL) of the gaseous mixture of 5 vol% hydrogen sulfide and 95 vol% hydrogen gas (silicon carbide is not considered as a volume part of the catalyst). The contact area is introduced to form a sulfide. The temperature of the contact zone was increased to 204 (400. ^) during i hours and maintained at 204 ° C for 2 hours. After keeping it at 204 ° C, the contact area was 10 hrs. The rate of 0 (50 T) was gradually increased to 316 (600 F). The contact area was kept at 3,6 for the next hour, and gradually increased to 370 during} hours. <: (700 卞) and stayed at 37 ° for two hours. Allow the contact area to cool to ambient temperature. Filter crude oil from the Mars rig in the Gulf of Mexico.

個接觸區的溫度係接著以下列順序增加和 °F) 500小時，接著為388它 管加和保持·· 3 7 9 (730 °F) 500 小時， 95 (742 200533737 接著為 390 艺 f734 + (F) 1800 小 4，接著為 394 〇c °F ) 2400 小時。 、:產物（換㊁之為原油產物和氣體）離開觸媒床。將總 產物導入乳液相分離器。於氣液相分離器中，將總產物分 離成原油產物和氣體。系統的氣體輸入係由質量流量控制 器測定。離開系統的氣體係由測濕計測定。原油產㈣定 期刀析以測定原油產物成分的重量百分率。所列結果為成The temperature of each contact zone was then increased in the following order and ° F) for 500 hours, followed by 388 tube addition and hold. · 3 7 9 (730 ° F) for 500 hours, 95 (742 200533737 and then 390 ff734 + ( F) 1800 min 4 followed by 394 ° C ° F) 2400 hours. : The products (in other words, crude oil products and gases) leave the catalyst bed. The total product was introduced into an emulsion phase separator. The total product is separated into a crude product and a gas in a gas-liquid separator. The gas input to the system is measured by a mass flow controller. The gas system leaving the system is determined by a hygrometer. Crude oil production is periodically analyzed to determine the weight percent of crude oil product components. The listed results are

刀之實測重！百分率的平均值。原油產物性質係摘要於 7的表1中。 ' Q 如表1所示，原油產物在每克原油產物中具有〇 〇〇75 克的3 &里，〇·255克的殘留物含量，〇 〇〇〇7克的含氧量。 原油產物具有MCR含量與cs瀝青質含量的比率為19里及 〇·09的TAN。鎳和飢的總量為22.4 wtppm。 觸媒壽命係藉由測量加權平均床溫度（“WABT”）對原油 進料的運轉時間而決定。觸媒壽命可能與觸媒床的溫度相 關。咸^當觸媒壽命減短時，WABT會增加。圖8為本實 她例中所述用於改善接觸區中的原油進料之WABt對時間 _ (t )的圖不。曲線136係表示三個接觸區的平均WABT對 原油進料與頂部、中間’和底部觸媒接觸之運轉時間的時 數。於大多數的運轉時間過程中，接觸區的WABT僅改變 、、’、 。從相當穩定的WABT來看，可判斷觸媒的催化 活性並未受到影響。典型而言，3000至3500小時的中間 工廠運轉時間與1年的工業操作相關。 a 此實施例說明在控制接觸條件的情況下，使原油進料 96 200533737 與具有中位孔徑至少為180 A之孔徑分佈的一種觸媒接觸 以及與具有中位孔徑介於9〇至18〇 A範圍内之孔徑分佈， 該孔徑分佈中至少60%的總孔數具有在45人之中位孔徑 範圍内的孔徑之附加觸媒接觸，以生產含有原油產物的總 產物。如同P值所測定者，係保持了原油進料/總產物混合 物的穩定性。該原油產物與原油進料相比，具有降低的 TAN，降低的Nl/V/Fe含量，降低的含硫量，及降低的含 氧量，而原油產物的殘留物含量和VG〇含量為9〇%至ιι〇% 之原油進料的該等性質。 i·施例6·原生產^^^1^^於90至/川人 IU内之孔徑的兩籍觸蛘夕！1里__ 反應器設備（除了接觸區的數目和内容以外）、觸媒形 成硫化物法、分離總產物的方法和分析原油產物的方法係 與實施例5所述者㈣。每—種觸制與等㈣的碳化石夕 混合0The actual weight of the knife! Percentage mean. Crude product properties are summarized in Table 1 of 7. As shown in Table 1, the crude oil product has a residual content of 0.0075 g per gram of crude product, a residual content of 255 g, and an oxygen content of 007 g. The crude oil product has a TAN with a ratio of MCR content to cs asphaltene content of 19 li and 0.09. The total amount of nickel and hunger was 22.4 wtppm. The catalyst life is determined by measuring the weighted average bed temperature ("WABT") operating time of the crude feed. The catalyst life may be related to the temperature of the catalyst bed. As the catalyst life decreases, WABT increases. Figure 8 is a graph of WABt versus time _ (t) for improving crude oil feed in the contact zone described in this example. Curve 136 represents the average number of hours that the WABT vs. contact time of the crude feed with the top, middle, and bottom catalysts in the three contact zones. During most of the running time, the WABT in the contact zone changes only,, ', and. From the perspective of fairly stable WABT, it can be judged that the catalytic activity of the catalyst is not affected. Typically, 3000 to 3500 hours of intermediate plant uptime are associated with one year of industrial operation. a This example illustrates that under the control of contact conditions, crude oil feed 96 200533737 is brought into contact with a catalyst having a pore size distribution with a median pore size of at least 180 A and with a median pore size between 90 and 18 A A pore size distribution within the range. At least 60% of the total pore numbers in the pore size distribution have additional catalyst contacts with pore sizes in the median pore size range of 45 to produce a total product containing crude oil products. As measured by the P value, the stability of the crude oil feed / total product mixture was maintained. Compared with the crude oil feed, the crude oil product has a reduced TAN, a reduced Nl / V / Fe content, a reduced sulfur content, and a reduced oxygen content, while the residual content and VG0 content of the crude product are 9 0% to ιι0% of these properties of crude oil feed. i · Example 6 · Original production ^^^ 1 ^^ The two series of pore diameters within 90 to / Sichuan people IU are touching! 1 __ Reactor equipment (except the number and content of contact zones), catalyst sulfide formation method, total product separation method, and crude oil product analysis method are the same as those described in Example 5. Every kind of carbonized fossils that touch and wait

反應器的原油進料流動係由反應器的頂部至反應器 底部。該反應器係以下列方式由底部填充至頂部。：: 係配置在反應器的底部作為底部載體。底部的觸媒/碳化 混合物⑽W)係配置在該碳切上方以形成底部接 區。底部觸媒具有中位孔徑4 127 A的孔徑分佈，该孔 分佈中有66.7%的總孔數具有在32A之中位孔徑以内的 徑。該底部觸媒在每克觸心包含m克的錮和⑽ 的鎳，其餘部分為載體。 頂部的觸媒/碳化石夕混合物（8〇 cm3)係配置在底部⑹ 97 200533737 區上方以形成頂部The crude oil feed flow from the reactor is from the top of the reactor to the bottom of the reactor. The reactor was filled from bottom to top in the following manner. ::: It is arranged at the bottom of the reactor as the bottom carrier. The catalyst / carbonized mixture (W) at the bottom is disposed above the carbon cut to form a bottom junction. The bottom catalyst has a pore size distribution with a median pore size of 4 127 A, and 66.7% of the total pore number in the pore distribution has a diameter within the 32 A median pore size. The bottom catalyst contains m grams of rhenium and rhenium nickel per gram of contact, and the remainder is a carrier. The catalyst / carbon fossil mixture (80 cm3) at the top is arranged above the bottom ⑹ 97 200533737 area to form the top

的孔徑分佈，…、頂摘媒具有中位孔徑為100A 之中位孔徑以==佈中有66.7%的總孔數具有在2〇人 克的錄和…克的Γ㈣部觸媒在每克觸媒中包含〇·03 在第一接觸區上方以目填充其Γ部分為氧化紹。碳切係配置 裝入㈤位並且作為預熱區。觸媒床係 I /、包括對應於預熱區、兩個接觸區，及 履"卩戟體的四個加熱區。 #徂：有摘要於表2’圖9之性質的BS_4原油(—a) '、厂入反應H頂部。原油進料係流過反應器的預熱區、 广P接觸區、底部接觸區和底部載體。原油進料係於氫氣 在下〃每種觸媒接觸。接觸條件如下··氫氣與供應至 Μ Γ之原油進料的比率為16〇 (1〇〇〇 ， MSVg i f，及壓力為6·9 Mpa (1〇147㈣。兩個接觸 區係加熱至260 °C (500卞）並且保持在260 °C (500卞） 下287小時。兩個接觸區的溫度係接著以下列順序增加和 呆持 270 c (525 F) 190 小時，接著為 288 °C (550 T) 16】、日守’接著為315 °C (600 T ) 360小時，接著為343 °C (650 F ) 120小時，以達到丨丨73小時的總運轉時間。 總產物離開反應器並且像實施例5所述一樣地分離。 原油產物在加工期間具有〇·42的平均Tan和12.5的平均 I比重。遠原油產物在每克原油產物中含有0.0 0 2 3克的 硫’ 0.0034克的氧，0.441克的VGO，和0.378克的殘留 物。原油產物的額外性質係列於圖9的表2中。 此實施例顯示使原油進料與具有中位孔徑介於90至 98 200533737 圍内之孔後分佈的觸媒接觸 的性質相比，具有降低的tan，降低的Η· S里’及降低的合ft旦 _ 含量為99%和100%之產物的殘留物含量和_ 之原油進料的個別性質。 的接觸。 反應裔設備丨除了 # @ $ 、妾觸區的數目和内容以外）、觸媒、 、、心產物分離法、原油產^八 y> 實施例6所述者相同。” ^媒形成硫化物法係與 ^有摘要於表3’圖1G之性f的原油進料CO原油） ，…°入反應益頂部。原油進料係流過反應器的預献區、 頂部接觸區、底部接觸區和底部載體。接觸條件如;：氫 氣與供應至反應器之原油進料的比…〇 Μ · SCF.LHSVUy，及壓力為69奶（編7响。 兩個接觸區係逐漸加熱i 343。。（㈣。F)。總運轉時間 為1 0 0 7小時。 原油產物在加工期間具有0·16的平均tan和162的 平均ΑΡΙ比重。該原油產物含有！ 9 wtppm的約，6卿㈣ 的納，0.6,的辞，和3 wtppm的鉀。該原油產物在 每克原油產物中含有請33克的硫，G GG2克的*，Ο」％ 克的VGO’和0.401克的殘留物。原油產物的額外性質係 列於圖10的表3中。 此實施例顯示使原油進料與具有孔徑分佈在9〇至“Ο A之範圍内的選定觸媒接觸以生產原油產物，其具有降低 的TAN ’降低的總鈣、鈉、辞，和鉀含量，而原油產物的 99 200533737 含硫量、VGO含量和殘留物含量為76%、94%和1〇3%之 原油進料的個別性質。 1_跑例8 __媒系統在各播搵 觸條件下的接觸。 每個反應器設備（除了接觸區的數目和内容以外）、每 個觸媒形成硫化物法、每個總產物分離法和每個原油產物 分析係與實施你"所述者相同。除另有說明外，所有觸媒 係以2份碳切對丨份觸媒的體積比與碳切混合。通過 每個反應器的原油進料流動係由反應器 ㈣。碳切聽置在每個反應器的底部作為底部=的 母個反應器具有底部接觸區和頂部接觸區。在觸媒/碳化石夕 混合物放入每個反應器的接觸區之後，碳化矽係配置在頂 Ρ接觸區上方以填充空位並且作為每個反應器的預熱區。 每個反應器係裝人Lindberg爐’其包括對應於預熱區、兩 個接觸區，及底部載體的四個加熱區。 於貫她例8中，未煅燒過的鉬/鎳觸媒/碳化矽混合物 ⑽3)係配置在底部接觸區中。該觸媒 〇-克的一克的錄，和咖克的鱗二；： 為氧化鋁載體。 包a具有中位孔徑為丨80 A的孔徑分佈之觸媒的鉬觸 媒/碳化矽混合物（12 cm3)係配置在頂部接觸區中。該翻觸 媒具有每克觸媒中含〇.〇4克鉬的總含量，其餘部分為包含 母克載體中至少為〇.5〇克γ氧化|g的載體。 於實施例9中，未煅燒過的鉬/鈷觸媒/碳化矽混合物（48 100 200533737 cm3)係配置在兩個接觸區中。該未煅燒過的鉬/鈷觸媒包含 〇·Μ3克的銦’ 0.〇43克的鈷，和0.021克的磷，其餘部= 為氧化鋁載體。 銷觸媒/碳化石夕混合物（12 cm3)係配置在頂部接觸區 中。該翻觸媒與實施例8之頂部接觸區者相同。 於實施例10中，如實施例8之頂部接觸區中所述的鉬 觸媒係與碳化矽混合並配置在兩個接觸區中（6〇 em3)。 於實施例11中，未煅燒過的鉬/鎳觸媒/碳化矽混合物 (48 cm3)係配置在底部接觸區中。該未煅燒過的鉬/鎳觸媒魯 在每克觸媒中包含〇.〇9克的鉬，〇·025克的鎳，和〇〇ι克 的麟’其餘部分為氧化鋁載體。 鉬觸媒/碳化矽混合物（12 cm3)係配置在頂部接觸區 中。該翻觸媒與實施例8之頂部接觸區者相同。 過濾來自Mars鑽臺（Gulf of Mexico)的原油，接著在93 C (200 T)下，於烘箱中加熱12至24小時以生成用於實 施例8至1 1之具有摘要於表4，圖丨丨之性質的原油進料。 將原油進料供給入此等實施例的反應器頂部。原油進料係 _ 流過反應器的預熱區、頂部接觸區、底部接觸區和底部载 體。原油進料係於氫氣存在下與每一種觸媒接觸。每個實 施例的接觸條件如下：氫氣與接觸期間之原油進料的比率 為160 NmVmMl〇〇〇 SCFB)，及每個系統的總壓力為μ MPa (1014.7 psi)。在接觸的前2〇〇小時期間，LHSV為2.〇 h ，而接著在剩下的接觸時間LHSV降低至1〇 h-i。所有 接觸區的溫度為343 °C (650 T)接觸500小時。在5〇〇 101 200533737 小％後’所有接觸區的溫度係控制如下：使接觸區的溫度 升到354 t： (670 T)，保持在3M t下2〇〇小時；升到 366 C (690 °F)，保持在 366 °C 下 200 小時；升到 371 °C (700 F )，保持在 371 °C 下 1000 小時；升到 385 °C (725 F )’保持在385 °C下200小時；然後升到399 °C (750 °F ) 的最終溫度並保持在399 °C下200小時，以達到23〇〇小 時的總接觸時間。 原油產物係定期分析以測定TAN、原油進料之氫的吸 取、P值、VGO含量、殘留物含量，及含氧量。實施例8 至1 1所生產之原油產物性質的平均值係列於圖11的表5 中。 圖1 2為實施例8至11的每個觸媒系統之原油產物之 p值（“p”）對運轉時間（“t”）的圖示。原油進料具有至少 的P值。曲線14〇、142、144，和146係表示藉由使原油 進料個別與實施例8至丨丨的四種觸媒系統接觸所得到的 原油產物之P值。對於實施例8至1〇的觸媒系統而言， 達到2300小時的原油產物之p值剩下至少為1 ·5。於實施 例1 1中，多數運轉時間的ρ值大於丨·5。在實施例11運 轉（2300小時）結束時，ρ值為14。從每個試驗的原油產物 之Ρ值來看，可推斷在每個試驗中原油進料於接觸期間保 持相當穩定（例如原油進料沒有相分離）。如圖丨2所示，除 I實施例10中的ρ值增加之外，原油產物之ρ值在大: 刀的每個試驗中均保持相當固定。 圖1 3為氫氣存在下四種觸媒系統的原油進料之氫的、、爭 102 200533737 吸取γ H2 )對運轉時間（“t”）的圖示。曲線MS、15〇、m 1 54係表不藉由使原油進料個別與實施例8至η的每個觸 媒系統接觸所得到之氫的淨吸取。原油進料之氮的淨吸取 在2300小時的運轉期間係於7至48 NmVm3 (43.8至3〇〇 SCFB)的抵圍内。如圖13所示，原油進料之氫的淨吸取在 母個试驗中柄當固定。 ^圖Μ為實施例8至1 1的每個觸媒系統之以重量百分 率表不的原油產物之殘留物含量（“R”）對運轉時間（“t”）的圖 不。於四個試驗的每一個之中，原油產物具有殘留物含i _ 為88/至90%之原油進料的殘留物含量。曲線、⑸、⑽、 1 62係表不藉由使原油進料個別與實施例8至1 1的觸媒系 統接觸所得到之原油產物的殘留物含量。如圖Μ所示:、 原油產物的殘留物含量在大部分的每個試驗中均保持相當 圖15為實施例8至11的每個觸媒系統之原油產物 API比重改變（“Δ Αρι”）對運轉時間的圖示。曲線…The pore size distribution, ..., the top pick media has a median pore size of 100A, the median pore size is 66.7% of the total number of pores in the cloth. The catalyst contains 0.03 and the Γ portion is filled with a mesh over the first contact area as oxide. Carbon cutting system configuration is loaded into the position and used as a preheating zone. The catalyst bed is I /, including four heating zones corresponding to the preheating zone, two contact zones, and the " mould body. # 徂: BS_4 crude oil (—a) 'with the properties summarized in Table 2 ′ and FIG. The crude oil feed flows through the preheating zone, the wide P contact zone, the bottom contact zone, and the bottom carrier of the reactor. The crude oil feed was contacted with hydrogen under each catalyst. The contact conditions are as follows: The ratio of hydrogen to the crude feed supplied to Γ is 160 (1000, MSVg if, and pressure is 6.9 Mpa (10147㈣). The two contact zones are heated to 260 ° C (500 卞) and maintained at 260 ° C (500 卞) for 287 hours. The temperature in the two contact zones was then increased and held at 270 c (525 F) for 190 hours, followed by 288 ° C (550 T) 16], Rishou 'followed by 360 hours at 315 ° C (600 T) and 120 hours at 343 ° C (650 F) to reach a total run time of 73 hours. The total product leaves the reactor and looks like It was separated as described in Example 5. The crude oil product had an average Tan of 0.42 and an average I specific gravity of 12.5 during processing. The far crude oil product contained 0.02 3 grams of sulfur '0.0034 grams of oxygen per gram of crude oil product. , 0.441 grams of VGO, and 0.378 grams of residue. The additional properties of the crude oil series are shown in Table 2 of Figure 9. This example shows a crude oil feed with pores with a median pore size within the range of 90 to 98 200533737. Compared to the nature of the catalyst distribution after contact, it has a reduced tan and a reduced Η · S ' Reducing the residual content of the product with 99% and 100% content and the individual properties of the crude oil feed. Contact. Reactive equipment (except for # @ $, the number and content of contact areas) , Catalyst,, product separation method, crude oil production ^ eight y > The same as described in Example 6. "^ medium formation sulfide method and ^ crude oil feed has the characteristics f as summarized in Table 3 'Figure 1G CO crude oil),… ° into the top of the reaction benefit. Crude oil feed flows through the pre-production zone, top contact zone, bottom contact zone and bottom carrier of the reactor. Contact conditions such as: hydrogen and crude oil feed to the reactor The ratio of 〇 ·· SCF.LHSVUy, and the pressure is 69 milk (ed. 7). The two contact zones gradually heat i 343 ... (㈣.F). The total operating time is 10 7 hours. The crude product is at During processing has an average tan of 0.16 and an average specific gravity of 162. The crude oil product contains! 9 wtppm of sodium, 6 cyanine sodium, 0.6, and 3 wtppm potassium. The crude oil product is per gram of crude oil The product contains 33 grams of sulfur, G GG2 grams of *, 〇 ″% grams of VGO 'and 0.401 grams of residue The additional properties of the crude oil series are shown in Table 3 of Figure 10. This example shows that a crude oil feed is contacted with a selected catalyst having a pore size distribution in the range of 90 to "0 A to produce a crude oil product, which has Reduced TAN 'reduced total calcium, sodium, potassium, and potassium content, while crude oil products have 99 200533737 sulfur content, VGO content, and residue content of 76%, 94%, and 103% of individual crude oil feeds nature. 1_ 跑 例 8 __ Contact of the media system under various broadcast conditions. Each reactor device (except for the number and content of contact zones), each catalyst sulfide formation method, each total product separation method, and each crude oil product analysis system are the same as those implemented by you. Unless otherwise stated, all catalysts are mixed with carbon cut at a volume ratio of 2 parts carbon cut to 1 part catalyst. The crude feed stream through each reactor is passed through the reactor ㈣. The carbon cut was placed at the bottom of each reactor as the bottom = the parent reactor has a bottom contact zone and a top contact zone. After the catalyst / carbide carbide mixture was placed in the contact area of each reactor, the silicon carbide system was arranged above the top contact area to fill the voids and serve as a preheating area for each reactor. Each reactor is housed in a Lindberg furnace 'which includes four heating zones corresponding to a preheating zone, two contact zones, and a bottom carrier. In Example 8, the uncalcined molybdenum / nickel catalyst / silicon carbide mixture ⑽3) was arranged in the bottom contact area. The catalyst is 0-gram of one gram, and gram of scale two; is an alumina carrier. A molybdenum catalyst / silicon carbide mixture (12 cm3) with a catalyst having a pore size distribution with a median pore size of 80 A is arranged in the top contact area. The flip-catalyst has a total content of 0.04 g of molybdenum per gram of catalyst, and the remainder is a carrier containing at least 0.50 g of γ-oxidized | g of the mother gram carrier. In Example 9, an uncalcined molybdenum / cobalt catalyst / silicon carbide mixture (48 100 200533737 cm3) was disposed in two contact areas. The uncalcined molybdenum / cobalt catalyst contained OM3 g of indium '0.043 g of cobalt and 0.021 g of phosphorus, and the remainder = alumina support. A pin catalyst / carbonized carbide mixture (12 cm3) is placed in the top contact area. This flip catalyst is the same as that in the top contact area of Example 8. In Example 10, the molybdenum catalyst system described in the top contact region of Example 8 was mixed with silicon carbide and arranged in two contact regions (60 em3). In Example 11, an uncalcined molybdenum / nickel catalyst / silicon carbide mixture (48 cm3) was disposed in the bottom contact area. The uncalcined molybdenum / nickel catalyst contained 0.09 g of molybdenum, 0.025 g of nickel, and 0.00 g of lin ', and the remainder was alumina support. A molybdenum catalyst / silicon carbide mixture (12 cm3) is placed in the top contact area. This flip catalyst is the same as that in the top contact area of Example 8. The crude oil from the Mars rig (Gulf of Mexico) was filtered, and then heated in an oven at 93 C (200 T) for 12 to 24 hours to generate a summary for Examples 8 to 11 in Table 4, Figure 丨The nature of the crude oil feed. Crude oil feed was fed to the top of the reactors of these examples. Crude oil feed system _ flows through the preheat zone, top contact zone, bottom contact zone and bottom carrier of the reactor. The crude feed is contacted with each catalyst in the presence of hydrogen. The contact conditions for each example were as follows: the ratio of hydrogen to the crude feed during the contact was 160 NmVmM (100 SCFB), and the total pressure of each system was μ MPa (1014.7 psi). During the first 200 hours of contact, the LHSV was 2.0 h, and then the LHSV decreased to 10 h-i during the remaining contact time. The temperature of all contact zones was 343 ° C (650 T) for 500 hours of contact. After 500101 200533737 small%, the temperature of all contact zones was controlled as follows: the temperature of the contact zone was raised to 354 t: (670 T), maintained at 3M t for 200 hours; rose to 366 C (690 ° F), kept at 366 ° C for 200 hours; rose to 371 ° C (700 F), kept at 371 ° C for 1000 hours; rose to 385 ° C (725 F) 'kept at 385 ° C for 200 hours ; Then rose to a final temperature of 399 ° C (750 ° F) and held at 399 ° C for 200 hours to reach a total contact time of 23,000 hours. Crude oil products are regularly analyzed to determine the TAN, hydrogen uptake of the crude oil feed, P value, VGO content, residue content, and oxygen content. The series of average values of the properties of the crude oil products produced in Examples 8 to 11 are shown in Table 5 of FIG. 11. Figure 12 is a graphical representation of the p-value ("p") versus operating time ("t") of the crude product of each catalyst system of Examples 8 to 11. The crude feed has at least a P value. Curves 140, 142, 144, and 146 represent the P values of the crude oil products obtained by contacting the crude oil feeds individually with the four catalyst systems of Examples 8 to 丨. For the catalyst systems of Examples 8 to 10, the p-value of the crude product reaching 2300 hours is at least 1.5. In the embodiment 11, the ρ value of most of the operating time is greater than 丨 · 5. At the end of Example 11 operation (2300 hours), the ρ value was 14. From the P value of the crude oil product from each test, it can be inferred that the crude oil feed remained fairly stable during the contact during each test (for example, the crude oil feed did not have phase separation). As shown in FIG. 2, in addition to the increase in the value of ρ in Example 10, the value of ρ of the crude oil product was large: each test of the knife remained fairly constant. Figure 13 is a graphical representation of the hydrogen in the crude oil feeds of the four catalyst systems in the presence of hydrogen, and the competition time (“t”). The curves MS, 150, and m 54 represent the net uptake of hydrogen obtained by contacting the crude oil feed individually with each of the catalyst systems of Examples 8 to n. The net uptake of nitrogen from the crude feed is within a range of 7 to 48 NmVm3 (43.8 to 300 SCFB) during a 2,300-hour operation. As shown in Figure 13, the net uptake of hydrogen from the crude feed was fixed in the parent test. ^ Figure M is a graph showing the residual content of crude oil products ("R") versus operating time ("t") expressed by weight percentage for each catalyst system of Examples 8 to 11. In each of the four trials, the crude oil product had a residue content with a residue i_ of 88 / to 90% of the crude feed. The curves, ⑸, ⑽, 162 are the residual contents of crude oil products obtained by contacting the crude oil feeds individually with the catalyst systems of Examples 8 to 11. As shown in Figure M, the residual content of the crude oil product remained comparable in most of each test. Figure 15 shows the API specific gravity change of each catalyst system of Examples 8 to 11 ("ΔΑρι"). Graphical representation of running time. curve…

166 1 68、170係表示藉由使原油進料個別與實施例8 的觸媒系統接觸所得到之原油產物的ΑΡι比重。於四 試驗的每一個之中，每個原油產物具有在58.3至72·、7 ς 之範圍内的黏度。每個原油產物的Αρι比重係增加！ 度。增加的API比重係對應於217至22·95曰範圍内I 原油產物之ΑΡΙ比重。此範圍内的ΑΡΙ比重為11〇至m 之原油進料的API比重。 圖16為實施例8至11的每個觸媒系統之以重量百^ 103 200533737 率表示的原油產物之含董蔷,“ n，，、 〜3虱里（〇2 )對運轉時間（“t，，）的圖 示。曲線172、174、176、178係表示藉由使原油進料個 別與貫施例8 i 11的觸媒系統接觸所得到之原油產物的 含氧量。每個原油產物具有含氧量最多為原油進料的16%。 每個原油產物在每個試驗期間具有含氧量為每克原油產物 中0.0(H4至0.0015克的範圍内。如圖16所示原油產物 的含氧量纟200小時的接觸時間之後仍保持相當固定。原 油產物相當固定的含氧量顯示選定的有機氧化合物在接觸166 1 68 and 170 represent the Apy specific gravity of the crude oil product obtained by contacting the crude oil feed individually with the catalyst system of Example 8. In each of the four tests, each crude oil product had a viscosity in the range of 58.3 to 72 ·, 7 ς. The specific gravity of Αρι increases for each crude oil product! degree. The increased API specific gravity corresponds to the API specific gravity of the I crude product in the range of 217 to 22.95. Within this range, the API specific gravity of the API feedstock is from 110 to m. FIG. 16 shows Dong Qiang, a crude product containing crude oil products expressed in terms of weight percent of each catalyst system of Examples 8 to 11 as a percentage by weight, "n,", ~ 3 lice (〇2) versus operating time ("t ,,). Curves 172, 174, 176, and 178 represent the oxygen content of the crude oil product obtained by contacting the crude oil feed with the catalyst system of Example 8i 11 individually. Each crude product has an oxygen content of up to 16% of the crude feed. Each crude oil product has an oxygen content in the range of 0.0 (H4 to 0.0015 g per gram of crude oil product during each test period. As shown in Figure 16, the oxygen content of the crude oil product remains comparable after 200 hours of contact time Fixed. The fairly constant oxygen content of crude oil products indicates that the selected organic oxygen compounds are in contact

期間減少。因為在這些實施例中TAN也降低，所以可推斷 至少一部分的含羧酸有機氧化合物比含非羧酸有機氧化合 物選擇性減少的更多。 於實施例11中，反應條件為：371 t (7〇〇卞），壓 力為6.9 MPa (1()14.7 Psi)，及氫和原油進料的比率為⑽ (1_ SCFB)，以原油進料重量計，原油進料mcr 含量的降低為17.5 Wt%。在399它（75〇卞）的溫度下， 於相同壓力及氳和原油進料的比率下，以原油進^重量 计’原油進料MCR含量的降低為25.4 wt%。 於實施例9中，反應條件為·· 371 t (7〇〇卞），壓 力為6.9 MPa (1014.7 psi)，及氫和原油進料的比率為16〇 (1000 SCFB)，以原油進料重量計，原油進料mcr 含量的降低為17·5 wt%。在399 〇c (750卞）的溫度下， 於相同壓力及氫和原油進料的比率下，以原油進料重量 計’原油進料MCR含量的降低為19 wt〇/0。 原油進料MCR含量中此等降低的增加係顯示未煅燒 104 200533737 過的第6和10攔金屬觸媒於較高溫度下比未锻燒過的第6 和9欄金屬觸媒更能促使MCR含量的降低。 、這些實施例顯示具有相對高TAN (0.8的TAN)的原油 進料〃或夕種觸媒接觸係生產原油產物，而同時保持原 油進料/總產物混合物的穩定性並且具有相當少量氫的淨吸 取。選定的原油產物性f最多為7G%之原油進料的同樣性 質’同時原油產物的選定性質在2〇 i 3〇%之原油進料的 同樣性質範圍内。 /、體而曰，如表4所示，每個原油產物係以最多為 Nm /m (275 SCFB)的原油進料之氫的淨吸取生產。這類產 物具有平均TAN最多為原油進料的4%，平均總Ni/V含量 最多為61〇/〇之原油進料的總Ni/V含量，而同時保持高於3 的原油進料之p值。每個原油產物的平均殘留物含量為88 至90%之原油進料的殘留物含量。每個原油產物的平均 VGO含1為1 is至117%之原油進料的vG〇含量。每個原 油產物的平均API比重為11〇至117%之原油進料的 比重，而每個原油產物的黏度最多為45%之原油進料的黏 度。 貫方也例~~~~~~—原油進料在最小氫消耗詈的悄>、况下 m i 之孔徑分佈的觸媒之 於實施例12至14中，每個反應器設備（除了接觸區的 數目和内容以外）、每個觸媒形成硫化物法、每個總產物分 離法和每個原油產物分析係與實施例5所述者相同。所有 觸媒係與等體積的碳化矽混合。每個反應器的原油進料流 105 200533737 動係由反應器的頂部至反應器的底部。碳化矽係配置在每 _ 個反應為的底部作為底部載體。每個反應器包含一個接觸 區。在觸媒/碳化矽混合物放入每個反應器的接觸區之後， 碳化矽係配置在頂部接觸區上方以填充空位並且作為每個 反應器的預熱區。每個反應器係裝入Lindberg爐，其包括 對應於預熱區、接觸區，及底部載體的三個加熱區。使原 油進料於氫氣存在下與每一種觸媒接觸。 觸媒/碳化矽混合物（4〇 cm3)係配置在碳化矽上方以形 成接觸區。用於實施例12的觸媒係如實施例2所製備的 _ 釩觸媒。用於實施例丨3的觸媒係如實施例3所製備的鉬 觸媒。用於實施例14的觸媒係如實施例4所製備的鉬/釩 觸媒。 實施例12至14的接觸條件如下：氫與供應至反應器 之原油進料的比率為160 Nm3/m3 (1000 SCFB)，LHSV為1 h 1 ’及壓力為6·9 MPa (1014.7 psi)。接觸區係於一段時間 過程中逐漸加熱至343 t (65〇卞）並且保持在343艺下 120小時’以達到36G小時的總運轉時間。 · 總產物離開接觸區並且像實施例5所述一樣地分離。 在接觸期間係測定每個觸媒系統之氫的淨吸取。於實施例 12中’氫的淨吸取為]〇·7 Nm3/m3 (_65 SCFB)，原油產物 具有6·75的TAN。於實施例13中，氫的淨吸取在2.2至 3.0 Nm3/m3 (13·9至18·7 SCFB)的範圍内，原油產物具有 在0.3至0.5之範圍内的TAN。於實施例14中，在原油進 料與钥/釩觸媒的接觸期間，氫的淨吸取在 -0.05 Nm3/m3 至 106 200533737 〇·6 NmVm3 (.〇.36 SCFB ^ 4 〇 SCFB) 具有在0.2至。.5之範圍内的ΤΑΝ。目内’原油產物 從接觸期間氫的淨吸取值來看，估 觸媒接觸期間1牡原油進料與釩 ㈣觸』間 1G 7Nm3/m3(65scFB) 接觸期間的氫氣發生與習知製 七生。 今产制，丄 1丨用的風里相比，可究 程中使用較少的氯來改善劣質原油的性質。二 間而要較少的氫會傾向於降低加工原油的成本。 ， 此外，原油進料與鉬/釩觸媒的接 單獨銦觸媒所生產 座/、有低於由 〜 原，由產物的ΤΑΝ之TAN的原油產物。 觸。媒的接 每個反應器設備（除了接觸區的數目和㈣㈣卜4 個觸媒形成硫化物法、每個總產物分離法和每個原油產物 分析係與實施例5所述者相同。除另有說明外，所有觸媒 係以j份碳化石夕對i份觸媒的體積比與碳化石夕混合。每個 反應器的原油進料流動係由反應器的頂部至反應器的底 部。碳化矽係配置在每個反應器的底部作為底部載體。每 個反應器具有底部接觸區和頂部接觸區。在觸媒/碳化矽混 合物放入每個反應器的接觸區之後，碳化矽係配置在頂部 接觸區上方以填充空位並且作為每個反應器的預熱區。每 個反應器係裝入Lindberg爐，其包括對應於預熱區、兩個 接觸區，及底部載體的四個加熱區。 在每個實施例中，釩觸媒像實施例2所述一樣地製備 並且和附加觸媒一起使用。 107 200533737 於貫施例15中，附加觸媒/碳化矽混合物（45 cm3)係配 置在底部接觸區中，該附加觸媒為藉由實施例3所述之方 法製備的翻觸媒。釩觸媒/碳化矽混合物（15 cm3)係配置在 頂部接觸區中。 於實施例16中，附加觸媒/碳化矽混合物（30 cm3)係配 置在底部接觸區中，該附加觸媒為藉由實施例3所述之方 法製備的翻觸媒。釩觸媒/碳化矽混合物（30 cm3)係配置在 頂部接觸區中。 於實施例17中，附加觸媒/碳化矽混合物（3() cm3)係配 置在底部接觸區中，該附加觸媒係如實施例4所製備的鉬/ 釩觸媒。釩觸媒/碳化矽混合物（3() cm3)係配置在頂部接觸 區中。 於實施例 1 8 中，Pyrex® (Glass w〇rks c〇rp〇rati〇n，New York，U.S.A·)小珠（3〇 cm3)係配置在每個接觸區中。 用於實施例1 5至1 8之具有摘要於表5，圖1 7之性質 的原油（Santos Basin，Brazil)係供給入反應器頂部。原油進 料係流過反應器的預熱區、頂部接觸區、底部接觸區和底 部載體。原油進料係於氫氣存在下與每一種觸媒接觸。每 個實施例的接觸條件如下：氫氣與供應至反應器之原油進 料的比率在前86小時為160 Nm3/m3 (1〇〇〇 SCFB)而在剩下 的時限為 80 Nm3/m3 (500 SCFB)，LHSV 為 i y，及壓力 為6.9 MPa (1014.7 psi)。接觸區係於一段時間過程中逐漸 加熱至343 °C (650卞）並且保持在343它下以達到14〇〇 小時的總運轉時間。 108 200533737 這些實施例顯示於氫源存在下， 亍隹卜原油進料與具有中位 孔徑為350 A之孔徑分佈的第5攔今屬總说 ^ 孟屬觸媒與結合具有中 位孔徑在250 i则A範圍内之孔徑分佈的附加㈣㈣ 以生產原油產4勿，其與原油進料之同樣性質相比具有改變 的性質’而該原油產物的其 I厂王貝興原油進料之同樣性質 相比只有少置改變。此外，在知工：s日門及—& 长加期間係觀察到原油進料 之相當少量氫的吸取。 具體而言，如表5,圖！7所示，實施例15至17的原 油產物具有TAN最多4 15%之原油進料的TAN。實施例15 _ 至1 7中所生產的原油產物與原油進料的同樣性質相比， =具有最多為44%的總Ni/V/Fe含量，最多為5〇%的含 氧里，及最多為75%的黏度。此外，實施例丨5至17中所 生產的原油產物分別具有API比重為1〇〇至1〇3%之原油 進料的API比重。 對比之下，在非催化條件（實施例1 8)下所生產的原油 產物與原油進料的黏度和Αρι比重相比，係生成具有增加 钻度和降低API比重的產物。從增加黏度和降低Αρι比重 _ 來看’可推斷已引發原油進料的焦化及/或聚合。 _ϋ進料在备# LHS V下的接觸。 接觸系統和觸媒係與實施例6所述者相同。原油進料 的性貝列於圖18中的表6。接觸條件如下：氫氣與供應至 反應器之原油進料的比率為160 Nm3/m3 (1000 SCFB)，壓 力為6.9MPa(l〇i4.7pSi)，及接觸區的溫度為371 °C (7〇〇 F )達總運轉時間。於實施例19中，接觸期間的LHSV於 109 200533737 h'1增加到12 1Γ1 增加到20.7 h·1， 一段時間過程中由1 小時，接著使LHSV 小時。 ’保持在12 h·1下48 保持在20.7 h1下％ 於貝施例19中，分析原油產物以測定在LHSV為12 γ 和20.7 h_i之時限期間的丁錢、黏度、密度、彻含旦 :留物含量、雜原子含量，及有機酸金屬鹽形態的金：含 $。原油產物性質的平均值示於表6，圖18。The period decreases. Since the TAN is also reduced in these examples, it can be inferred that at least a portion of the carboxylic acid-containing organic oxygen compound has a more selective decrease than the non-carboxylic acid-containing organic oxide. In Example 11, the reaction conditions were: 371 t (700 MPa), pressure was 6.9 MPa (1 () 14.7 Psi), and the ratio of hydrogen to crude oil feed was ⑽ (1_SCFB), and crude oil was used to feed The reduction in mcr content in the crude feed was 17.5 Wt% by weight. At a temperature of 399 ° C (75 ° F), at the same pressure and the ratio of 氲 to the crude oil feed, the reduction in the MCR content of the crude oil feed, based on the crude oil feed weight, was 25.4 wt%. In Example 9, the reaction conditions were 371 t (700 MPa), pressure was 6.9 MPa (1014.7 psi), and the ratio of hydrogen to crude oil feed was 160 (1000 SCFB), based on the weight of the crude oil feed. The reduction in the mcr content of the crude feed is 17.5 wt%. At a temperature of 399 ° C (750 ° F), at the same pressure and the ratio of hydrogen and crude oil feed, the reduction in the MCR content of the crude oil feed by weight of crude oil feed was 19 wt / 0. The increase in these reductions in the MCR content of crude oil feeds indicates that uncalcined 104 200533737 6th and 10th metal catalysts have been able to promote MCR at higher temperatures than uncalcined metal catalysts in columns 6 and 9 Decreased content. These examples show that crude oil feeds with relatively high TAN (0.8 TAN) or catalyst contact systems produce crude oil products while maintaining the stability of the crude oil feed / total product mixture and have a net amount of relatively small amounts of hydrogen. draw. The selected crude product properties f are at most 7G% of the same properties of the crude feed. At the same time, the selected properties of the crude product are within the same range of 20-30% of the crude feed. In short, as shown in Table 4, each crude oil product is produced by a net absorption of hydrogen from a crude oil feed of at most Nm / m (275 SCFB). This type of product has a total Ni / V content of a crude oil feed with an average TAN of up to 4% of the crude oil feed and an average total Ni / V content of up to 61/0, while maintaining a p of crude oil feed above 3 value. The average residue content of each crude oil product is from 88 to 90% of the residue content of the crude feed. The average VGO per crude product contains a vGO content of 1 to 117% of the crude feed. The average API specific gravity of each crude oil product is from 110 to 117% of the crude oil feed, and the viscosity of each crude oil product is at most 45% of the viscosity of the crude oil feed. Guan Fang is also an example ~~~~~~ —The catalyst for the pore size distribution of the crude oil feed with minimum hydrogen consumption and, in this case, mi is used in Examples 12 to 14, each reactor equipment (except for contact Except for the number and content of zones), each catalyst sulfide formation method, each total product separation method, and each crude oil product analysis system are the same as those described in Example 5. All catalysts are mixed with an equal volume of silicon carbide. Crude feed stream for each reactor 105 200533737 The drive train runs from the top of the reactor to the bottom of the reactor. The silicon carbide system is arranged at the bottom of each reaction behavior as a bottom carrier. Each reactor contains a contact zone. After the catalyst / silicon carbide mixture was placed in the contact zone of each reactor, the silicon carbide system was arranged above the top contact zone to fill the voids and serve as a preheating zone for each reactor. Each reactor was charged into a Lindberg furnace, which included three heating zones corresponding to a preheating zone, a contact zone, and a bottom carrier. The crude oil feed was contacted with each catalyst in the presence of hydrogen. The catalyst / silicon carbide mixture (40 cm3) was placed over the silicon carbide to form the contact area. The catalyst used in Example 12 is the vanadium catalyst prepared in Example 2. The catalyst used in Example 3 was the molybdenum catalyst prepared in Example 3. The catalyst used in Example 14 was the molybdenum / vanadium catalyst prepared in Example 4. The contact conditions of Examples 12 to 14 were as follows: the ratio of hydrogen to the crude oil feed to the reactor was 160 Nm3 / m3 (1000 SCFB), the LHSV was 1 h 1 ', and the pressure was 6.9 MPa (1014.7 psi). The contact zone was gradually heated to 343 t (65 ° F) over a period of time and maintained at 343 ° C for 120 hours' to achieve a total operating time of 36G hours. The total product leaves the contact zone and separates as described in Example 5. The net uptake of hydrogen by each catalyst system was measured during the contact period. In Example 12, the net absorption of 'hydrogen was] 0.7 Nm3 / m3 (_65 SCFB), and the crude product had a TAN of 6.75. In Example 13, the net absorption of hydrogen was in the range of 2.2 to 3.0 Nm3 / m3 (13.9 to 18.7 SCFB), and the crude product had a TAN in the range of 0.3 to 0.5. In Example 14, during the contact between the crude oil feed and the molybdenum / vanadium catalyst, the net hydrogen uptake was between -0.05 Nm3 / m3 to 106 200533737 〇6 NmVm3 (.〇.36 SCFB ^ 4 〇SCFB) having 0.2 to. TAN in the range of .5. From the point of view of the net absorption value of hydrogen during the contact period, it is estimated that between 1 gram of crude oil feed and vanadium contact during the catalyst contact period, 1G 7Nm3 / m3 (65scFB), hydrogen generation during the contact period and the conventional system. Today's production system, compared with the use of wind, can use less chlorine in the process to improve the properties of inferior crude oil. Less intermediate hydrogen would tend to reduce the cost of processing crude oil. In addition, the crude oil feed and the molybdenum / vanadium catalyst are produced separately from the indium catalyst. There are crude oil products with lower than TAN and TAN of the product. touch. The media is connected to each reactor equipment (except the number of contact zones and the 4 catalyst formation sulfide method, each total product separation method, and each crude product analysis system are the same as those described in Example 5. Unless otherwise Except for the explanation, all catalysts are mixed with carbonized rock in the volume ratio of j parts of carbonized rock to i parts of catalyst. The crude oil feed flow of each reactor is from the top of the reactor to the bottom of the reactor. The silicon system is disposed at the bottom of each reactor as a bottom carrier. Each reactor has a bottom contact area and a top contact area. After the catalyst / silicon carbide mixture is placed in the contact area of each reactor, the silicon carbide system is disposed at Above the top contact zone to fill the voids and as a preheating zone for each reactor. Each reactor is charged into a Lindberg furnace, which includes four heating zones corresponding to the preheat zone, two contact zones, and the bottom carrier. In each example, a vanadium catalyst was prepared as described in Example 2 and used with an additional catalyst. 107 200533737 In Example 15, the additional catalyst / silicon carbide mixture (45 cm3) was placed at bottom In the contact area, the additional catalyst is a flip catalyst prepared by the method described in Example 3. A vanadium catalyst / silicon carbide mixture (15 cm3) is disposed in the top contact area. In Example 16, the additional catalyst The catalyst / silicon carbide mixture (30 cm3) is disposed in the bottom contact area, and the additional catalyst is a flip catalyst prepared by the method described in Example 3. The vanadium catalyst / silicon carbide mixture (30 cm3) is It is arranged in the top contact area. In Example 17, an additional catalyst / silicon carbide mixture (3 () cm3) is arranged in the bottom contact area. The additional catalyst is the molybdenum / vanadium catalyst prepared in Example 4. The vanadium catalyst / silicon carbide mixture (3 () cm3) is disposed in the top contact area. In Example 18, Pyrex® (Glass Worcrk Corporation, New York, USA · ) Beads (30cm3) are arranged in each contact zone. The crude oil (Santos Basin, Brazil) having the properties summarized in Table 5, and Figure 17 used in Examples 15 to 18 is fed into the reaction. The top of the reactor. The crude oil feed flows through the preheating zone, top contact zone, bottom contact zone and bottom carrier of the reactor. Crude oil feed It is in contact with each catalyst in the presence of hydrogen. The contact conditions of each example are as follows: The ratio of hydrogen to the crude oil feed to the reactor was 160 Nm3 / m3 (100 SCFB) in the first 86 hours, During the remaining time limit is 80 Nm3 / m3 (500 SCFB), the LHSV is iy, and the pressure is 6.9 MPa (1014.7 psi). The contact zone is gradually heated to 343 ° C (650 () over a period of time and maintained at 343 under it to reach a total operating time of 14,000 hours. 108 200533737 These examples show that in the presence of a hydrogen source, the crude oil feedstock and the fifth column with a pore size distribution with a median pore size of 350 A. This is a general ^ Menganese catalyst with a median pore size of 250 i is the addition of the pore size distribution in the range A to produce crude oil, which has changed properties compared to the same properties of the crude oil feed, and the crude oil product has the same properties as its Wang Changxing crude oil feed from plant I. Only a few changes. In addition, the absorption of a relatively small amount of hydrogen from the crude oil feed was observed during the Zhigong: s-day door and — long period. Specifically, as shown in Table 5, Figure! As shown in Figure 7, the crude oil products of Examples 15 to 17 have a TAN of up to 4 15% of the crude oil feed. Compared with the same properties of the crude oil feed, the crude oil products produced in Examples 15--17 have a total Ni / V / Fe content of up to 44%, a maximum of 50% oxygen, and a maximum of 75% viscosity. In addition, the crude oil products produced in Examples 5 to 17 each have an API specific gravity of a crude oil feed having an API specific gravity of 100 to 103%. In comparison, the crude oil product produced under non-catalytic conditions (Example 18) compared with the viscosity and Aρι specific gravity of the crude oil feed produced a product with increased drillability and reduced API specific gravity. From the point of view of increasing viscosity and decreasing the specific gravity _, it can be concluded that coking and / or polymerization of the crude oil feed has been initiated. _ϋFeeding contact under preparation # LHS V. The contact system and the catalyst system are the same as those described in the sixth embodiment. The properties of the crude feed are shown in Table 6 in FIG. The contact conditions were as follows: the ratio of hydrogen to the crude oil feed to the reactor was 160 Nm3 / m3 (1000 SCFB), the pressure was 6.9 MPa (10i4.7pSi), and the temperature in the contact zone was 371 ° C (7 ° 〇F) to reach the total operating time. In Example 19, the LHSV during the contact was increased from 109 200533737 h'1 to 12 1Γ1 to 20.7 h · 1, from 1 hour during a period of time, and then the LHSV was allowed to be hours. 'Keep at 12 h · 1 48Keep at 20.7 h1% In Bei Shi Example 19, analyze the crude oil product to determine the Ding Dian, viscosity, density, and complete denier during the time period of LHSV of 12 γ and 20.7 h_i: Residue content, heteroatom content, and gold in the form of organic acid metal salts: Contains $. The average values of the properties of the crude oil products are shown in Table 6 and FIG. 18.

如表6 ’圖18所示’實施例19的原油產物與原油進 料的TAN和黏度相比具有降㈣TAN㈣低的黏度，而 原油產物的API比重為1〇4至11〇%之原油進料的A"比 重。MCR含量與C5瀝青質含量的重量比至少為1.5。MCR a里與C5瀝青質含量的和比原油進料之mcr含量與q瀝 青質含量的和減少。從MCR含量與cs瀝青質含量的重量 比及MCR含量與q瀝青質的和減少來看，可推斷是瀝青 質而不是具有形成焦炭傾向的成分會減少。原油產物也具 有鉀、鈉、辞和鈣的總含量最多為6〇%的原油進料之相同 金屬的總含量。原油產物的含硫量為80至90%之原油進 料的含硫量。 實施例6和1 9顯示可控制接觸條件以便與具有lhSV 為1 h·1的製程相比，使通過接觸區的LHSV大於1〇 h·1， 以生產具有類似性質的原油產物。在液體空間速度大於i 〇 h·1下選擇性改變原油進料性質的能力可容許接觸法在比市 售可得容器縮小尺寸的容器中進行。較小的容器尺寸可容 許劣質原油的處理在具有尺寸限制的生產場所（例如近海設 110 200533737 備）進行。 JL^L^~~在各種〇 接觸系統和觸媒係與實施例6所述者相同。將具有列 於圖19的表7之性質的原油進料加到反應器頂部，於氫 存在下與兩個接觸區中的兩種觸媒接觸以生產原油產物。 兩個接觸區係於不同溫度下操作。 頂部接觸區的接觸條件如下：LHSV為丨;頂部接 觸區的溫度為260 t; (500 τ);氫和原油進料的比率為 160 Nm /m3 (1〇〇〇 SCFB);及壓力為 6 9 Mpa psi)。 底部接觸區的接觸條件如下：LHSV為丨•，底部接 觸區的溫度為315 °C (_ T);氫和原油進料的比率為 16〇 Nm3/m3 (1〇〇〇 SCFB);及壓力為 6 9 ㈣（1〇14 7 ㈣。 〜產物離開底部接觸區並導入氣液相分離器。於氣液 才:離态中’將總產物分離成原油產物和氣體。原油產物 係疋期分析以測定TAN和C5瀝青質含量。 運轉期間所得到之原油產物性質的平均值列於表7, =19。原油進料具有9 3❸㈣及Q遞青質含量為每克 平油進料中有0.055克的C5瀝青質。原油產物具有〇.7的 ^ TAN & c5瀝青質的平均含量為每克原油產物中有 • 9克的C5瀝青質。原油產物的C5遞青質含量最多為μ 原油進料的c5瀝青質含量。 原油產物中鉀和納的總含量最多A 53%之原油進料中 料=二的總含量。原油產物的TAN最多* 10%之原油進 、 。在接觸期間係保持1 ·5或更高的p值。 111 200533737 如實施例6和20所示，具有低於第二（在此實例中為 底部）區之接觸溫度50 〇c的第一（在此實例中為頂部）接觸 溫度會傾向於使原油產物之Cs瀝青質含量比原油進料之 瀝青質含量更為降低。 此外，使用控制溫差會使有機酸金屬鹽形態的金屬含 量降低的更多。舉例而t，在每個實施例具有相當固定的 原油進料/總產物混合物之敎性（如p值所敎者）的情況As shown in Table 6 'shown in Figure 18', the crude oil product of Example 19 has a lower viscosity than the TAN and viscosity of the crude oil feed, and the crude oil product has an API specific gravity of 104 to 11% of the crude oil feed. A " Specific Gravity. The weight ratio of MCR content to C5 asphaltene content is at least 1.5. The sum of the MCR a and the C5 asphaltene content is lower than the sum of the mcr content and the q lutein content of the crude oil feed. From the weight ratio of the MCR content to the cs asphaltene content and the reduction of the sum of the MCR content and the q asphaltene, it can be inferred that it is the asphaltenes rather than the components with a tendency to form coke that will decrease. Crude oil products also have a total content of the same metals of a crude oil feed with a total potassium, sodium, hydrogen and calcium content of up to 60%. Crude products have a sulfur content of 80 to 90% of the sulfur content of the crude feed. Examples 6 and 19 show that the contact conditions can be controlled so that the LHSV through the contact zone is greater than 10 h · 1 compared to a process with lhSV of 1 h · 1 to produce crude products with similar properties. The ability to selectively change the properties of the crude oil feed at a liquid space velocity greater than i 0 h · 1 allows the contact method to be performed in a container that is smaller in size than a commercially available container. The smaller container size allows the processing of inferior crude oil to be carried out at production sites with size restrictions (eg offshore facilities 110 200533737). JL ^ L ^ ~~ The contact systems and catalyst systems are the same as those described in Example 6. A crude oil feed having the properties listed in Table 7 of Figure 19 was added to the top of the reactor and contacted with two catalysts in two contact zones in the presence of hydrogen to produce a crude oil product. The two contact zones operate at different temperatures. The contact conditions of the top contact zone are as follows: LHSV is 丨; the temperature of the top contact zone is 260 t; (500 τ); the ratio of hydrogen to crude oil feed is 160 Nm / m3 (1000 SCFB); and the pressure is 6 9 Mpa psi). The contact conditions in the bottom contact zone are as follows: LHSV is 丨 •, the temperature in the bottom contact zone is 315 ° C (_T); the ratio of hydrogen to crude oil feed is 160Nm3 / m3 (100SCFB); and pressure It is 6 9 ㈣ (1014 7 ㈣). ~ The product leaves the bottom contact area and is introduced into a gas-liquid separator. Only in the gas-liquid state: the total product is separated into crude oil products and gases. Crude oil products are in a periodical analysis To determine the TAN and C5 asphaltene content. The average value of the properties of the crude oil products obtained during the operation is shown in Table 7, = 19. The crude oil feed has a content of 9❸㈣ and the Q-degradation content is 0.055 per gram of flat oil feed. Grams of C5 asphaltenes. Crude oil products have an average content of ^ TAN & c5 asphaltenes of 9 grams of C5 asphaltenes per gram of crude oil products. C5 cyanide content of crude oil products is at most μ crude oil The c5 asphaltene content of the feed. The total content of potassium and sodium in the crude oil product is up to 53% of the crude feed. The total content of the crude oil feed = two. The TAN of the crude product is up to 10% of the crude oil feed. Maintain a p-value of 1.5 or higher. 111 200533737 As shown in Examples 6 and 20, has a low The contact temperature of the second (bottom in this example) zone is 50 ° C. The first (top in this example) contact temperature tends to make the Cs asphaltene content of the crude oil product more than the asphaltene content of the crude oil feed. In order to reduce. In addition, the use of a controlled temperature difference will reduce the metal content of the organic acid metal salt form. For example, t, in each embodiment, has a relatively fixed crude oil feed / total product mixture (such as p value The situation)

下實轭例之原油產物的鉀和鈉總含量降低比實施例6 之原油產物的鉀和鈉總含量降低的更多。 使用較低溫|的第-接觸區可容許移除高分子量化^ 物（例如C5il青質及/或有機酸金屬鹽），其會有形成聚合糸 或具有柔軟性及/或黏性的物理性質之化合物(例如膠及 或焦油）的傾向。於較低溫度下移除這些化合物可容許這藥 化t物在它們堵塞和被覆觸媒之前被移除，藉此增加配S 在第#觸區後面於較高溫度下操作的觸媒壽命。 ~體形式左_觸媒的接觸。The total potassium and sodium content of the crude product of the lower yoke example was reduced more than the total potassium and sodium content of the crude product of Example 6. The use of a lower-temperature first-contact zone allows the removal of high molecular weight compounds (such as C5il cyanide and / or organic acid metal salts), which have physical properties that form aggregates or have softness and / or stickiness Of compounds (such as gums and or tars). Removal of these compounds at lower temperatures may allow this medicinal substance to be removed before they plug and cover the catalyst, thereby increasing the catalyst life of the catalyst operating at higher temperatures after the #th contact zone. ~ Body form left_catalyst contact.

谁料2清案之塊狀金屬觸媒及/或觸媒沒100克的原括 進料中含0·〇〇〇 1 ? s古 克或0.02至4克的觸媒）於若干具靡 貫：可用原油進料使其懸浮並且於下列條件下反應：溫 度在85至42s公/ 至的範圍内 797 T)的範圍内，壓力在〇」Unexpectedly, the block metal catalyst and / or the catalyst in the cleared case did not contain 100 g of the original feed, which contained 0.0000 s s guc or 0.02 to 4 g of the catalyst). : It can be suspended by crude oil feed and reacted under the following conditions: the temperature is in the range of 85 to 42 s / to 797 T), and the pressure is 0 ″

NmVW達…±門及虱源和原油進料的比率為16至160( 後，原油產二 足以生產原油產物的反應時間之 ’、 係使用分離設備，如過濾器及/¾離< 觸媒及/或殘留的盾、丄、 汉/次離〜機，和 、原油進料分離。原油產物與原油進料相比 112 200533737 及降低的c5 可具有改變的TAN，鐵、錄，及/或鈒的含量 遞青質含量。 熟習該項技術者鑑於本說蚩 月曰應，、、、貝而易見本發明 種態樣的進一步修飾和替代 各 視為說明及用以達到教干孰 曰僅 逐』教不熟習該項技術者實施本發明 身又方法之目的。應瞭解本文中 _ 不又中所表不和敘述的本發明 態係作為具體實例的範例。可 " π π +又甲所圖不和敘述的 元件和材料，可顛倒本發明的部分和NmVW reaches… ± the ratio of the gate and lice source to the crude oil feed is 16 to 160 (after the reaction time of crude oil production is sufficient to produce crude oil products, the use of separation equipment such as filters and / ¾ ion < catalyst And / or residual shields, slugs, ions / times of separation, and crude oil feeds. Crude oil products compared to crude oil feeds 112 200533737 and reduced c5 may have altered TAN, iron, iron, and / or The content of tritium is the content of green matter. Those who are familiar with this technology, in view of the fact that this month should be described, further modification and substitution of various aspects of the present invention are considered as illustrations and used to achieve the teaching only. "Teach one by one" who is not familiar with the technology to implement the method of the present invention. It should be understood that the state of the present invention, which is shown and described in this article, is used as an example of a specific example. Quotable Elements and materials that are not illustrated or described may reverse some aspects of the present invention and

發明的某些特徵，以上全部在了早獨使用本 / 上王邛在獲致本發明說明書的效益之 後，應為熟習該項技術者所顯而易見。可進行本文中所述 之元件的改變而不致脫離如後附申請專利範圍所述之本發 明的精神與範疇。 义 【圖式簡單說明】 圖式簡單說明 對於热習該項技術者而言，本發明具有下列詳細說明 之效益的優點在參照附圖後將變得顯而易見，其中： 圖1為接觸系統之具體實例的簡圖。 圖2Α和2Β為包含兩個接觸區的接觸系統之具體實例 的簡圖。 圖3 Α和3Β為包含三個接觸區的接觸系統之具體實例 的簡圖。 圖4為結合接觸系統的分離區之具體實例的簡圖。 圖5為結合接觸系統的摻合區之具體實例的簡圖。 圖6為結合分離區、接觸系統和摻合區之具體實例的 113 200533737Some of the features of the invention are all obvious to those skilled in the art after using the book alone / Shang Wangyi after obtaining the benefits of the description of the invention. Changes may be made in the elements described herein without departing from the spirit and scope of the invention as described in the appended patent claims. [Simplified illustration of the diagram] For those skilled in the art, the advantages of the present invention with the following detailed description will become apparent after referring to the drawings, where: Figure 1 is the specific of the contact system Simplified illustration of the example. Figures 2A and 2B are schematic diagrams of a specific example of a contact system including two contact areas. 3A and 3B are schematic diagrams of a specific example of a contact system including three contact areas. Fig. 4 is a schematic diagram of a specific example of a separation zone incorporating a contact system. Fig. 5 is a schematic diagram of a specific example of a blending zone of a contact system. Figure 6 is a specific example of the combined separation zone, contact system and blending zone. 113 200533737

圖7為使原油進料盥二鍤 it 41 ^ . . ^ 一種觸媒接觸的具體實例之原油 進枓與原油產物的代表性質列表。 圖8為使原油進料盘一 ^ d^k irm ,τ ^ 次夕種觸媒接觸的具體實例之 加核平均床溫度對運轉時間的圖示。 】之 圖9為使原油進料血雨插_ ^ ^ 兩種觸媒接觸的具體實例之原油 進枓與原油產物的代表性質列表。 圖10為使原油進料盘雨 . 一兩種觸媒接觸之具體實例的原油Fig. 7 is a list of representative properties of crude oil feed and crude oil products for a specific example of contacting a crude oil feed it 41 ^.. ^ With a catalyst. Fig. 8 is a graph showing a specific example of contacting a crude oil feed tray with ^ d ^ k irm, τ ^ next night catalyst, and the average bed temperature versus operating time. Figure 9 is a list of representative properties of crude oil feeds and crude oil products for specific examples of contacting two types of catalysts with crude oil feeds. Figure 10 is the crude oil feed tray rain. One or two specific examples of contact with crude oil

枓〃原油產物之代表性質的另一個列表。 圖11為使原油進料盘錄 如 /、四種不同觸媒系統接觸的具體實 例之原油進料與原油產物的列表。 “圖12為使原油進料與四種不同觸媒系統接觸之具體實 歹的原油產物之P值對運轉時間的圖示。 圖13為使原油進料與四種不同觸媒系統接觸之具體實 歹1的原油進料之氫的淨吸取對運轉時間的圖示。 圖14為使原油進料與四種不同觸媒系統接觸的具體實列表 Another list of representative properties of crude oil products. Figure 11 is a list of crude oil feeds and crude oil products for specific examples of contacting the crude oil feed pan with four different catalyst systems. "Figure 12 is a graphical representation of the p-value of crude oil products versus operating time for contacting the crude feed with four different catalyst systems. Figure 13 is the specific contact for the crude feed with four different catalyst systems Figure 1 shows the net absorption of hydrogen from the crude oil feed to operating time. Figure 14 is a specific example of contacting the crude feed with four different catalyst systems.

之以重ϊ百分率表示的原油產物之殘留物含量對運轉 間的圖示。 圖15為使原油進料與四種不同觸媒系統接觸之具體實 歹，的原油產物之API比重改變對運轉時間的圖示。 例圖16為使原油進料與四種不同觸媒系統接觸的具體實 之以重ΐ百分率表示的原油產物之含氧量對運轉時間的 圖17為使原油進料與觸媒系統接觸的具體實例之原油 114 200533737 進料與原油產物的代表性質列表，該觸媒系統包含各種量 的翻觸媒和銳觸媒，與包含叙觸媒和銷/媒的觸媒系 統’以及玻璃珠。 圖18為在各種液體空間速度下使原油 戒多種 觸媒接觸的且濟眚γ " /、體實例之原油進料與原油產物的性質列表。 圖19為在各種接觸溫度下使原油進料進行接觸的具體 實例之原油進料與原油產物的性質列表。A graphical representation of the residual content of crude oil products as a percentage of weight versus operating room. Fig. 15 is a graph showing the change in the API specific gravity of the crude oil product versus operating time for a specific example of contacting the crude oil feed with four different catalyst systems. Example Figure 16 is the specific contact of crude oil feed with four different catalyst systems. The oxygen content of crude oil products expressed as weight percent versus operating time. Figure 17 is the specific contact of crude oil feed with catalyst system. Examples of crude oil 114 200533737 The feedstock and the list of representative properties of crude oil products. The catalyst system includes various amounts of flip catalyst and sharp catalyst, and catalyst systems including catalysts and pins / catalysts, and glass beads. Figure 18 is a list of properties of crude oil feeds and crude oil products that contact crude oils or various catalysts at various liquid space velocities and which are used in the " " example. Figure 19 is a list of properties of crude oil feeds and crude oil products for specific examples of contacting crude oil feeds at various contact temperatures.

* I官本發明容許各種修飾與替代形式，但謂定具體 只例係藉由圖示中的眚也丨主- μ ’ 制。^ r的實例表不。該等圖示可能未按比例繪 、 應瞭解其圖示和詳细％明计m + ^ ,. 、、、Π 並非用來將本發明限制在所 蜃不的特定形式，但相反地， m M r p, ^ w圖涵盍落入如後附申請 寻利乾圍所限定之精神盥鉻裱 代物。 揹砷與靶可内的所有修飾、等效物和替* The present invention allows various modifications and alternative forms, but it is presumed that the specific examples are made by the 眚 也 丨 主 -μ 'system in the illustration. ^ R's example shows. These illustrations may not be drawn to scale. It should be understood that their illustrations and details are clear. M + ^,.,,, Π are not intended to limit the invention to the particular form in which it is described, but instead, m M rp, ^ w Figure Han Han falls into the mental chrome frame as defined in the attached application for seeking profit Qianwei. All arsenic and all modifications, equivalents and substitutions within the target

【主要元件符號說明】 1〇〇:接觸系統 102 :接觸區 104 :導管 106 ;導管 106’ ：導管 1〇8 :分離區 110 :導管 112 :導管 114 :接觸區 1 1 6 :接觸區 115 200533737 118 :導管 120 :分離區 122 :導管 124 :導管 126 :導管 128 :導管 130 :摻合區 132 :導管 134 :導管 136 :加權平均床溫度（WABT)對運轉時間的曲線 140-146 :原油產物之P值對運轉時間的曲線 148-154:氫的淨吸取對運轉時間之曲線 15 6-162 :原油產物之殘留物含量對運轉時間之曲線 164-170 :原油產物之API比重對運轉時間之曲線 172-178 :原油產物之含氧量對運轉時間之曲線[Description of main component symbols] 100: contact system 102: contact area 104: conduit 106; conduit 106 ': conduit 108: separation area 110: conduit 112: conduit 114: contact area 1 16: contact area 115 200533737 118: Duct 120: Separation Zone 122: Duct 124: Duct 126: Duct 128: Duct 130: Blend Zone 132: Duct 134: Duct 136: Curve of Weighted Average Bed Temperature (WABT) vs. Run Time 140-146: Crude Oil Product P-value vs. operating time curve 148-154: Net absorption of hydrogen vs. operating time curve 15 6-162: Residual content of crude oil product vs. operating time curve 164-170: API gravity of crude oil product versus operating time Curves 172-178: Oxygen content of crude oil products versus operating time

Claims (1)

200533737 十、申請專利範圍： -種生產原油產物之方法，其包括： =原油進料與_或多種觸媒接觸以生產含有原 的總產物，其中該％、、山# ^ % &曰人 ，、，產物在25 °C和0.101 MPa下為液 悲：“勿，該原油進料包含一或多種有機酸的一或多種驗 至息 或夕種有機酸的鹼土金屬鹽，或其混合物，該200533737 10. Scope of patent application:-A method for producing crude oil products, which includes: = crude oil feed is contacted with _ or multiple catalysts to produce a total product containing the original, where the% ,, mountain The product is liquid at 25 ° C and 0.101 MPa: "Do n’t, this crude oil feed contains one or more organic acids or one or more organic acid alkaline earth metal salts, or mixtures thereof, The 原油進料在母克原油進料中具有至少請⑼丨克之有機酸 金屬鹽形態的驗金屬和驗土金屬總含量，該至少一種觸媒 具有中位孔徑至少# 23G A的孔徑分佈，其藉由ASTM法 D4282測又，該觸媒具有包含週期表第6欄的一或多種金 屬週』表第6攔之一或多種金屬的一或多種化合物，或 其混合物的孔徑分佈；及 拴制接觸條件以便使該原油產物具有有機酸金屬鹽形 悲的鹼金屬和鹼土金屬總含量最多為9〇%之該原油進料中 有私:¾金屬鹽形態的鹼金屬和鹼土金屬含量，其中有機酸 金屬鹽形態的鹼金屬和鹼土金屬含量係藉由ASTM法 D 1 3 1 8測定。The crude oil feed has a total metal test and soil test metal content in the form of an organic acid metal salt in the mother gram crude feed. The at least one catalyst has a pore size distribution with a median pore size of at least # 23G A. As measured by ASTM method D4282, the catalyst has a pore size distribution of one or more compounds containing one or more metals in column 6 of Table 6 of the Periodic Table, or a mixture thereof; and tethered contacts Conditions so that the crude oil product has organic acid metal salts in the form of alkali metals and alkaline earth metals with a total content of up to 90%. The crude oil feed has private: ¾ metal salts in the form of alkali metals and alkaline earth metals, of which organic acids The content of alkali metals and alkaline earth metals in the form of metal salts is measured by ASTM method D 1 3 1 8. 2·如申請專利範圍第1項之方法，其中該原油產物中 有機酸金屬鹽形態的驗金屬和驗土金屬總含量最多為 5〇%，最多為1〇%，或最多為5%之該原油進料中有機酸金 屬鹽形態的鹼金屬和鹼土金屬含量。 3.如申請專利範圍第1項之方法，其中該原油產物中 有機酸金屬鹽形態的鹼金屬和鹼土金屬總含量在1至 80%，10至70%，2〇至6〇%，或3〇至5〇%之該原油進料 117 200533737 中有機酸金屬鹽形態的驗金屬和驗土金屬含量之範圍内。 4·如申請專利範圍第1至3項中任一項之方法，其中 。亥原油產物在每克原油產物中含有〇·〇〇〇⑼〇 1克至〇 00005 克，0.0000003 克至 0.00002 克，或 O.OOOOOi 克至 〇 〇〇〇〇1 克之有機酸金屬鹽形態的鹼金屬和鹼土金屬。 5·如申請專利範圍第丨至4項中任一項之方法，其中 —或多種第6欄的金屬為鉬及/或鎢。2. The method according to item 1 of the scope of patent application, wherein the total content of the metal test and soil test metal in the form of the metal salt of the organic acid in the crude oil product is at most 50%, at most 10%, or at most 5%. Alkali and alkaline earth metal content in the form of metal salts of organic acids in crude oil feeds. 3. The method of claim 1, wherein the total content of alkali metals and alkaline earth metals in the form of metal salts of organic acids in the crude oil product is 1 to 80%, 10 to 70%, 20 to 60%, or 3 0 to 50% of the crude metal feed 117 200533737 in the range of metal and metal content of organic acid metal salt. 4. The method according to any one of claims 1 to 3, in which. The crude oil product contains 0.00000 g to 0.0005 g, 0.000000 g to 0.00002 g, or 10,000 g to 10,000 g of the base in the form of an organic acid metal salt per gram of crude oil product. Metals and alkaline earth metals. 5. The method according to any one of claims 1-4, wherein-or more of the metals in column 6 are molybdenum and / or tungsten. 6·如申請專利範圍第1至5項中任一項之方法，其中 该孔徑分佈的中位孔徑最多為500 A。 7.如申請專利範圍第1至6項中任一項之方法，其q 该觸媒具有另外包含週期表第5欄的一或多種金屬，一 ^ 夕種第5攔金屬的一或多種化合物，週期表第7至1 〇相 的-或多種金屬，-或多種帛7至1〇搁金屬的一或多毛 化合物’及/或其混合物的孔徑分佈。 ^ 8·如申請專利範圍第1至7項中任一項之方法，其亏6. The method according to any one of claims 1 to 5, wherein the median pore size of the pore size distribution is at most 500 A. 7. The method according to any one of claims 1 to 6, wherein the catalyst has one or more compounds additionally containing one or more metals in column 5 of the periodic table, and one or more compounds of the fifth metal. The pore size distribution of one or more hairy compounds of phase 7 to 10 of the periodic table, or one or more hairy compounds of metal 7 to 10, and / or mixtures thereof. ^ 8. If the method of any of the items 1 to 7 of the scope of patent application, its disadvantages :觸，具有另外包含週期表帛15攔的__或多種元素及^ 或多種第15欄元素的一或多種化合物的孔徑分佈。 如申請專利範圍第i纟8項中任一項之：法，其， 二或多種觸媒另外包含附加觸媒，該附加觸媒具有" 搜至少為6〇 A或至少為180 A的孔徑分佈。 10.如申請專利範圍第9項之方法，其 油谁％L⑼rr 得觸包括在眉 附加觸媒接觸之後使該原油 至少Α X < Tt ”具有中位孔控 馬230 A的觸媒接觸。 1 1 ·如申睛專利範圍第1至1 〇項中— 只τ仕項之方法，其 118 200533737 中使遠原油進料在位於或連接到近海設備的接觸區中一 接觸。 仃 12·如申請專利範圍第1至11項令任一項之方法， 中接觸包括於氫源存在下進行接觸。 '其 13.如申請專利範圍第〗至12項中任一項之方法，其 中：方法尚包括使該原油產物與該原油進料相同或不同的 原油結合以形成摻合物。 的 14·種原油產物或摻合物，其可 15 ! , J糟由申請專利範圍第 至1 3項中任一項之方法獲得。 U·—種生產運輸用燃料、加 ^ 品之方法，i勺紅a ^ I科、潤滑油或化學 或摻合物。 14項之原油產物 I6·如申請專利範圍第15項之方 # m >'4, 决’其中該加工包括 一 > 4勿或摻合物蒸餾成為一或多種餾分。 Π·如申請專利範圍第15或16 包括加氫處理。 万法，其中忒加工: Touch, the pore size distribution of one or more compounds that additionally contain __ or more elements and ^ or more of the 15th column element of the periodic table. For example, any one of item i 范围 8 of the scope of patent application: method, in which two or more catalysts additionally include an additional catalyst, the additional catalyst has a pore size of at least 60A or at least 180A distributed. 10. The method according to item 9 of the scope of patent application, whose oil contact may include contacting the catalyst with at least A X < Tt '' having a median pore control horse 230 A after the additional contact with the catalyst. 1 1 · As described in Shen Jing patent scope Nos. 1 to 10-only τ Shi's method, 118 200533737 makes Yuan crude oil feed contact in a contact zone located or connected to offshore equipment. 仃 12 · 如The method of applying any one of items 1 to 11 of the scope of patent application, wherein the contact includes contacting in the presence of a hydrogen source. 'It 13. The method of any one of the one or 12 items of scope of patent application, wherein: the method is still Including 14 types of crude oil products or blends that combine the crude oil product with the same or different crude oil feeds to form a blend, which can be 15! Obtained by any one of the methods. U · —A method of producing transportation fuels and additives, i spoon of red oil, lubricants or chemicals or blends. 14 crude oil products I6. Item 15 of the party # m > '4, decided' which processing Comprising a > 4 or not to be a blend of one or more fractions by distillation Π · Patent application range as 15 or 16 comprising hydrotreating methodology, wherein te processing. 十一、圖式： 如次頁 119XI. Schematic: as next page 119
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