TW200535224A - 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
TW200535224A
TW200535224A TW093139055A TW93139055A TW200535224A TW 200535224 A TW200535224 A TW 200535224A TW 093139055 A TW093139055 A TW 093139055A TW 93139055 A TW93139055 A TW 93139055A TW 200535224 A TW200535224 A TW 200535224A
Authority
TW
Taiwan
Prior art keywords
crude oil
catalyst
product
crude
feed
Prior art date
Application number
TW093139055A
Other languages
Chinese (zh)
Other versions
TWI440707B (en
Inventor
Opinder Kishan Bhan
Scott Lee Wellington
Original Assignee
Shell Int Research
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Publication date
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Application filed by Shell Int Research filed Critical Shell Int Research
Publication of TW200535224A publication Critical patent/TW200535224A/en
Application granted granted Critical
Publication of TWI440707B publication Critical patent/TWI440707B/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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Manufacture Of Alloys Or Alloy Compounds (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 25 DEG C and 0.101 Mpa. One or more other properties of the crude product may be changed by at least 10% relative to the respective properties of the crude feed.

Description

200535224 九、發明說明： 【發明所屬之技術領域】 本毛月大體上係有關處理原油進料之系統、方法和觸 媒並且有關能使用這類系統、方法和觸媒生產的組成物。 更存3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，纟中此總產物含 有原油產物’其在25°c和〇1〇1 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】 具有無法容許原油經濟地輸送，或使用習知設備加工 的一或多種不適當性質之原油通常稱為“劣質原油”。 劣質原油可能包含造成原油進料之總酸值（“tan”）的 酉欠性成分。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蝕。移除劣 質原油中的酸性成分可能涉及用各種鹼化學中和酸性成 分。或者，耐蝕金屬可用於輸送設備及/或加工設備中。使 用耐餘金屬通常涉及可觀的費用，因此在現行設備中使用 财餘金屬可能不是吾人所期望的。抑制腐蝕的另一種方法 可能涉及在輸送及/或加工劣質原油之前將腐蝕抑制劑添加 到劣質原油。使用腐蝕抑制劑可能對加工原油所用的設備 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。這類大量殘留 物會有使用習知設備難以輸送及/或加工和成本昂貴的傾 200535224 "劣質原油通常包含有機結合的雜原子（例如硫、氧，和 有機結合的雜原子於^干情況下對觸媒有不利的影 曰 劣質原油可能包含相當大量的金屬污染物，例如錄、 或鐵。在加工這類原油期間，金屬污染物及/或金 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。 在觸2工劣質原油期間焦炭可能會急劇地形成及/或沈積 …面上。使受到焦炭污染的觸媒之催化活性再生的 昂貴的。再生期間所❹的高溫也可能使觸媒 勺活性降低及/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、 士甲二及/或鈉）。有機酸金屬鹽形態的金屬典型而言無法藉 習知方法，例如脫鹽及/或酸洗從劣質原油中分離。曰 當存在有機酸金屬鹽形態的金屬日夺，習知方法常遇到 機:與典型沈積在觸媒之外表面附近的銻和鈒相比，有 隙鹽形態的金屬可能會優先沈積在觸媒粒子間的孔 金屬=能Γ是在觸媒床的頂部。污染⑯，例如有機酸 的金屬沈積在觸媒床頂部通常會導致通過觸媒 、墾降增加而且實際上會堵塞該觸 ’、 、，屬:形恶的金屬可能會導致觸媒的快速減活性。 每克！油可能包含有機氧化合物。加工具有含氧量為 :貝原油中至少含0.002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 200535224 受熱時可能會生成高級氧化物（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。 劣質原油可能包含不飽和烴。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氫 化觸媒的使用，可能需要抑制不飽和片段形成焦炭。氳的 生產成本昂貴及/或輸送到處理設備成本昂貴。 劣質原油在以習知設備加工期間也會傾向於表現出不 穩定性。原油不敎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0 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t，習知； 法通吊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 若干用以改善；^油口；^ μ +， ^ 、 京由口口貝的方法包括將稀釋劑添加至劣 質原油以降低造成不利性皙 人卜〜『王負之成分的重量百分率。然而， 添加稀釋劑通常會因為稀釋 禅μ的成本及/或加工劣質原油增 加的成本而增加處理劣皙历 π、 貝原，由的成本。稀釋劑添加至劣質 原油於若干情況下可能合隊彳 、 曰降低此種原油的穩定性。 頒予Sudhakar等人的蓋阳由 的美國專利案號6,547,957 ;頒予 200535224 ΓΓΙ!Γ !：277,269; ^ 、 ⑶ * 人 ^ 5,928,5G2 ;頒 ^ Beanlen 等人 5,914,030 ;頒予丁raclUe 望 χ a ^ 哥人的 算人的5⑺^ ，897,769;頒予丁純e 寻人的5,871，636 ;及頒予Tanaka ic 〇 加工原油的各種方法、李统及觸禅：5,851，381係敘述 種万凌纟統及觸媒。然而，這些專利 =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。 間&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)。其他非理想性質包括相當大量的非 理想成分（例如殘留物、有機結合雜原子、金屬污染物、有 機酉夂金屬鹽形態之金屬，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 处里期間腐蝕增加，觸媒壽命減短，製程堵塞，及/或氫使 用曰加因此，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 "、有選擇性改變劣質原油之其他性質的系統、方法，及/或 觸媒也有顯著經濟上和技術上的需求。 【發明内容】 本發明大體上係有關用以將原油進料轉化成含有原油 產物而在若干具體實例中含有非可凝氣體的總產物之系 、充方法和觸媒。本發明大體上亦有關含有其中成分之新 賴組合的組成物。這類組成物能使用本文中所述的系統和 200535224 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，該至少一種觸媒具有中位 孔控至少為90A的孔徑分佈，其藉由ASTM法D4282測定， "亥觸媒在母克觸媒中，以鉬的重量計，含有〇 〇〇〇ι克至0.08 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ΤΑΝ最多為9〇%之該原油進料的 TAN，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25t和〇·1()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 〇664測定， 孩至》一種觸媒具有中位孔徑至少為工8〇人的孔徑分佈， 200535224 其藉由ASTM法D4282測定，兮讎上甘曰士 a人 只J疋忒觸媒具有包含週期表 爛的-或多種金屬，週期表第6搁之一或多種金屬的 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& 9〇%之該原油 TAN，其中TAN係藉由ASTM法如以測定。 、 本發明亦提供生產原油產物之方法，其包括： =與-或多種觸媒接觸以生產含有原油產物的總產物： /、中該原油產物在饥和0.101 Mpa下為液態混合物，兮 ^由進料具有至少0.3的TAN,其藉由^頂法_測 疋’該至少一種觸媒包含：⑷週期表第6欄的一或多種 週期表帛6攔之一或多種金屬的一或多種化合物， 或』合物…b)週期表第1〇欄的一或多種金 =表第10攔之一或多種金屬的一或多種化合物，或其混 物其中第10欄金屬總量與第6攔金屬總量的莫耳比 且有1二二的範圍内；及控制接觸條件以便使該原油產物 =广敢多為90%之該原油進料的⑽，其中UN係 糟由ASTM法D664測定。 :發明亦提供生產原油產物之方法，纟包括：使原油 二;：多種觸媒接觸以生產含有原油產物的總產物， /、中4原油產物在25它和〇1〇1 Μ 原油進料且右S丨 下為液恶混合物，該 -種觸Γ、Γ ΤΑΝ，該一或多種觸媒包含··⑷第 有000 於每克第一種觸媒中，以金屬重量計，含 期表第广·06克之週期表第6攔的-或多種金屬，週 又 ㈣之—或多種金屬的-或多種化合物，或其混合 200535224 物’及（b)弟二種觸媒’該第二種觸媒在每克第二種觸媒 中，以金屬重量計，含有至少〇.〇2 ^ 七少必；八Μ 週/月表弟6欄的一 或夕種金屬，週期表第6攔之-或多種金屬的-或多種化 合物，或其混合物；及控制接觸條件以便使該原油產物呈 有TAN最多為90%之該原油進料的τΑΝ，其中μ夢 由ASTM法D664測定。 ’、200535224 IX. Description of the invention: [Technical field to which the invention belongs] This gross month 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. More specifically, the specific examples described herein relate to systems, systems, methods, and catalysts used to convert crude oil feeds into total products, where the total product contains crude oil products' It is a liquid mixture at 001 MPa and has one or more changed properties compared to the individual properties of the crude feed. [Prior Art] Crude oil with one or more inappropriate properties that cannot allow crude oil to be economically transported or processed using conventional equipment is often referred to as "inferior crude oil." Poor crude oil may contain owing components that contribute to the total acid number ("tan") of the crude feed. Poor crude oil with a fairly high TAN may cause corrosion of metal components during transportation and / or processing of this poor crude oil. Removal of acidic components from inferior crudes may involve neutralizing the acidic components with various alkali chemistry. Alternatively, corrosion resistant metals can be used in conveying equipment and / or processing equipment. The use of residual metals usually involves considerable costs, so using surplus metals in existing equipment may not be what we would expect. Another method of inhibiting corrosion may involve adding corrosion inhibitors to the inferior crude before transporting and / or processing the inferior crude. The use of corrosion inhibitors may negatively affect the quality of equipment used to process crude oil and / or products made from crude oil. Poor crude oil usually contains a considerable amount of residue. Such large amounts of residues can be difficult to transport and / or process using conventional equipment and are costly. 200535224 " Inferior crude oil often contains organically bound heteroatoms (such as sulfur, oxygen, and organically bound heteroatoms in dry conditions). The adverse effects of the catalyst below are that inferior crude oil may contain a considerable amount of metal contaminants, such as iron, or iron. During the processing of such crude oil, metal contaminants and / or gold compounds may be deposited on the catalyst surface Or the pore volume of the catalyst. Such deposits may cause a decrease in catalyst activity. During the contact with inferior crude oil, coke may form and / or deposit sharply on the surface. Catalytically active regeneration is expensive. The high temperatures encountered during regeneration may also reduce catalyst activity and / or cause catalyst degradation. Inferior crude oils may contain metals in the form of metal salts of organic acids (e.g., calcium, methyl formaldehyde, and / or Sodium). Metals in the form of metal salts of organic acids typically cannot be separated from inferior crude oil by conventional methods such as desalination and / or pickling. When organics are present Metals in the form of metal salts are often encountered in conventional methods: Compared with antimony and plutonium, which are typically deposited near the outer surface of the catalyst, metal in the form of gap salts may preferentially deposit in the pores between the catalyst particles Metal = energy Γ is on the top of the catalyst bed. Pollutants, such as the deposition of metals from organic acids on the top of the catalyst bed, will usually result in increased catalyst and land reclamation and will actually block the catalyst. Evil metals may cause rapid deactivation of the catalyst. Per gram! The oil may contain organic oxygen compounds. Processing of inferior crude oil with oxygen content of at least 0.002 grams of oxygen in shell crude oil may occur during the construction period. Encountered a problem. Organic oxygen compounds may generate advanced oxides (such as ketones and / or alcohols from the oxidation of alcohols' and / or ethers from the oxidation of organic acids) when heated during processing 200535224, which is difficult to process from processed crude oil. Removal and / or may corrode / contaminate equipment during processing and cause blockage of pipelines. Inferior crude oil may contain unsaturated hydrocarbons. When processing unsaturated hydrocarbons, especially if Unsaturated fragments from the solution usually require an increase in the average amount of hydrogen. Hydrogenation during processing, which typically involves the use of active hydrogenation catalysts, may require the suppression of unsaturated fragments to form coke. The production cost of tritium is expensive and / Or it is expensive to transport to processing equipment. Inferior crude oils also tend to show instability during processing with conventional equipment. Crude oil instability can cause component phase separation and / or generation of non-ideal by-products during processing (such as Hydrogen sulfide, water, and carbon dioxide) Tendency 0 Conventional methods often lack the ability to change selected properties of inferior crude oils without significantly altering other properties of inferior crude oils. For example, t, the conventional method lacks a significant reduction in inferiority. Tan in crude oil, while only changing the content of specific components (such as sulfur or metal pollutants) in inferior crude oil by a desired amount at the same time to improve; ^ oil mouth; ^ μ +, ^, Jingyou mouth shellfish methods include Diluents are added to inferior crude oils to reduce the weight percentage of the ingredients that cause disadvantages. However, the addition of diluent usually increases the cost of processing inferior calendar π and shellfish because of the cost of diluting the μμ and / or the increased cost of processing inferior crude oil. The addition of diluents to inferior crude oils may in some cases reduce the stability of such crude oils. U.S. Patent No. 6,547,957 to Gai Yangyou to Sudhakar et al .; to 200535224 ΓΓΙ! Γ !: 277,269; ^, ⑶ * person ^ 5,928,5G2; ^ Beanlen et al. 5,914,030; to Ding raclUe Hope χ a ^ 5⑺ of my brother's ^^, 897,769; 5,871,636 awarded to Ding Chune for tracing; and Tanaka ic 〇 Various methods for processing crude oil, Li Tong and Touch Zen: 5,851,381 are narrative species Wanling System and catalyst. However, the methods, systems, and catalysts of these patents have limited applicability due to the many technical issues raised above. Inferior ' 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-ideal properties include considerable amounts of non-ideal ingredients (such as residues, organically bound heteroatoms, metal contaminants, metals in the form of organic metal salts, and / or organic oxygen compounds). Such properties tend to cause problems with conventional conveying and / or processing equipment, including increased corrosion during transit, reduced catalyst life, process blockages, and / or increased hydrogen use. Therefore, for the conversion of inferior crude oil There are still significant economic and technical needs for improved systems, methods, and / or catalysts to form crude oil products with more desirable properties. There is also a significant economic and technical need for systems, methods, and / or catalysts that can change the selected properties of inferior crude oil, and selectively change other properties of inferior crude oil. [Summary of the Invention] The present invention relates generally to a system, a charging method, and a catalyst for converting a crude oil feed into a total product containing a crude oil product and, in some specific examples, a non-condensable gas. The present invention also generally relates to compositions containing novel combinations of the ingredients therein. Such compositions can be obtained using the system and 200535224 method described herein. The present 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 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 ranging from 90 A to 180 people, and at least 60% of the total pore size in the pore size distribution has 45 people 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 ASTM Assay 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 liquid mixture at 0 · 101 MPa, 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 control of at least 90A, which is determined by ASTM method D4282, & quot Hai catalyst in the mother gram catalyst, based on the weight of molybdenum, contains 0.00000 grams to 0.08 grams of molybdenum, one or more molybdenum compounds, or mixtures thereof; and control the contact conditions so that the crude oil product has The TAN is at most 90% of the TAN of the crude oil feed, wherein the TAN is determined by aSTM method d664. The present invention also provides a method for producing a crude oil product, comprising: contacting the crude oil feed with one or more catalysts to produce Total product containing crude oil products, wherein the crude oil product is a liquid mixture at 25t and 〇1 () 1 MPa, the crude oil feed has a TAN of at least 0.3, which is determined by ASTM 0664, a kind of The catalyst has a pore size distribution with a median pore size of at least 80 workers. 200535224 It was determined by ASTM method D4282. Xishang Shanggan Shishi A. J. The catalyst has a periodic table-or multiple metals. One or more metals of the sixth table of the periodic table Pore size distribution of various compounds, or mixtures thereof; and controlling the contact conditions so that the crude oil product has the maximum TAN of & 90% of the crude oil TAN, where TAN is determined by ASTM method, etc. The invention also provides production A method of crude oil products, comprising: = contacting with-or a plurality of catalysts to produce a total product containing crude oil products: /, the crude oil product is a liquid mixture under the condition of 0.101 Mpa, and the feedstock has a content of at least 0.3 TAN, by which method at least one catalyst includes: ⑷ one or more of the periodic table 栏 column 6 of the periodic table 帛 one or more compounds of one or more metals, or a compound ... b) One or more gold in column 10 of the periodic table = one or more compounds of one or more metals in the tenth column of the table, or a mixture thereof. And within a range of 1 to 2; and control the contact conditions so that the crude oil product = 90% of the crude oil feedstock, the UN system is determined by ASTM method D664. : The invention also provides a method for producing crude oil products, including: contacting crude oil two ;: contacting various catalysts to produce a total product containing crude oil products; The bottom right is a liquid-evil mixture. The one kind of catalyst Γ, Γ ΤΑΝ, the one or more catalysts include the first 000 in each gram of the first catalyst, based on the weight of the metal. Cantonese-06 grams of Periodic Table 6-or more metals, and Zhou Jiuzhi-or more metals-or more compounds, or a mixture of 200535224 and 'b) two catalysts' the second catalyst The medium in the second catalyst per gram, based on the weight of the metal, contains at least 0.002 ^ Qi Shao Bi; 8 M week / month cousin of one or the evening metal in column 6, block 6 of the periodic table- Or more metals or compounds, or mixtures thereof; and controlling the contact conditions so that the crude oil product exhibits τAN of the crude oil feed with a TAN of up to 90%, wherein μ dream is determined by ASTM method D664. ’,

本發明亦提供觸媒組成物，其包括：⑷週期表第5 欄的-或多種金屬，週期表第5搁之一或多種金屬的—或 多種化合物’或其混合物；(b)載體，其具有㊀氧化鋁含 =每克載體中至少（M克的㊀氧化紹，其藉由χ射線繞射測 定，其中該觸媒具有中位孔徑至少$ 23〇Α的孔徑分佈， 其藉由ASTM法D4282測定。The present invention also provides a catalyst composition comprising: (i) the metal of the periodic table in column 5 or more, one or more metals in the periodic table of 5 or more compounds, or a mixture thereof; (b) a carrier, which It has alumina oxide content of at least (Mg of alumina oxide per gram of carrier, which is determined by X-ray diffraction, wherein the catalyst has a pore size distribution with a median pore size of at least $ 23〇Α, which is determined by the ASTM method. D4282 determination.

本發明亦提供觸媒組成物，其包括：⑷週期表第6 ^的-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；⑻載體，其具有Θ氧化鋁含量 =母克載體中至少（U克的θ氧化銘，其藉由χ射線繞射測 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。 本毛明亦提供觸媒組成物，其包括··（a)週期表第5 =的一或多種金屬，週期表第5欄之一或多種金屬的一或 夕種化s物，週期表第6欄的一或多種金屬，週期表第6 攔之或多種金屬的一或多種化合物，或其混合物；（b)載 體八具有㊀氧化鋁含量為每克載體中至少〇·ι克的θ氧化 鋁，其藉由X射線繞射測定；其中該觸媒具有中位孔徑至 11 200535224 少為23GA的孔徑分佈，其藉由aSt^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…，而一或多種金屬包括週期表第5欄的一或多種 金屬、，週期表帛5攔之—或多種金屬的—或多種化合物， 或:、匕口物’於至^ 400 C的溫度下熱處理Θ氧化鋁載體/ 金屬混合物；及形成觸媒，丨中該觸媒具有中位孔徑至少 為230A的孔徑分佈，其藉*astm*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乳化鋁，而一或多種金屬包括週期表第6攔的一或多種 金屬’週期表f 6攔之-或多種金屬的—或多種化合物， 或其混合物；於至少鐵的溫度下熱處理Θ氧化銘載體/ 金屬混合物；及形成觸媒，#中該觸媒具有中位孔徑至少 為230A的孔徑分佈，其藉由ASTM法Du”測定。The present invention also provides a catalyst composition, including: ⑷ of the periodic table of the sixth or more metals-or the metal of the sixth table of the periodic table-or a plurality of compounds, or a mixture thereof; ⑻ carrier, which has Θ Alumina content = at least (U grams of θ oxidized oxide in the mother gram carrier, which is determined by X-ray diffraction ', where the catalyst has a pore size distribution with a median pore size of at least 23〇A, which is determined by ASTM method D4282 This Maoming also provides a catalyst composition, which includes (a) one or more metals of the fifth table of the periodic table, one or more species of one or more metals in the fifth column of the periodic table, the period One or more metals in column 6 of the table, one or more compounds of metal or metals in the periodic table, or mixtures thereof; (b) Carrier VIII has a content of alumina of at least 0.00 g per gram of carrier. θ alumina, which is measured by X-ray diffraction; wherein the catalyst has a pore size distribution with a median pore diameter of 11 200535224 and less than 23GA, which is measured by aSt ^ D4282. The invention also provides a method for producing a catalyst, which Including: combining a carrier with one or more metals to form a carrier / Metal mixture, where the carrier contains θ ..., and the one or more metals include one or more metals in column 5 of the periodic table, or # 5 of the periodic table—or more than one metal—or more compounds, or: Heat treatment of Θ alumina carrier / metal mixture at a temperature of up to 400 C; and formation of a catalyst, wherein the catalyst has a pore size distribution with a median pore size of at least 230A, which is determined by * astm * d4282. The present invention A method for producing a catalyst is also provided, which comprises combining a carrier with one or more metals to form a carrier / metal mixture, wherein the carrier comprises Θ emulsified aluminum, and the one or more metals include one or more metals in the sixth table of the periodic table. 'Periodic table f 6-or more metals-or more compounds, or mixtures thereof; heat-treated at least the temperature of iron Θ oxidized carrier / metal mixture; and forming a catalyst, # 中 中 updated with a median pore size A pore size distribution of at least 230 A, as determined by ASTM method Du ".

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#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〇.1()1 MPa下為液態混合物該 原油進料具有至少G.3 Μ TAN，該至少—種觸媒具有中位 ^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θ氧化鋁和週期表第6攔的一或多種 金屬，週期表帛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 勿八有TAN敢多為90%之s亥原油進料的tan，其中TAN 12 200535224 係藉由ASTM法D664測定。 本毛明亦提供生產原油產物之方法，其包括：於氯源 存在下，使原油進料與一或多種觸媒接觸以生產含有原油 產物的總產物，其中該原油產物在饥和〇 l〇l Mpa下為 液態混合物，該原油進料具有至少〇3的TAN，該原油進 料具有含氧量為每克原油進料至少有〇〇〇〇1克的氧，該至 少一種觸媒具有中位孔徑至少為9〇A的孔徑分佈，其藉由 ASTM法D4282測定；及控制接觸條件使TAN減少以便使 該原油產物具有TAN最多為9〇%之該原油進料的tan， 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 ASTM法D664測^ ’而含氧量係藉由ASTM法£385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G.1G1 MPa下為液態混合物，該 原油進料具有至少〇.!的TAN，該至少一種觸媒在每克觸 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接觸區中 的液體空間速度超過10 ，並且使該原油產物具有TAN 最多為90%之該原油進料的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··於氫源 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 200535224 產物的總產物，其中該原油產物在抑和g iqi Mpa下為 液態混合物’該原油進料具有至少G1的⑽，該原油進 料具有含硫量為每克原油進料至少有Q⑼qi克的硫，該至 少一種觸媒包含週期表帛6攔的—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㈣1〇h'使該原油產物 具有TAN最多為·之該原油進料#㈣，並且使該原 油產物具有含硫量為7〇至13〇%之該原油進料的含硫量，、 其中TAN係藉由ASTM法_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’其中該原油產物纟抑和g⑻贴 下為液態混合物；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氳以抑制該原油進料在接觸期 相分離。 夕本發明亦提供生產原油產物之方法，其包括；於一或 多種觸媒存在下，使原油進料與氫接觸以 _總產物，其中該原油產物在25t和。二= 怨混合物；及控制接觸條件以便使該原油進料於第一氫吸 取條件下及接著於第二氫吸取條件下與氫接觸，第一氫吸 取條件與第二氫吸取條件不同，控制第—氫吸取條件中氫 200535224 勺淨及取以防止原油進料/總產物混合物的p值減至1 · $以 下’該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90%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，其中該原油產物 在25°C和〇·ι01 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溫度至少低於The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with-or a multi- # catalyst to produce a total product containing a crude oil product, wherein the crude oil product is at a pressure of 0.1 MPa and 1 MPa; Liquid mixture The crude oil feed has at least G.3M TAN, and the at least one catalyst has a pore size distribution with a median diameter of at least 180a, as determined by the astm method D4282, the catalyst has a And the pore size distribution of 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 produces no more than TAN It is the tan of 90% of shai crude oil feed, of which TAN 12 200535224 is determined by ASTM method D664. Ben Maoming 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 chlorine source to produce a total product containing a crude oil product, wherein the crude oil product is at a level between 100 and 10,000. l Mpa is a liquid mixture, the crude feed has a TAN of at least 0, the crude feed has an oxygen content of at least 0.001 g of oxygen per gram of crude feed, and the at least one catalyst has a medium Pore size distribution with a pore size of at least 90A, as determined by ASTM method D4282; and controlling the contact conditions to reduce the TAN so that the crude oil product has a tan of the crude oil feed with a TAN of up to 90%, and reduces The content of oxygen compounds so that the crude oil product has the oxygen content of the crude oil feed with an oxygen content of at most 90%, where ταν is measured by ASTM method D664 ^ and oxygen content is measured by ASTM method £ 385 . The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25 ° C and G.1G1 MPa The crude feed has a TAN of at least 0.1, and the at least one catalyst, in terms of metal weight per gram of catalyst, contains at least 0.0001 grams of one or more metals in column 6 of the Periodic Table. Table 6 lists 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 10 ℃, and the crude oil product has a crude oil inlet with a TAN of at most 90%. The TAN of the raw material was determined by astm method D664. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts in the presence of a hydrogen source to produce a total product containing a crude oil 13 200535224 product, wherein the crude oil product iqi Mpa is a liquid mixture 'The crude oil feed has at least G1 ⑽, the crude oil feed has a sulfur content of at least Q⑼qi grams of sulfur per gram of crude oil feed, and the at least one catalyst contains 帛 6 of the periodic table -Or more metals, column 6 of the periodic table-or more metals-or more compounds, or mixtures thereof; and controlling the contact conditions so that the crude oil feed absorbs molecular hydrogen at a selected rate during the contact to inhibit the crude oil feed Phase separation of the feedstock during contact, so that—or the liquid space velocity in the multiple contact zones ㈣10h ′, makes the crude oil product have the crude oil feed # ㈣ with a TAN of at most, and the crude product has a sulfur content The sulfur content of the crude oil feed is 70 to 13%, where TAN is measured by ASTM method and sulfur content is measured by ASTM method D4294. ~ The present invention also provides a method for producing a crude oil product, which includes: 'contacting a crude oil feed with one or more catalysts in the presence of a gaseous lice source to produce a total product containing a crude oil product' The following is a liquid mixture; and the contact conditions are controlled so that the crude oil feed absorbs radon at a selected rate during the contact period to suppress the crude feed phase separation during the contact period. The present invention also provides a method for producing a crude oil product, which comprises: contacting a crude oil feed with hydrogen in the presence of one or more catalysts to produce a total product, wherein the crude oil product is at 25 tons. Two = mixture; and control the contact conditions so that the crude oil feed is brought into contact with hydrogen under the first hydrogen uptake condition and then under the second hydrogen uptake condition, the first hydrogen uptake condition is different from the second hydrogen uptake condition, and the first —Hydrogen uptake conditions 200535224 Spoon and take to prevent the p value of the crude oil feed / total product mixture from falling below 1. $ 'One or more properties of the crude oil product are in line with one or more individual properties of the crude oil feed A change of up to 90%. The present invention also provides a method for producing a crude oil product, comprising: 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, wherein the crude oil The product is a liquid mixture at 25 ° C and 0.001 MPa. The crude oil feed has a TAN of at least 0.3, and the contact conditions are controlled such that the first contact temperature is at least lower than

第一接觸溫度30°C，使該原油產物與該原油進料的TAN 相比，具有最多為90%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 原油進料具有至少〇·3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ΤΑΝ最多為9〇%之該原油進料的 TAN，並且使該原油產物具有含硫量為7〇至ι3〇%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 200535224 其中該原油產物在乃它和0·101 MPa下為液態混合物，該 原油進料具有至少〇·丨的TAN，該原油進料具有殘留物含 量為每克原油進料至少有〇· 1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TAN最多為9〇%之該原油進料 的TAN ’使該原油產物具有殘留物含量為7〇至1 3〇%之該 原油進料的殘留物含量，其中TAN係藉由AStm法d664 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0.101 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vG〇含 量為每克原油進料至少有0.1克的VG0，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欄之一戋 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 ’使該原油產物具有VG0含量為7〇至ι3〇%之該原油 進料的VGO含量，其中VG0含量係藉由ASTM法〇53〇7 測定。 本發明亦提供生產原油產物之方法，其包括：使原油 進料與一或多種觸媒接觸以生產含有原油產物的總產物， 其 原 中該原油產物在25T：和0.101 MPa下為液態混合物該 油進料具有至少0.3的TAN’該至少一種觸媒可藉由; 16 200535224 列獲得：使載體與週期表第 — 义肩衣弟6攔的一或多種金屬，週期表 :、6欄之一或多種金屬的-或多種化合物，或其混合物結 口以產生觸媒前驅物；於—或多種含硫化合物存在下，在 低於5 0 0 C的溫度下加軌丨t卜網碰上《 …、此觸媒別•物形成觸媒；及控制 接觸條件以便使該原油產物且有 I职淘1 ΑΝ最多為90%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25t和0, MPa下為液態混合物，該 原油進料在37.rc(1，F)下具有至少10cSt的黏度，該原 油進料具有至少、10 @ 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 使邊原油產物具有在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Αρι比重 為7〇至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25T：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， 17 200535224 一或多種第6欄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法〇664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：和〇·1〇1 MPa下為液態混合物，該 原油進料具有至少的TAN ’該至少一種觸媒包含釩， 或夕種釩化合物，或其混合物；及控制接觸條件以便使 接觸酿度至少為2〇〇。(：，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係藉由八灯河法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—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购下為液態混合物，該 ^由進料具有至少Μ # TAN，該至少—種觸媒包含叙， 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最多為二之咳 18 200535224 原油進料的丁AN，其中丁AN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· 10 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1 8〇人的 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 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 至少一種觸媒包含釩，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；及控制接觸條件以 便使邊原油產物具有有機酸金屬鹽形態之驗金屬和驗土金 屬總含量最多為90%之該原油進料中有機酸金屬鹽形態的 驗金屬和驗土金屬含量，其中有機酸金屬鹽形態的鹼金屬 和驗土金屬含量係藉由ASTM法D13 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 進料與或多種觸媒接觸以生產含有原油產物的總產物， 19 200535224 其中該原油產物在25°C和G.lGl MPa下為液態混合物，該 原油進料匕§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冑，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 鹽形恶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 A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 屬和鹼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 悲的鹼金屬和鹼土金屬含量係藉由ASTM法D1 3 18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 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 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 200535224 其中該原油產物在25。。和0101 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18〇人的孔徑分佈，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 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 中位孔徑至少為23〇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 21 200535224 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 媒具有包含週期表第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 進料與一或多種_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—或多種驗土金屬冑，《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 金 鹽形態的鹼金屬和鹼土金屬總含量，該至少一種觸媒具有 中位孔仫至、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㈣重量計，$有總含翻 里為0.0001克至0.3克的錮、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冑機酸金屬 22 200535224 鹽形態之驗金屬和鹼土金屬總含量最多為9〇❶之該原油進 料中有機:酸金屬鹽形恶的驗金屬和驗土金屬含量，其中有 機酸金屬鹽形態的鹼金屬和鹼土金屬含量係藉由法 D 1 3 1 8測定。The first contact temperature is 30 ° C, so that the crude product has a TAN of up to 90% compared to the TAN of the crude feed, where TAN is determined 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 feed has a TAN of at least 0.3, the crude feed has a sulfur content of at least 0.0001 g of sulfur per gram of crude feed, and the at least one catalyst contains one or more metals in the sixth table of the periodic table. , One or more compounds of one or more metals of the Periodic Table, or a mixture thereof; and controlling the contact conditions so that the crude oil product has a TAN of TAN of up to 90% of the crude oil feed, and the crude product The sulfur content of the crude oil feed having a sulfur content of 70 to 30% is determined by ASTM method D664 and the sulfur content is measured by ASTM method D4294. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing the crude oil product, 15 200535224 wherein the crude oil product is liquid at Naita and 0 · 101 MPa Mixture, the crude feed having a TAN of at least 0, the crude feed having a residue content of at least 0.1 g per gram of crude feed, the at least one catalyst comprising column 6 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 TAN of tan up to 90% of the crude oil feed The crude product has a residue content of 70 to 130% of the crude feed, wherein TAN is determined by AStm method d664 'and residue content is determined by 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 0.101 MPa, the crude oil feed has a TAN of at least 0.1, the crude oil feed has a VG0 content of at least 0.1 g of VGO per gram of crude oil feed, and the at least one catalyst contains One or more metals in column 6, one or more compounds of one or more compounds in the periodic table, or mixtures thereof; and controlling the contact conditions so that the crude oil product has a TAN of up to 90% of the crude feed. TAN 'makes the crude oil product have a VGO content of the crude oil feed with a VG0 content of 70 to 30%, wherein the VG0 content is determined by the ASTM method 0507. The present invention also provides a method for producing a crude oil product, which Including: 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 was a liquid mixture at 25T: and 0.101 MPa; the oil feed had a TAN of at least 0.3; A catalyst can be obtained by: 16 200535224 column: the carrier and one or more metals of the Periodic Table 6-Yi Yi Yi Di, the periodic table: one or more metals of column 6-or more compounds, or mixtures thereof In order to produce catalyst precursors; in the presence of-or a variety of sulfur compounds, at a temperature lower than 500 ° C 丨 tbunet encountered "..., this catalyst species and catalyst; and The contact conditions are controlled so that the crude oil product has a TAN of 90% of the crude oil feed. The invention also provides a method for producing a crude oil product, which comprises: crude oil feed with one or more catalysts. Contact to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25t and 0, MPa, the crude oil feed has a viscosity of at least 10 cSt at 37.rc (1, F), and the crude oil feed has A specific gravity of at least 10 @ API, the at least one catalyst comprising 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; and controlling the contact conditions so that The crude oil product has a viscosity at 37.8 ° C of 90% of the crude oil feed at 37.8 C, and the crude product has an API specific gravity of 70 to 130% of the API feed of the crude oil feed. Where ApI specific gravity is determined by ASTM method D682 2 and the viscosity is determined by astM method D2669. 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 Liquid mixture at 25T: and 0.101 MPa, the crude feed has a TAN of at least 0.1, the one or more catalysts include ... one or more catalysts containing vanadium, one or more vanadium compounds, or mixtures thereof ; And an additional catalyst, wherein the additional catalyst comprises one or more metal of column 6, 17 200535224 one or more compounds of one or more metal of column 6, or a combination thereof; and controlling the contact conditions so that the crude oil product has a TAN Up to 90% of the TAN of the crude oil feed, where TAN is determined 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 feed has at least a TAN; hydrogen is produced during the contact; and the contact conditions are controlled so that the crude product has a TAN of the crude feed of up to 90% of the TAN, where TAN is determined by ASTM method 0664. 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 liquid at 25t: and 0.11 MPa A mixture, the crude feed having at least TAN ', the at least one catalyst comprising vanadium, or a vanadium compound, or a mixture thereof; and controlling the contact conditions so that the contact fermentation is at least 200. (: Make the crude oil product have a TAN of 90% of the crude oil feed, where TAN is determined by the Ba Denghe method D664. The present invention also provides a method for producing crude oil products, which includes: The raw material is contacted with—or multiple catalysts to produce a total product containing a crude oil product, wherein the crude oil product is purchased as a liquid mixture at 25t and 0.1 () 1, and the feedstock has at least M # TAN, the at least— This type of catalyst contains uranium, or multiple vanadium compounds, or a mixture thereof; a gas source containing hydrogen is supplied during the contact, and the gas stream is supplied in the opposite direction of the crude oil feed flow; and the contact conditions are controlled so that the crude oil product has the maximum TAN Ding AN 18, 200535224 Crude oil feed, wherein Ding AN is determined by ASTM method D664. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with 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. 10 1 MPa, and the crude oil feed has at least 20000 grams of total Ni / g per gram of crude oil feed V / Fe containing 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 180 people; 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 with a 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, which includes ... 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 at least one catalyst comprises vanadium, one or more vanadium compounds, Or a mixture thereof, the crude oil feed comprises one or more metallurgical 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 is in each gram of crude oil feed A total alkali metal and alkaline earth metal content in the form of a metal salt of an organic acid of at least 0.0000 g; and a metal and soil test metal that controls the contact conditions so that the crude oil product has the form of a metal salt of an organic acid The test metal and soil test metal content of organic acid metal salt form in the crude oil feed with a content of up to 90%, among which the alkali metal and test soil metal content of organic acid metal salt form are determined by ASTM method D13 1 8. 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, 19 200535224 wherein the crude oil product is a liquid mixture at 25 ° C and G.lGl MPa The crude oil feed or one or more metal test salts of organic acids, one or more alkaline earth metal hydrazones of one or more organic acids, or a mixture thereof, the crude oil feed has at least 0.00001 per gram of crude oil feed The total content of alkali metals and alkaline earth metals in grams of organic acid metal salts, the at least one catalyst has a pore size distribution with a median pore size in the range of 90 A to 180 A, and at least 60% of the total number of pores in the pore size distribution has Pore size within the median pore size range of 45 people, where the pore size distribution is determined by ASTM method D4282; and the contact conditions are controlled so that the crude oil product has an organic gold salt in the form of an organic acid metal salt Alkali metal and alkaline earth metal content in the form of organic acid metal salt of the crude oil feed with a total content of 90% of metal and alkaline earth metal, wherein the content of the alkali metal and alkaline earth metal in the form of the organic acid metal salt is determined by ASTM method D1 3 18Measurement. 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 pore size with a median pore size ranging from 90a to 280 people. Distribution, at least 60% of the total number of pores in the pore size distribution has a pore size in the 45 A median pore size range, wherein the pore size distribution is determined by ASTM method D4282; and the contact conditions are controlled so that the crude oil product has total Ni The Ni / V / Fe content of the crude oil feed at which the / V / Fe content is at most 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 feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is at 25. . It is a liquid mixture at 0101 MPa. The crude oil feed has a total alkali metal and alkaline earth metal content in the form of an organic acid metal salt per gram of crude oil feed. The at least one catalyst has a median The pore size distribution of at least 18 people is determined by the astm method D4282. The catalyst has one or more compounds containing one or more metals in column 6 of the periodic table and one or more metals in column 6 of the periodic table. Pore size distribution of a mixture thereof or a mixture thereof; and controlling the contact conditions so that the crude oil product has a total content of alkali metals and alkaline earth metals in the form of organic acid metal salts of up to 90% of the alkali metals in the form of organic acid metal salts in the crude oil feed and Alkaline earth metal content, in which the alkali metal and alkaline earth metal content in the form of a metal salt of an organic acid are measured by ASTM method D1318. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25 ° C and 0.101 MPa, The crude oil feed comprises one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or a mixture thereof. The crude oil feed has at least 0 per gram of crude oil feed. The total content of alkali metals and alkaline earth metals in the form of 0.001 g of an organic acid metal salt. The at least one catalyst has a pore size distribution with a median pore size of at least 230 A, which is determined by ASTM method D4282. The pore size distribution of one or more metals in the sixth table of the periodic table, 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 the form of a metal salt of an organic acid. The total content of alkali metals and alkaline earth metals is up to 90%. The content of alkali metals and alkaline earth metals in the form of organic acid metal salts in the crude oil feed is 21 200535224. Alkali metal and alkaline earth metal content was measured based metal salt form by means of 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 0.00002 grams of Ni / V / Fe per gram of crude feed. The at least one catalyst has a pore size distribution with a median pore size of at least 230A. D4282 determined that the catalyst has a pore size distribution 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; The product has a Ni / V / Fe content of the crude oil feed with a total Ni / v / Fe content of up to 90%, where the Ni / v / Fe content is determined by ASTM method D5708. The present invention also provides a method for producing a crude oil product, which comprises: contacting a crude oil feed with one or more oils 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 The feed contains one or more alkali metal salts of one or more organic acids, one or more organic acid-or earth-testing metals, and mixtures thereof. The crude oil feed has at least 0.0000 per gram of crude oil feed. The total content of alkali metal and alkaline earth metal in the form of gold salt is 0.01 g. The at least one catalyst has a pore size distribution with a median pore diameter of 90 A, which is determined by the astm method d4282. In the medium, based on the weight of thorium, there are thallium, one or more molybdenum compounds, or mixtures thereof with a total content of 0.0001 g to 0.3 g; and the contact conditions are controlled so that the crude oil product has a gadolinium acid 22 200535224 salt The total content of metal and alkaline earth metals in the form is up to 90%. The content of organic and acid metal in the crude oil feed of the crude oil feed is: alkali metal and alkaline earth in the form of organic acid metal salts. The metal content was measured by 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25t和〇.1()1 MPaT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9从的隸分佈，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tanThe present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25t and 0.1 (1) MPaT 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, and the at least one catalyst has a median pore size of at least 9 μm. The distribution is determined by ASTM method D4282. The catalyst has a total molybdenum content of 0.0001 to 0.3 g of molybdenum, one or more molybdenum compounds, based on the weight of molybdenum per gram of catalyst, or A mixture thereof; and controlling contact conditions so that the crude oil product has 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含塁最多為90%之該原油進料的Ni/V/Fe含量，其 中Ni/V/Fe含畺係藉由ASTM法D5708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：使原油 進料與或夕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 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，該至少一種觸媒包 23 200535224 含.（a)週期表第6欄的一或多種金屬，週期 、 n早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10攔的一或多種金屬，週期表第1〇攔之—或多種 金屬的一或多種化合物，或其混合物，其中第10欄=屬 總量與第6攔金屬總量的莫耳比在i至1〇的範圍内\及 控制接觸條件以便使該原油產物具有有機酸金屬鹽形熊之 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Μ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G.1G1 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= 0.00002克的Ni/V/Fe，該至少一種觸媒包含：（a)週^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ι〇欄的 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 金屬總量的莫耳比纟i至H)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9〇。/。之該原 油進料的Ni/V/Fe含量，其中Ni/V/Fe含量係藉由 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 200535224 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 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 鹽形態的驗金屬和鹼土金屬總含量，該一或多種觸媒包 含：（a)第一種觸媒，該第一種觸媒在每克第一種觸媒中， 以金屬重量計，含有（)·〇_至〇·()6克之週期表第6棚的 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)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，含有至少〇〇2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，其中有機酸金屬鹽形態的鹼金屬 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°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〇·〇0001克之有機酸金屬 鹽形態的鹼金屬和鹼土金屬總含量，該至少一種觸媒在每 25 200535224 克觸媒中，以金屬重量計，含有至少〇·〇〇ι克之週期表第 6襴的-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 區中的液體空間速度㈣101rl，並且使該原油產物呈有 有機酸金屬鹽形態之驗金屬和驗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，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。 曰Up to 90% of the TNA of the crude feed and the crude product has a total Ni / V / Fe content of up to 90% of the Ni / V / Fe content of the crude feed, where Ni / V / Fe contains actinide It was measured by ASTM method D5708, and TAN was measured by ASTM method D664. The invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with a catalyst to produce a total product containing a crude oil product, wherein the crude oil product is at 25. (: And a liquid mixture at 0.11 MPa, the crude oil feed comprises one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or a mixture thereof, the The crude oil feed has a total alkali metal and alkaline earth metal content in the form of an organic acid metal salt per gram of crude oil feed. The at least one catalyst package 23 200535224 contains. (A) Periodic Table 6 One or more metals in the column, period, one or more compounds of one or more metals in the 6th column, or mixtures thereof, and (b) one or more metals in column 10 of the periodic table, column 10 -— One or more compounds of multiple metals, or mixtures thereof, where column 10 = the molar ratio of the total amount to the total amount of the 6th metal is in the range of i to 10, and the contact conditions are controlled so that the The crude oil product has organic acid metal salts in the form of bears with a total content of alkali metals and alkaline earth metals of up to 90%. The alkali metal and alkaline earth metal contents in the form of organic acid metal salts in the crude oil feed, among which the alkali metals in the form of organic acid metal salts And alkaline earth metal content Determined by ASTM method M. 'The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is at 25 ° C And G.1G1 MPa is a liquid mixture, the crude oil feed has a total Ni / V / Fe content of at least = 0.00002 grams of Ni / V / Fe per gram of crude feed, the at least one catalyst comprises: (a) One or more metals in column 6 of the weekly table, one or more compounds of one or more metals in column 6 of the periodic table, or mixtures thereof; and (b) metal or metals in column ιo of the periodic table, column 1 One or more compounds of one or more metals in column 10, or mixtures thereof, in which the molar ratio of the total amount of metal in column 10 to the total amount of metal in column 6 is in the range of mol (i to H); and controlling the contact conditions so that This crude product has a total Ni / V / Fe content of up to 90. /. The Ni / V / Fe content of this crude oil feed was determined by method D5708. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil 24 200535224 feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25t and 0-101 MPa, The crude oil feed comprises one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or a mixture thereof. The crude oil feed has at least 0 · per gram of crude oil feed. The total content of test metal and alkaline earth metal in the form of organic acid metal salt of 00001 grams, the one or more catalysts include: (a) the first catalyst, the first catalyst in each gram of the first catalyst, Metal weight, containing () · 〇_ to 〇 (6) one or more metals of the sixth shelf of the periodic table, one or more compounds of one or more metals of the periodic table, or a mixture thereof; and ( b) the second catalyst, which contains at least 0.02 g of one or more metals in column 6 of the periodic table, based on the weight of the metal, per gram of the second catalyst; One or more conversions of one or more metals Materials, or mixtures thereof; 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 in a total amount of 90% of the alkali metal and alkaline earth metal in the form of organic acid metal salts in the crude oil feed Content, in which the content of alkali metal and soil metal in the form of metal salt of organic acid 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 oil feed comprises one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or a mixture thereof, the crude oil feed having at least 0.000 per gram of crude oil feed. The total content of alkali metals and alkaline earth metals in the form of 0001 grams of organic acid metal salt. The at least one catalyst contains at least 0.0000 g of Periodic Table 6 襕 per 25 200535224 grams of catalyst based on the weight of the metal. One or more metals, one or more compounds of one or more metals of the Periodic Table 'or a mixture thereof; and controlling the contact conditions so that the liquid space velocity in the contact zone is rl101rl, and the crude oil product presents an organic acid metal salt The total content of metal and soil metal in the form is up to 90%, and the content of alkali metal and alkaline earth metal in the form of metal salt of organic acid in the crude oil feed, of which organic acid gold The metal and soil metal contents in the salt form are determined by ASTM method D1318. Say

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G.⑻MPa下為液態混合物，該 原油進料在每克原油進料中具有至少克的總 =/v/Fe含量，該至少一種觸媒在每克觸媒中，以金屬重 量計，含有至少〇·_克之週期表第6欄的—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The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with-or a plurality of catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture under generation 2 and G. The crude oil feed has a total content of at least grams per gram of crude oil feed // v / Fe, and the at least one catalyst in the catalyst contains at least 0. g of the periodic table in terms of metal weight per gram of catalyst. -Or more metals, column 6 of the periodic table-or more metals-or more compounds, or mixtures thereof

σ物，及控制接觸條件以便使接觸區中的液體空間速度超 0 h並且使5亥原油產物具有總Ni/V/Fe含量最多為90% 之》亥原油進料的Nl/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〃或夕種觸媒接觸以生產含有原油產物的總產物， 其中忒原油產物在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 氧，含硫量至少為〇·〇〇〇1克的硫，該至少一種觸媒包含週 26 200535224 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 使該原油產物具有含氧量最多為9〇%之該原油進料的含氧 量，並且使該原油產物具有含硫量為7〇至13〇%之該原油 進料的含硫量，其中含氧量係藉由ASTM法E385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，含硫量至少為〇 〇〇〇1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含 硫量為70至130%之該原油進料的含硫量，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〇.〇〇〇〇1克之有機酸金屬 27 200535224 鹽形恶的驗金屬和驗土金屬總含量，殘留物含量至少為〇.丄 克的殘留物，該至少一種觸媒包含週期表第6攔的一或多 種至屬’週期表第6搁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13〇%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；!：係藉由AS TM法D13 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 之該原油進料的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σ, and control the contact conditions so that the liquid space velocity in the contact zone exceeds 0 h and the 5 Hai crude oil product has a Nl / V / Fe content of the Hai Hai crude oil feed with a total Ni / V / Fe content of up to 90% Where 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 feedstock or a catalyst to produce a total product containing a crude oil product, wherein the crude oil product is at 25. . It is a liquid mixture at 0.101 MPa. The crude oil feed has an oxygen content of at least 0.001 g of oxygen and a sulfur content of at least 0.0001 g of sulfur per gram of crude oil feed. At least one catalyst comprising one or more metals contained in Period 6 of the 200535224 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 contains The oxygen content is at most 90% of the oxygen content of the crude oil feed, and the crude product has a sulfur content of 70 to 13% of the crude oil feed, where the oxygen content is determined by It was measured by ASTM method E385, and the sulfur content was measured by ASTM method D4294. The invention also provides a method for producing a crude product, comprising: contacting a crude feed with one or more catalysts to produce a total product containing a crude product, wherein the crude product is a liquid mixture at 25 ° C and 0.101 MPa, the The crude oil feed has a total Ni / V / Fe content of at least 20,000 grams per gram of crude oil feed and a sulfur content of at least 0.001 grams of sulfur, the at least one catalyst comprising a periodic table One or more metals in column 6, one or more compounds of one or more metals in column 6 of the periodic table, or a mixture thereof; and controlling the contact conditions so that the crude oil product has a total Ni / V / Fe content of up to 90. % Of the Ni / V / Fe content of the crude oil feed, and the crude product having a sulfur content of 70 to 130% of the crude oil feed, wherein the Ni / V / Fe content is determined by the ASTM method D5708 was determined, and sulfur content was measured by aSTM method D4294. The invention also provides a method for producing a crude product, comprising: contacting a crude feed with one or more catalysts to produce a total product containing a crude product, wherein the crude product is a liquid mixture at 25 ° C and 0.101 MPa, the The crude oil feed comprises one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or a mixture thereof, and the crude oil feed has at least 0.000 per gram of crude oil feed. 〇OO1 g of organic acid metal 27 200535224 The total content of metal and soil test metal salt-shaped evils, the content of residue is at least 0. gram of residue, the at least one catalyst contains one or One or more compounds of one or more metals belonging to No. 6 of the Periodic Table, or mixtures thereof; and controlling the contact conditions 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 9 0% of the alkali metal and alkaline earth metal content in the form of metal salts of organic acids 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, wherein the alkali metal salts of organic acids and alkaline earth metal form comprising;:! Line by line while the residue content was measured by ASTM method D5307 Method TM D13 1 8 assay, AS. 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 residue content of at least 0.1 grams per gram of crude feed and a total Ni / V / Fe content of at least 0.00002 grams, the at least one catalyst comprising one or Multiple 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 at most Ni / V for the crude oil feed V / Fe content, and the crude product has a residual content of 70 to 130% of the crude feed, wherein

Ni/WFe含量係藉由ASTM法D57〇8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， 28 200535224 其中該原油產物在25它和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· 1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VGO含量為70至130% 之該原油進料的VGO含量，其中VGO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，至少〇_丨克的VGO含量，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 夕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90%之該 原油進料的Ni/V/Fe含量，並且使該原油產物具有VGO含 ϊ為70至130%之該原油進料的VGO含量，其中VGO含 29 200535224 量係藉由ASTM法D5307測定，而Ni/V/Fe含量係藉由 ASTM 法 D5708 測定。 測定。The Ni / WFe content is measured by ASTM method D57008, and the residue content is measured 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 the crude oil product, 28 200535224 wherein the crude oil product is a liquid mixture at 25 ° C and 0.101 MPa, The crude oil feed comprises one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or a mixture thereof, and the crude oil feed has at least 0 per gram of crude oil feed. 1 g of vacuum gas oil ("VGO") content, 0.0001 g of total alkali metal and alkaline earth metal content in the form of an organic acid metal salt, the at least one catalyst containing one or more metals in the sixth table of the periodic table, One or more compounds of one or more metals in column 6, or mixtures thereof; and controlling the contact conditions so that the crude oil product has an organic acid metal salt in the form of alkali metals and alkaline earth metals with a total content of up to 90% in the crude oil feed Alkali and alkaline earth metal content in the form of a metal salt of an organic acid, and the crude product having a VGO content of 70 to 130% of the VGO content of the crude feed, wherein VG The O content was measured by ASTM method D5 307, and the alkali metal and alkaline earth metal contents in the form of metal salts of organic acids were measured by ASTM method D1318. The present invention also provides a method for producing a crude oil product, comprising: contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein the crude oil product is a liquid mixture at 25 ° C and 0. 101 MPa The crude oil feed has a total Ni / V / Fe content and a minimum VGO content of at least 0.0002 grams per gram of crude feed, and the at least one catalyst includes column 6 of the periodic table. One or more metals, one or more compounds of one of the six columns of the periodic table, or a mixture thereof; and controlling the contact conditions so that the crude oil product has a total Ni / V / Fe content of up to 90% of the Ni / V / Fe content of the crude oil feed, and the crude product having a VGO content of 70 to 130% of the VGO content of the crude oil feed, wherein the VGO content of 29 200535224 is determined by ASTM method D5307, and Ni The / V / Fe content is measured by ASTM method D5708. Determination.

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 鹽形態的驗金屬和驗土金屬總含量，該至少一種觸媒可萨 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欄之一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，在低於400°C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d = U 枯：使原油 的總產物， 混合物，該 克的總 得：使載體 攔之一或多 200535224 種五屬的或多種化合物’或其混合物結合以產生觸媒前 驅物；於-或多種含硫化合物存在下，在低於彻。c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 的犯/V/Fe含量，其中Ni/V/Fe含量係藉由astm法D57〇8 測定。 本毛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 七和260°C之間的烴；至少〇·〇〇1克之沸程分佈在〇1〇1 Mpa 下介於260°C和320°C之間的烴；至少〇 〇〇1克之沸程分佈 在0.101 MPa下介於32(rc* 65〇t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（：5瀝青質含量的重量比， 其中MCR含量係藉由ASTM法〇4530測定，C5瀝青質含 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 31 200535224 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500°C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0.001克的MCR含量，該 至少一種觸媒具有中位孔徑在70人至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MCR 最多為90%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 克的鹼性氮，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 200535224 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法〇5307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I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 方法或組成物者亦提供下列原油進料：（a)尚未於精煉廠 中處理，蒸餾及/或分餾者；含有碳數大於4之成分者， 該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：在〇·ι〇ι MPa下低於l〇〇°C 的沸程分佈，在0.101 MPa下介於10(TC和200°C之間的沸 程分佈，在0.101 MPa下介於200°C和3 0(TC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：0.001克之具有沸程分佈 在0.101 MPa下低於100°C的烴，0.001克之具有沸程分佈 在0.101 MPa下介於100°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°C之間的 烴，0.001克之具有沸程分佈在0.101 MPa下介於300°C和 400°C之間的烴，及0.001克之具有沸程分佈在0.101 MPa 下介於400°C和650°C之間的烴；Ο)具有至少為0.1，至 33 200535224 少為0.3，或是在0.3至20，0.4至l〇，或〇 5 5 s _ .王^之範圍 内的TAN ; (f)具有在0.101 MPa下至少為2〇〇t：的起始 沸點；（g)包含鎳、釩和鐵；（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0.05克的硫；（k)在每克原 油進料中含有至少0.001克的VGO; (1)在每克原油進^ 中含有至少0· 1克的殘留物；（m)包含含氧烴；（n)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 oil feed comprises one or more alkali metal salts of one or more organic acids, one or more alkaline earth metal salts of one or more organic acids, or a mixture thereof. The crude oil feed has at least 0 · per gram of crude oil feed. The total content of metal and soil in the form of 00001 grams of organic acid metal salt. The at least one catalyst can be obtained from the carrier and one or more metals in the sixth table of the periodic table. One or more compounds of a plurality of metals, or a mixture thereof, to produce a catalyst precursor, which is heated at a temperature below 400 ° C in the presence of one or more sulfur-containing compounds to form a catalyst; and control Contact conditions so that the crude oil product has an alkali metal and alkaline earth metal in the form of organic acid metal salt in a total amount of 90% of the alkali metal and alkali in the form of organic acid metal salt in the crude oil feed Metal 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 = U: make the total product of crude oil, mixture, the total of this gram: make the carrier block one or more 200535224 five genus Or more of the compounds' or mixtures thereof to produce a catalyst precursor; in the presence of-or more sulfur-containing compounds, at a lower temperature. heating the catalyst precursor at a temperature of c to form a catalyst; and controlling the contact conditions so that the crude oil product has a crude N / V / Fe content of at most 90% of the crude feed / V / Fe content, of which The Ni / V / Fe content was measured by the astm method D57708. Ben Maoming also provides crude oil compositions containing the following in each gram of crude oil composition. At least 0.001 grams of hydrocarbons having a boiling range distribution between 0,007 and 260 ° C at 0,001 MPa; at least 0. 〇1 gram boiling range distribution of hydrocarbons between 260 ° C and 320 ° C at 001 MPa; at least 0.001 grams boiling range distribution between 32 (rc * 65 〇t at 0.101 MPa) Hydrocarbons; and one or more catalysts per gram of crude oil product, but less than 0.001 grams. The present invention also provides crude oil compositions containing at least one of the following in each gram of crude oil composition. 〇1 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 of at least 1.5 to (: 5 asphaltene content, The MCR content is determined by ASTM method 054530, 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 includes: contacting a crude oil feed with one or more catalysts to produce Total product containing crude oil product, where the crude oil product is at 25 ° C and 0.101 MPa Condensable, the crude oil feed has an MCR content of at least 0.001 grams per gram of crude oil feed, and the at least one catalyst can be obtained by the following: the carrier and one or more metals in the sixth table of the periodic table , One or more compounds of one or more metals in column 6 of the Periodic Table 31 200535224, or a combination thereof to produce a catalyst precursor; in the presence of one or more sulfur compounds, at a temperature below 500 ° C Heating the catalyst precursor to form a catalyst; and controlling the contact conditions so that the crude oil product has an MCR content of the crude oil feed with an MCR content of up to 90%, wherein the MCR content is measured by ASTM method D4530. The present invention also Provided is 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 condensable at 25 ° C and 0.101 MPa, and the crude oil feed is at Each gram of crude oil feed has an MCR content of at least 0.001 grams, the at least one catalyst has a pore size distribution with a median pore size ranging from 70 to 180 people, and at least 60% of the total pore size in the pore size distribution has a 4 5 A 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 an MCR of 90% of the MCR of the crude oil feed, where the MCR is obtained by Determined by ASTM method D4530. The present invention also provides a crude oil composition that contains the following in each gram of composition ... up to 0.004 grams of oxygen, measured by ASTM method E385; up to 0.003 grams of sulfur, by ASTM method D4294 Assay; and at least 0.3 grams of 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 Basic nitrogen, which is determined by ASTM method D2896; at least 0.2 g of residue, which is measured by ASTM method D5307; and the composition, which has a maximum of 32 200535224 and a TAN of 0.5, which is measured by ASTM method D664. The present invention also provides a crude oil composition containing at least 0.001 grams of sulfur per gram of composition, which is determined by ASTM method D4294; a residue of at least 0.2 grams, which is measured by aSTM method 05307; 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 I asphaltene was determined 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, are distilled and / or fractionated; contain carbon greater than 4 In terms of composition, the crude oil feed contains at least 0.5 g of such feeds per gram of crude oil feed; (c) contains hydrocarbons, part of which has: less than 100 MPa at 0.00 MPa ° C boiling range distribution between 0.1 ° C and 200 ° C boiling range distribution at 0.101 MPa, boiling range distribution between 200 ° C and 30 ° C (0.101 MPa) at 0.101 MPa Boiling range distribution between 300 ° C and 400 ° C at MPa, and boiling range distribution between 400 ° C and 650 ° C at 0.101 MPa; (d) Contained in each gram of crude oil feed At least: 0.001 grams of hydrocarbons with boiling range distribution below 0.101 MPa, 0.001 grams of hydrocarbons with boiling range distribution between 0.1 ° C and 200 ° C at 0.101 MPa, and 0.001 grams of boiling range distribution Hydrocarbons between 200 ° C and 300 ° C at 0.101 MPa, 0.001 g of hydrocarbons with a boiling range distribution between 300 ° C and 400 ° C at 0.101 MPa, and 0.001 g Hydrocarbons having a boiling range distribution between 400 ° C and 650 ° C at 0.101 MPa; 0) having at least 0.1, to 33 200535224 and less to 0.3, or 0.3 to 20, 0.4 to 10, or TAN in the range of 0 5 5 s _. Wang; (f) has an initial boiling point of at least 200 t at 0.101 MPa; (g) contains nickel, vanadium and iron; (h) per gram Crude feed contains at least 0.00002 grams of total Ni / V / Fe; ⑴ contains sulfur; ⑴ contains at least 0.0001 grams or 0.05 grams of sulfur per gram of crude feed; (k) contains at least 0.001 grams per gram of crude feed 0.001 grams of VGO; (1) contains at least 0.1 grams of residue in each gram of crude oil feed; (m) contains oxygen-containing hydrocarbons; (n)

多種有機酸的一或多種驗金屬鹽，一或多種有機酸的 戈 多種鹼土金屬鹽，或其混合物；（〇)包含有機酸的至少— 種鋅鹽；及/或（P)包含有機酸的至少一種坤鹽。 於若干具體實例中，本發明與結合本發明之一充夕 我多種 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武夕 故夕種One or more metal test salts of a plurality of 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 kind of kun salt. 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 which can be obtained by removing naphtha in crude oil and compounds more volatile than naphtha. Crude oil feed. In several specific examples, the present invention and a combination of one of the present inventions

方法或組成物者亦提供使原油進料與一或多種觸媒接觸以 生產含有原油產物之總產物的方法，其中該原油進料和原 油產物兩者都具有C5遞青質含量和MCR含量，且·,、 ^ ^ 且· U)原 油進料之I瀝青質含量和原油進料之MCR含量的和為s， 原油產物之C5瀝青質含量和原油產物之MCR含量的和為 S ’控制接觸條件以便使s’最多為99%的S ;及/或（b) # 制接觸條件以便使原油產物之MCR含量與原油產物之c 遞青質含量的重量比在1.2至2.0,或1.3至1.9的範圍内。5 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氫源，其中該氫源為：（a)氣態；（七) 34 200535224 氫氣’（C)甲烧，⑷輕垣；（e)惰性氣體；及/或⑴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一或多種觸媒接觸以 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，使原油進料與一或多種觸媒接觸及控制接觸條件籲 以便使：（a)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8〇0標準立方米之氣 態氫源的範圍内；（b)藉由改變氫源分壓以控制氫的選定 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)氫的選定吸取率 在每立方米的原油進料中為i至3〇或1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 _ 為丨1 h-1，至少為15 1Γ1，或最多為20 h-i ;⑴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(rc 的範圍内’氣體及/或氫源的總液體空間速度在〇. i至3 〇 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/或氳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130%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 200535224 原油進料中悬1… 匕^取夕為80及/或1至80或1至5〇標準立方米 之氳的範圍内，（k)該原油產物具有總Ni/V/Fe含量最多 =〇%’取多為5〇%，或最多為之該原油進料的Ni/V/Fe ^ () °亥原'由產物具有硫含量為70至130%或80至120% 之5亥原油進料的硫含量；㈣該原油產物具有VG0含量The method or composition also provides a method of contacting a crude oil feed with one or more catalysts to produce a total product containing a crude oil product, wherein both the crude oil feed and the crude oil product have a C5 cyanide content and an MCR content, And ,,, ^ ^ and · U) The sum of the I asphaltene content of the crude oil feed and the MCR content of the crude oil feed is s, and the sum of the C5 asphaltene content of the crude oil product and the MCR content of the crude oil product is S 'control contact Conditions so that s' is at most 99% of S; and / or (b) # contact conditions so that the weight ratio of the MCR content of the crude product to the c-cyanocyanine content of the crude product is 1.2 to 2.0, or 1.3 to 1.9 In the range. 5 In some specific examples, the present invention and those combining one or more methods or compositions of the present invention also provide a hydrogen source, wherein the hydrogen source is: (a) gaseous state; (seven) 34 200535224 hydrogen '(C) methylbenzene , Li Qingyuan; (e) an inert gas; and / or a mixture thereof. In certain 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 one or more 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 several specific examples, the present invention and those combining one or more methods or compositions of the present invention also provide a method comprising contacting a crude oil feed with one or more catalysts in the presence of a gas and / or hydrogen source and The contact conditions are controlled so that: (a) the ratio of the gaseous hydrogen source to the crude oil feed is 5 to 800 standard cubic meters of the gaseous hydrogen source per cubic meter of crude oil feed in contact with one or more catalysts; Within the range; (b) controlling the selected net absorption rate of hydrogen by changing the partial pressure of the hydrogen source; (c) the absorption rate of hydrogen makes the crude oil product have a TAN less than 0.3, but the hydrogen absorption system is less than that during contact Hydrogen uptake that results in substantial phase separation between the crude oil feed and the total product; (d) The selected hydrogen uptake rate is from i to 30 or 1 to 80 standard cubic meters of hydrogen per cubic meter of crude feed (E) the liquid space velocity of the gas and / or hydrogen source is at least _ 1 h-1, at least 15 1 Γ1, or at most 20 hi; 控制 controls the gas and / or hydrogen source during contact Partial pressure; (g) contact temperature in the range of 50 to 50 (rc) of the gas and / or hydrogen source The space velocity of the liquid is in the range of 0.1 to 30, and the total pressure of the gas and / or hydrogen source is in the range of 10 to 20 MPa. (H) The flow of the gas and / or tritium source is toward the crude oil. The feed flows in the opposite direction; (i) the crude product has an H / C of 70 to 130% of the H / C of the crude feed; (j) the hydrogen absorbed by the crude feed is 35 200535224 per cubic meter The crude oil feed is suspended in the range of 1 ... 取 夕 is within the range of 80 and / or 1 to 80 or 1 to 50 standard cubic meters, (k) the crude product has a maximum total Ni / V / Fe content = 〇 % 'Is taken as 50%, or at most Ni / V / Fe ^ () ° of the crude oil feed, from the product of 50 Hai crude oil with a sulfur content of 70 to 130% or 80 to 120% Sulfur content of the feedstock; ㈣ the crude oil product has a VG0 content

為7〇入至旦13〇%或9〇至11〇%之該原油至13〇%或9進料的 GO 3里’⑷该原油產物具有殘留物含量為7⑼至η 〇% ^該原油進料的殘“含量；（。）該原油產物具有氧含量 =多為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；（ρ)該原油產物且有 有機酸金屬鹽形態的驗金屬和驗土金屬總含量最多為 9〇%，最多為5G%，或最μ 1()%之㈣油進㈣有機酸 金屬鹽形態的驗金屬和驗土金屬含量；⑷在接觸期間， 3亥原油進料的p值曼少或彳< ./ 。 丁十7 F值至夕為丨·5, ω該原油產物具有在37.8It is 70% to 130% or 90% to 110% of the crude oil to 13.0% or 9 of the GO 3 feed. The crude product has a residue content of 7% to η0%. Residual content of feedstock; (.) The crude oil product has an oxygen content = 90% at most, 70% at most, 50% at most, 40% at most, or 10% of the crude oil feed (Ρ) The total content of the test metal and soil test metal in the form of organic acid metal salt of the crude oil product is at most 90%, at most 5G%, or at most 1 ()% of the oil in the oil Test metal and soil metal content in the form of acid metal salt; ⑷ During the contact period, the p value of the crude oil feed of Hai Hai was less than or 彳 < ./. The product has a value of 37.8

c下的黏度最多為9G%，最多為5G%，或最多$肌之該 原油進料纟37.8。。下的黏度；(s) f亥原油產物具有Αρι比 重為70至130%之該原油進料的Αρι比重；及/或⑴該 原油產物具有TAN最多為9G%，最多為鄕，最多為麗， 最多為20%，或最多為10%之該原油進料的tan及/或在 〇.〇(Η至0.5,0.01至0_2,或0.05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，其包含使原油進料盥一 或多種觸媒接觸及控制接觸條件以減少含有機氧化合物的 含量’其中：⑷減少選定有機氧化合物的含量以便使該 36 200535224 原油產物具有含氧S最多為90%之該原油進料的含氧量；（b) 含有機氧化合物的至少一種化合物包含羧酸之金屬鹽；（幻 含有機氧化合物的至少一種化合物包含羧酸之鹼金屬鹽；（d) 含有機氧化合物的至少一種化合物包含羧酸之鹼土金屬 鹽，（e)含有機氧化合物的至少一種化合物包含羧酸之金 屬鹽，其中此金屬包括週期表第12欄的一或多種金屬；（f) 孩原油產物具有含非羧酸有機化合物含量最多為9〇%之該 原油進料中的含非魏酸有機化合物含量；及/或（g)該原 油進料中的至少一種含氧化合物係產自含環烷酸或非羧酸 的有機氧化合物。 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方法，其包含使原油進料與一 或多種觸媒接觸，其中：（a)於第一溫度下，使該原油進 料與至少一種觸媒接觸，接著於第二溫度下接觸，控制接 觸條件以便使第一接觸溫度至少低於第二接觸溫度3〇£^ ; (七）於第一氫吸取條件下然後在第二氫吸取條件下，使該 原油進料與氫接觸，第一吸取條件的溫度係至少低於第2 吸取條件的溫度3(TC ; (c)於第一溫度下，使該原油進料 與至少一種觸媒接觸，接著於第二溫度下接觸，控制接觸 條件以便使第一接觸溫度最多低於第二接觸溫度2⑼艺；（旬 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 使該原油進料與第一和第二種觸媒接觸，該原油進料與第 種觸媒的接觸生成初原油產物，其中此初原油產物具有 37 200535224 TAN最多為90%之該原 器中進行接觸.仆、的丁AN; (g)於堆疊床反應 該原油進料在與中進行接觸；⑴使 /種觸媒接觸之後與附加觸媒接觸，·⑴ 口亥或多種觸媒為釩觸婵，伯兮店丄 U； 觸之後，於進料在與該飢觸媒接 方乎斥、山Γ 與附加觸媒接觸；（k)氫係以每立 π 〇軚準立方米之範圍内的速率產生，·⑴ 在接觸期間產生氫，於痛 下，# s、 於礼體和至少一部分生成氫的存在 下使W亥原油進料盘RU Μ gw Ky.The viscosity under c is at most 9G%, at most 5G%, or at most $ 37.8 for this crude oil feed. . (S) f Hai crude oil product has an Aρι specific gravity of 70 to 130% of the crude oil feed; and / or 原油 the crude oil product has a TAN of at most 9G%, at most 鄕, at most Li, The tan of the crude oil feed is at most 20%, or at most 10%, and / or is in the range of 0.000 to 0.5, 0.01 to 0_2, or 0.05 to 0.01. In several specific examples, the present invention In combination with one or more methods or compositions of the present invention, there is also provided a method comprising contacting crude oil feed with one or more catalysts and controlling the contact conditions to reduce the content of organic oxygenated compounds, wherein: ⑷ reduce selected organic The content of oxygen compounds so that the 36 200535224 crude oil product has the oxygen content of the crude oil feed containing oxygen S of at most 90%; (b) at least one compound containing organic oxygen compounds contains a metal salt of a carboxylic acid; At least one compound of an organic oxygen compound comprises an alkali metal salt of a carboxylic acid; (d) at least one compound containing an organic oxygen compound comprises an alkaline earth metal salt of a carboxylic acid; (e) at least one compound containing an organic oxygen compound contains gold of a carboxylic acid Salt, where the metal includes one or more metals in column 12 of the periodic table; (f) the crude oil product has a non-weilic acid-containing organic compound content in the crude oil feed with a non-carboxylic acid-containing organic compound content of up to 90% And / or (g) the at least one oxygen-containing compound in the crude oil feed is produced from a naphthenic acid or a non-carboxylic acid-containing organic oxygen compound. In several specific examples, the present invention is combined with one or more of the present invention The method or composition also provides a method comprising contacting a crude oil feed with one or more catalysts, wherein: (a) contacting the crude oil feed with at least one catalyst at a first temperature, followed by Contact at two temperatures, control the contact conditions so that the first contact temperature is at least 30 pounds lower than the second contact temperature; (seven) under the first hydrogen uptake conditions and then under the second hydrogen uptake conditions, feed the crude oil In contact with hydrogen, the temperature of the first absorption condition is at least lower than the temperature of the second absorption condition 3 (TC; (c) at a first temperature, the crude oil feed is brought into contact with at least one catalyst, and then at a second temperature Down contact, control contact bar In order to make the first contact temperature lower than the second contact temperature at most 2 times; (ten times to generate hydrogen during the contact; (e) to generate hydrogen during the contact, and control the contact conditions so that the crude oil feed absorbs at least a portion of the hydrogen produced. (0) The crude oil feed is brought into contact with the first and second catalysts, and the contact of the crude oil feed with the first catalyst produces a crude oil product, wherein the crude oil product has 37 200535224 TAN at most 90% of the (G) reacting the crude oil feed in contact with the stacker; contacting the additional catalyst after contacting the catalyst / kind of catalyst; The medium is vanadium catalyst, Bo Xidian 丄 U; after the contact, Yu feed is in contact with the catalyst, and Γ is in contact with the additional catalyst; (k) hydrogen system is quasi-cubic cubic per cubic π Rates in the range of meters are produced, · ⑴ generates hydrogen during contact, and under pain, # s, in the presence of ceremonial body and at least a portion of the generated hydrogen, makes the Whai crude oil feed tray RU MW gw Ky.

# # ^ ^ Μ ^力觸媒接觸，並且控制接觸條件以 便使氣體動朝菩、丄、# 與原油進料_和生成氫㈣相反的方 向，（m)使該原油進料於M 一 w 、 μ度下與釩觸媒接觸，隨後 、:：：？度下與附加觸媒接觸，控制接觸條件以便使第一 >皿度至少低於第二溫产 祐#店、丄、 又 C , (η)在接觸期間產生氳氣， 使以原油進料與附加觸媒 安觸控制接觸條件以便使該附 ;μ吸取至少一部分的生成氨’·及/或（〇)隨後於第二溫 :下使该原油進料與附加觸媒接觸，控制接觸條件以便 弟二溫度至少為l8(rc。# # ^ ^ Μ ^ force the catalyst to contact, and control the contact conditions so that the gas moves in the opposite direction to the crude oil feed_ and the hydrogen generation, (m) feed the crude oil to M_w , In contact with vanadium catalyst at μ degree, and then :::? Contact with the additional catalyst at a lower temperature, and control the contact conditions so that the first temperature is at least lower than the second temperature. # 产, 店, and C, (η) generates radon gas during the contact period, and feeds with crude oil. An contact with an additional catalyst to control the contact conditions in order to make the adhesion; μ suck at least a part of the generated ammonia '· and / or (〇) and then contact the crude feed with the additional catalyst at a second temperature: to control the contact conditions So that the second temperature is at least 18 (rc.

於若干具體實例中’本發明與結合本發明之一或多種In several specific examples, the invention is combined with one or more of the invention

方法或組成物者亦提供—錄古土 甘A A J Μ、種方法，其包含使原油進料盥一 或多種觸媒接觸，其中：⑷該觸媒為受載觸媒而載體包 含乳化銘、氧化石夕、氧化石夕-氧化銘、氧化鈦、氧化錯、氧 化叙，或其混合物；⑻該觸媒為受載觸媒而載體為多孔 性；⑷此方法尚包括在硫化前已在高於4〇〇。。之溫度下 處理過的附加觸媒；⑷該至少一種觸媒的壽命至少：〇 5 年；及/《⑷該至少一種觸媒係於固定床中或懸浮於原 38 200535224 油進料中。 於若干具體實例中，本發明與結合本發明之 方法或組成物者亦提佴— 次夕種 或多種觸媒接觸，…彳法，其包含使原油進料與- 觸媒，該受載觸媒種觸媒為受載觸媒或塊狀金屬 至10椚Μ 一 Α狀金屬觸媒：（a)包含週期表第5 至10攔的一或多 力衣弟5 金屬的-或多種务人 期表第5至1〇欄之-或多種 含有至少〇.〇〇〇 °物’或其混合物；⑻在每克觸媒中 之：週期表第5至1M〇·0001至〇.6克，或〇.001至〇·3克 攔之-或多種金層」 多種金屬，週期表第5至1〇 含週期表第6至 或多種化合物，或其混合物；（c)包 攔之-或多種攔的—或多種金屬，週期表第6至10 含週期表繁7 或夕種化合物，或其混合物；（d)包 搁之一或多種金Μ 或多種金屬，週期表第7至1〇 每克觸媒中人古的或多種化合物，或其混合物；（e)在 期表第7至1Ω /侧1至G·6克或請1至G.3克之：週 一或多種金屬或多種金屬，週期 週期表第5至 &lt; 夕種化合物，或其混合物；（f)包含 一或多種金屬：攔的一或多種金屬，週期表第5至6襴之 週期表第5攔的一：：種化合物’或其混合物；⑻包含 金屬的一或夕、或夕種金屬，週期表第5攔之一或多種 含有至少合物’或其混合物，·（h)在每克觸媒中 至°，1克，或 金屬，週期表第5攔之一;多之種=第::的-或多種 飞夕禋I屬的一或多種化合物， 39 200535224 或其混合物；4人、 期表第6捫 匕3週期表第6攔的一戋多種i 期表弟6攔之—或多 -乂夕種金屬，週The method or composition also provides-recording ancient tugan AAJ M, a method comprising contacting the crude oil feed with one or more catalysts, wherein: the catalyst is a supported catalyst and the carrier contains an emulsified name, oxidation Shi Xi, Shi Xi-oxide oxide, titanium oxide, oxide oxide, oxide oxide, or mixtures thereof; ⑻ the catalyst is a supported catalyst and the carrier is porous; 方法 this method also includes 4〇〇. . Additional catalyst treated at the temperature; the life of the at least one catalyst is at least: 05 years; and / / the at least one catalyst is in a fixed bed or suspended in the original 38 200535224 oil feed. In several specific examples, the present invention and those who combine the method or composition of the present invention also mention-contacting the next species or catalysts, ..., the method, which comprises feeding crude oil with-catalysts, the loaded catalysts The medium catalyst is a loaded catalyst or a block metal to 10 μM, an A-shaped metal catalyst: (a) one or more of the five or more metal-containing agents including the 5th to the 10th periodic table. Columns 5 to 10 of the Periodic Table-or more containing at least 0.00000 ° 'or mixtures thereof; ⑻ per gram of catalyst: 5 to 1M.0001 to 0.6g of the Periodic Table, Or 0.001 to 0.3 grams of gold- or more gold layers "a variety of metals, 5 to 10 of the periodic table containing 6 to or more compounds of the periodic table, or mixtures thereof; (c) contained-or more Blocked—metals or metals, Periods 6 to 10 of the periodic table containing 7 or more compounds of the Periodic Table, or mixtures thereof; (d) One or more gold M or metals, per 7 to 10 of the Periodic Table Grams of the ancient or multiple compounds in the catalyst, or mixtures thereof; (e) in the period 7 to 1 Ω / side 1 to G · 6 grams or 1 to G.3 grams: Monday or more metals or Metals, Periodic Table 5 to <Even compounds, or mixtures thereof; (f) one or more metals containing one or more metals: one or more metals of Periodic Table 5 to 6; :: a compound 'or a mixture thereof; 一 one or more metals containing one or more metals, one or more of the Periodic Table 5 contains at least a compound' or a mixture thereof, (h) in each gram of catalyst To °, 1 gram, or metal, one of the fifth block of the Periodic Table; multiple species = No. :::-or one or more compounds of the genus Feijing I, 39 200535224 or a mixture thereof; 4 persons, the periodic table A 6th period of the Periodic Table 3 A 6th period of the Periodic Table, a cousin of a period i of 6 or more-a kind of metal, Zhou Xi

物；⑴在每克觸媒中含有/H化合物，或其混合 克，㈣5至（U克，2 1至〇·6克，至U 十夕必：八研 至〇·〇8克之週期矣笙 或夕種金屬’週期表第6攔之_ :表“欄的一 合物，或其混合物；（k 八、/ 、，屬的一或多種化 匕含週期表第1〇欄的一 屬/週期表第1〇_之-或多種金屬的-或多種= 或其混合物；（1)在备古鎞讲 飞夕種化合物， 至。.3克之：週期表第10們中含有〇__至°.6克或ο·。。1 攔之一或多種全屬的-戈夕或多種金屬’週期表第10 種金屬㈤或多種化合物，或其混合物；⑻包 “凡’ -或多種釩化合物，或其混合物；⑻&amp;含鎳，一 或多種鎳化合物’或其混合物·，（。）&amp;含始，-或多種始 化合物，或其混合物；（P)包含，一或多種鉑化合物， 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：鉬，一或多種鉬化合物，或其混合物；（〇包 δ嫣’一或多種鎢化合物，或其混合物；（s)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1〇欄的一或多種金屬，其中第1〇欄金屬與第6攔金屬 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0 00001至0.06克之： 週期表第15欄的一或多種元素，週期表第15欄之一或多 種元素的一或多種化合物，或其混合物；（w)填，一或多 200535224 種碟化合物， 克的α氧化鋁 氧化鋁。 或其混合物’· (χ)在每克觸媒中含有最多 及/或（y)在每克觸媒中含有至少0.5 0.1 的Θ 方^若干具體實財，本發明與結合本發日月之一或多牙 者亦提供形成觸媒之方法，其包括使㈣Contains / H compound per gram of catalyst, or a mixed gram thereof, ㈣5 to (U gram, 21 to 0.6 grams, to U december must: the period of eight research to 〇08 gram Or a kind of metal 'Periodic Table 6 of the _: a compound in the column of the table, or a mixture thereof; (k eight, / ,, one or more of the genus contains a genus of column 10 of the periodic table / Periodic Table 10th-or more metals-or more = or mixtures thereof; (1) In the ancient history of Beiguquan compounds, to .3 grams: the 10th period of the periodic table contains 0_ to ° .6 grams or ο ... 1 block of one or more of the genus-Ge Xi or multiple metals 'Periodic Table 10th metal rhenium or multiple compounds, or mixtures thereof; "Van'-or multiple vanadium compounds , Or a mixture thereof; ⑻ &amp; containing nickel, one or more nickel compounds' or a mixture thereof, (.) &Amp; containing a starting compound, or a plurality of starting compounds, or a mixture thereof; (P) comprising, one or more platinum compounds, Or a mixture thereof; (q) containing 0.001 to 3.0 g or 0.05 to 0.1 g per gram of catalyst: molybdenum, one or more molybdenum compounds, or a mixture thereof ; (0 package δ Yan 'one or more tungsten compounds, or mixtures thereof; (s) containing 0.001 to 0.3 g per gram of catalyst: tungsten, one or more tungsten compounds, or mixtures thereof; (t) containing cycles One or more metals in Table 6 and one or more metals in column 10 of the Periodic Table, wherein the molar ratio of the metal in column 10 to the metal in column 6 is 1 to 5; (u) Includes 15 of the periodic table One or more elements in the column 'One or more compounds of one or more elements in the Periodic Table, or mixtures thereof; (V) containing 0 00001 to 0.06 g per gram of catalyst: one in column 15 of the Periodic Table Or more elements, one or more compounds of one or more elements of column 15 of the periodic table, or mixtures thereof; (w) fill in one or more 200535224 dish compounds, grams of alpha alumina alumina. Or mixtures thereof (χ) contains the most per gram of catalyst and / or (y) contains at least 0.5 0.1 of Θ per gram of catalyst ^ Several specific real assets, the present invention and the combination of one or more teeth Methods of forming catalysts are also provided, including using

一或多種金屬結合以报士 # Μ ,人P 7成载體/金屬混合物，其中該載體έ 含Θ氧化鋁，於至少4〇n〇r ΑΑ、泣十 1 ^ v 40〇c的溫度下熱處理Θ氧化鋁載體ΜOne or more metals are combined with a report of #M, human P7 into a carrier / metal mixture, wherein the carrier contains Θ alumina at a temperature of at least 4n0r ΑΑ, 1% v 4 0c. Heat-treated Θ alumina support Μ

θ物而且尚包括·（a)使載體/金屬混合物盥水έ士 A 以：成糊狀物，擠壓此糊狀物；(b)於至少800;的二 :糟由熱處理氧化銘而得到㈣化紹；及/或⑷使該觸销 硫化。 、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一 或了種觸媒接觸，其中該一或多種觸媒的孔徑分佈具有⑷ 至少為60人，至少為9〇人，至少為18〇 A，至少為2〇〇 A， v為230人’至少為300人，最多為230人，最多為500人， 或是在 90 至 180 Λ，1〇〇 至 140 Λ，120 至 130 Λ，230 至 25〇 A，180 至 500 A，230 至 500 人；或 6〇 至 300 人之範 圍内的中位孔徑；（b)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；（c)至少為6〇 m2/g，至 少為90 m2/g，至少為1〇〇 m2/g，至少為i2〇 mVg，至少為 15〇 m2/g，至少為200 m2/g，或至少為22〇 m2/g的表面積； 及/或（d)至少為0.3 cm3/g，至少為〇·4 cm3/g，至少為〇 5 cm /§ ’或至少為0·7 cm3/g之所有孔徑的總體積。 41 200535224 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，其中該載體：（a)包含氧化鋁、氧 化矽、氧化矽-氧化鋁、氧化鈦、氧化锆、氧化鎂，或其混 合物，及/或沸石；（b)包含丫氧化鋁及/或δ氧化鋁；（c)在 每克載體中含有至少0.5克的7氧化鋁；（d)在每克載體中 3有至y 0.3克或至少〇·5克的㊀氧化鋁；（e)包含以氧化 鋁、丫氧化鋁、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α氧化鋁。 於若干具體實射，本發明與結合本發明 &lt; —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 少為60A的孔徑分佈；（b)包含載體，此載體包含㊀氧化 鋁，而該釩觸媒具有中位孔徑至少為6〇人的孔徑分佈；（c) 包含週期表第6攔的-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/或（句在 每克觸媒中含有至少、0·001克之··週期表第6搁的一或多 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。 於右干具體實例中 方法或組成物者亦提供一種原油產物，其具有：最多 為 0.1 ’ 0.001 至 0.5，〇〇1 υ·υΐ 主 υ·2，或 0.05 至 〇·1 的 TAN ; 不贫明與結合本發明 ⑻在每克原油產物中最多為請咖9克之有機酸金屬鹽 形態的鹼金屬和鹼土金屬；⑷纟每克原油產物中最多為 0.0_2克之而V/Fe;及/或⑷在每克原油產物中大於 42 200535224 〇克’但小於〇.〇1克的至少一種觸媒。 於若干具體實例中，本發明鱼处人I * 月興結合本發明之一或多種 方法或組成物者亦提供一或多猶古 乂夕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於 • Λ夕禋鹼土金屬鹽，或其混合物， 其中·（a)該至少一種驗金屬為叙 蜀兩鋰、鈉，或鉀；及/或（b)該 至J 一種驗土金屬為鎮或舞。 於右干具體實例中，本發明血从人丄々 +心月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Theta also includes: (a) making the carrier / metal mixture to wash water A to: form a paste, squeeze the paste; (b) at least 800; two: the bad is obtained by heat treatment and oxidation ㈣ Hua Shao; and / or ⑷ vulcanize the contact pin. In certain specific examples, the present invention and those who combine 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 one or more catalysts Has a pore size distribution of at least 60, at least 90, at least 180A, at least 2000A, v at 230, 'at least 300, at most 230, and at most 500, or Is the median aperture in the range of 90 to 180 Λ, 100 to 140 Λ, 120 to 130 Λ, 230 to 25 OA, 180 to 500 A, 230 to 500 people; or 60 to 300 people; ( b) at least 60% of the total number of pores have a pore size in the median pore size range of 45, 35, or 25 people; (c) at least 60 m2 / g, at least 90 m2 / g, at least 1 〇m2 / g, at least i20mVg, at least 150m2 / g, at least 200m2 / g, or at least 22m2 / g surface area; and / or (d) at least 0.3 cm3 / g The total volume of all pore diameters of at least 0.4 cm3 / g, at least 0.05 cm / § ', or at least 0.7 cm3 / g. 41 200535224 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 supported catalysts, wherein the carrier: (a ) Comprises alumina, silica, silica-alumina, titania, zirconia, magnesia, or mixtures thereof, and / or zeolites; (b) comprises alumina and / or delta alumina; (c) in Each gram of support contains at least 0.5 grams of 7 alumina; (d) 3 to y 0.3 grams or at least 0.5 grams of rhenium alumina in each gram of support; (e) contains alumina, alumina, Delta alumina, theta alumina, or mixtures thereof; (f) containing up to 0.1 grams of alpha alumina per gram of support. In some specific shots, the present invention and the combination of the present invention &lt; or more methods or compositions also provide a vanadium catalyst: (a) having a pore size distribution with a median pore size of at least 60A; (b) including a carrier, which The support contains thorium alumina, and the vanadium catalyst has a pore size distribution with a median pore size of at least 60 people; (c) contains the metal of the sixth table of the periodic table-or more metals, and the One or more compounds, or mixtures thereof; and / or (in each gram of the catalyst, at least, 0.001 g of the one or more metals of the sixth table of the periodic table, one or more metals of the sixth table of the periodic table One or more compounds, or a mixture thereof. The method or composition in the specific example of the right also provides a crude oil product having: at most 0.1 '0.001 to 0.5, 0.001 υ · υΐ main υ · 2, or TAN from 0.05 to 0.1; not depleted and combined with the present invention, the maximum amount of alkali metal and alkaline earth metal in the form of organic acid metal salt is 9 g per gram of crude oil product; the maximum value of 0.0 per gram of crude oil product _2 grams of V / Fe; and / or At least one catalyst in a crude oil product that is greater than 42 200535224 0 g 'but less than 0.01 g. In several specific examples, the fish of the present invention I * Yue Xing combines one or more methods or compositions of the present invention. Provide one or more alkali metal salts of one or more organic acids, one or more organic acids of one or more organic acids, or mixtures thereof, wherein (a) the at least one test The metal is Lithium, Sodium, or Potassium; and / or (b) the soil testing metal is Jin or Wu. In the specific example of the right stem, the blood of the present invention consists of a human heart, a heart, and a heart. Inventor of one or more methods or compositions also provides a method

乃次其包含使原油進料與一 或多種觸媒接觸以生產含有席、、占 3虿原油產物的總產物，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 結合以形成適詩運輸㈣合物；（b)使㈣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處理設備的 摻合物；⑷分館該原油產物；及蜮⑷使該原油產物 分顧成為—或多種餾分，並且由該至少-種顧分生產運輸 用燃料。 於若干具體實例中’本發明與結合本發明之一或多種 方或、.且成物者亦提供一種受载觸媒組成物，其：⑷在 每克載體中含有至少〇.3克或至少0.5克的Θ氧化鋁;(b)在 載&quot;體中包含δ氧化鋁；⑷在每克載體中含有最多〇1克的 °&quot;氧化銘，⑷具有中位孔徑至少為230人的孔徑分佈；（e) 具有該孔徑分佈之孔至少為0.3 cmVg或至少為0.7 CmVg 的孔體積;(f)具有至少6〇m2/g或至少9〇m2/g的表面積； (g)i〇包含週期表第7至1〇攔的-或多種金屬，週期表第7 至攔t或多種金屬的一或多種化合物，或其混合物； 43 200535224 (h)包含週期表第5 一或多種金屬的一 2、一或多種金屬，週期表第5欄之 克觸媒中含有0 00二多種化合物，或其混合物；⑴在每 多種第5攔金屬，二0二克或〇.001至〇·3克…或 物；⑴包含週期夺笛’ 7 4 5攔金屬化合物，或其混合 x第6攔的一或多 屬， 欄之-或多種金屬的 1夕種金屬㈣表弟6 每克觸媒中含有〇.〇〇 勿Ί“物，(k)在 或多種第6攔金屬，—或、&lt; 〇·001至〇.3克之：- 合物；⑴包含飢，1 L 6欄金屬化合物，或其混 ^ 或夕種釩化合物，或其混合物；（m)包 含鉬，一或多種鉬化合物， 或其混合物；（η)包含鎢，一 或夕種鎢化合物，或其混合物 化合物，或其混合物； （）一，-或夕種姑 或（Ρ)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-種原油組成物，纟：⑷具有最 多為1 ’最多為0.5 ’最多為0.3，或最多為〇」的ΤΑΝ ;⑻ 在每克組成物中含有至少〇·_克之沸程分佈在Q 1〇1奶 下介於95 C和260°C之間的烴；至少〇.〇〇1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26〇π 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克的驗性氮，（d)在每克組成物中含有至少 0.001克或至少0.01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 200535224 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18〇人， 最多為500 A，及/或在90至18〇 A，1〇〇至14〇人，12〇 至/30 A的孔徑分佈；（b)具有至少9〇人的中位孔徑，該 孔徑分佈中有超過6〇%的總孔數具有在45人、35人，或乃人 之中位孔徑範圍内的孔徑；⑷具有至少1〇〇…，至少 /§或至夕220 m2/g的表面積；（d)包含載體；該 載體包含氧化鋁、氧化矽、氧化矽_氧化鋁、氧化鈦、氧化 在口氧化鎮，/弗石，及/或其混合物；⑷&amp;含週期表第^ 至1〇攔的—或多種金屬，週期表第5至10欄之-或多種 金屬的-或多種化合物，或其混合物；⑴&amp;含週期表第5 欄的一或多種金屬，调如矣筮 蜀週期表第5攔之一或多種金屬的一 多種化合物，或其混合物；（g)在每克觸媒中含有至少 〇·0001克之：一或多種第5攔金屬，-或多種第5攔金屬 化合物’或其混合物’· (h)包含週期表第6欄的-或多種 金屬’週期表帛6欄之—或多種金屬的_或多種化合物， 或其混合物；⑴在每吞網丄甘士人 牡母見觸媒中含有至少〇 〇〇〇1克之一Next, it includes contacting the crude oil feed with one or more catalysts to produce a total product containing 3% of the crude oil product. The method further includes: making the crude oil product the same or different from the crude oil feed. Combine to form a Shishi transportation complex; (b) combine the emu oil product with crude oil that is the same or different from the crude feed to form a blend suitable for processing equipment; The crude product is divided into-or more fractions, and the fuel for transportation is produced from the at least-divided fractions. In several specific examples, the present invention and one or more of the present invention or a combination thereof, and the creator also provides a supported catalyst composition, which contains at least 0.3 grams or at least 0.5 g of Θ alumina; (b) δ alumina contained in the carrier; 含有 contains up to 0.01 g of 氧化 oxide per gram of carrier, ⑷ has a pore size with a median pore size of at least 230 people Distribution; (e) a pore volume having a pore size distribution of at least 0.3 cmVg or at least 0.7 CmVg; (f) a surface area of at least 60 m2 / g or at least 90 m2 / g; (g) iO contains One or more metals of the seventh to tenth periodic table of the periodic table, one or more compounds of t or more metals of the periodic table, or a mixture thereof; 43 200535224 (h) one of the five or more metals of the periodic table 2. One or more metals, the catalyst in column 5 of the periodic table contains more than 200 kinds of compounds, or mixtures thereof; ⑴ In each kind of 5th metal, 202 grams or 0.001 to 0.3 Gram ... or matter; ⑴ contains a period of flute '7 4 5 bar metal compounds, or a mixture of one or more genus of bar 6 or more The metal is a kind of metal, cousin 6 per gram of catalyst, and does not contain "," (k) in one or more of the sixth metal,-or, &lt; 0.001 to 0.3 grams: -Compounds; ⑴ contains hunger, 1 L 6 column metal compounds, or mixed or vanadium compounds, or mixtures thereof; (m) contains molybdenum, one or more molybdenum compounds, or mixtures thereof; (η) contains tungsten One or more tungsten compounds, or a mixture of compounds thereof, or a mixture thereof; () one,-or one or more species of nickel, or one or more nickel compounds, or a mixture thereof. In several specific examples, this Inventions and combinations of one or more of the methods or compositions of the present invention also provide a crude oil composition, 纟: ⑷ has a maximum of 1 ′, a maximum of 0.5 ′, a maximum of 0.3, or a maximum of 0 ″ TAN; ⑻ per gram The composition contains at least 0.00 g of hydrocarbons having a boiling range distribution between 95 C and 260 ° C under Q 100 milk; at least 0.0001 g, at least 0.05 g, or at least 0.01 Grams of boiling range distribution of hydrocarbons between 26〇π and 320 ° C at 0.11 MPa; and boiling range distribution of at least 0.001 grams Hydrocarbons between 320 ° C and 650 ° C at 0 001 Mpa; (c) contains at least 0.0005 g of nitrogen per gram of composition, (d) contains at least 0.005 g of gram of nitrogen per gram of composition 0.001 grams or at least 0.01 grams of total nitrogen; and / or (e) containing up to 0.00005 grams of total nickel and vanadium per gram of composition. 44 200535224 In some specific examples, the present invention and those who combine one or more methods or compositions of the present invention also provide a crude oil composition comprising one or more catalysts, the at least one catalyst ... (a) has a medium The pore size is at least 180 people, up to 500 A, and / or the pore size distribution is between 90 to 180 A, 100 to 140 people, and 120 to / 30 A; (b) having a pore size distribution of at least 90 people Median pore size, with more than 60% of the total number of pores in the pore size distribution having a pore size in the range of 45, 35, or the median pore size of a person; ⑷ having at least 100 ..., at least / § or up A surface area of 220 m2 / g; (d) including a carrier; the carrier comprising alumina, silica, silica-alumina, titania, oxidized oxidized oxidized oxidized sulfite, and / or fossil, and / or mixtures thereof; ⑷ &amp; Contains ^ to 10 of the periodic table-or more metals, columns 5 to 10 of the periodic table-or more metals-or more compounds, or mixtures thereof; ⑴ &amp; contains one or more metals of column 5 of the periodic table , A compound or compounds of one or more metals tuned to block 5 of the periodic table (G) Each gram of catalyst contains at least 0.0001 g of: one or more of the fifth metal,-or more of the fifth metal compound 'or a mixture thereof'. (H) contains column 6 of the periodic table-or Multi-metal 'Periodic Table Column 6-or more metals _ or compounds, or mixtures thereof; 含有 contains at least one 001 grams per gram of Gan Shiren Mumu catalyst per swallow net

或多種第6攔金屬’-或多種“攔金屬化合物，或复I 合物；⑴包含週期表第1G攔的—或多種金屬，週期= 1〇欄之一或多種金屬的-或多種化合物，或其混合物.及 /或㈨包含週期表第15欄的一或多種元素，週期表第b 欄之-或多種元素的一或多種化合物，或其混合物。 在進步的具體實例中，本發明之特定具體實例的特 45 200535224 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以。 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。 附加特徵可加入本文中所述 在進一步的具體實例中 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。 API比重係指在15 5 c (6〇卞）下的A?〗比重。'Η 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 彿程分佈係藉由ASTM法D5307測定。 “C5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欄金屬，，係指週期表第X攔的一或多種金屬及/ 或週期表第X攔之一或多種金屬的一或多種化合物，其中 X係對應於週期表的欄數（例如1至12)。舉例而言，“第6 搁金屬”係指週期表第6攔的一或多種金屬及/或週期表第 6欄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 200535224 /或週期表第x搁 中X係對應於週2 的一或多種化合物，其 15椚-去表的欄數（例如13至18)。舉例而言，“第 #兀素係指週期表第15攔 表第丨5攔之—或 次夕種凡素及/或週期 及夕種7G素的一或多種化合物。 在本申請案的範疇内’週期表的 金屬化合物重巧期表的 合物重量^二素重量，或週期表的元素化 — ’、、屬重篁或凡素重量計算。舉例而言，如果Or more of the sixth metal 'or more of the "metal metal compounds, or complexes; ⑴ containing one or more metals of the 1G of the periodic table, the period = one or more of the metals in column 10-or more compounds, Or a mixture thereof, and / or a compound or compounds comprising one or more elements in column 15 of the periodic table, or one or more elements in column b of the periodic table, or a mixture thereof. In a specific embodiment of the present invention, The characteristics of a specific specific example 45 200535224 may be combined with the characteristics of other specific examples of the present invention. For example, the characteristics of the specific examples of the present invention may be combined with the characteristics of other specific examples. In further specific examples, crude oil products may be borrowed Obtained by any of the methods and systems described in the text. Additional features can be added to specific specific examples described in further specific examples herein. [Embodiment] Specific specific examples of the invention are described in more detail herein. The terms used in this article are defined as follows. "ASTM" refers to the American Standard for Materials Testing. API specific gravity refers to the specific gravity of A? At 15 5 c (6〇 卞). 'Η Specific gravity Determined by ASTM method D6822. The percentage of atomic hydrogen and the percentage of atomic carbon of crude oil feeds and crude products are determined by ASTM method D5291. Unless otherwise stated, crude feed, total products, and / or Buddhist product distributions It is measured by ASTM method D5307. "C5 asphaltene" means asphaltene which is insoluble in pentane. The C5 asphaltene content is determined by ASTM method D2007. "Column X metal means one or more metals of the X-block of the periodic table and / or one or more compounds of one or more metals of the X-block of the periodic table, where X is the number of columns in the periodic table (for example 1 to 12). For example, "sixth metal" refers to one or more metals in column 6 of the periodic table and / or one or more compounds of one or more metals in column 6 of the periodic table. '' X Block element, refers to one or more elements of the X-block of the periodic table, and 46 200535224 / or x-table of the periodic table, X is one or more compounds corresponding to week 2, its 15 椚 -the number of columns in the table ( For example, 13 to 18). For example, "## 素 means the one or more compounds of the 15th and 5th of the periodic table—or the next and the 7G hormones of the periodic table. Within the scope of this application, the weight of the metal compound of the periodic table is the weight of the compound of the periodic table, the weight of the two primes, or the elementalization of the periodic table-', which is the weight of 篁 or the weight of ordinary elements. For example, if

母克觸媒使用(Μ克的Μο〇3,則該觸媒中翻金屬的計算重 量為每克觸媒0.067克。 “含量’’係指以基質總重量計表示成重量分率或重量百 分率=基質（例如原油進料、總產物，或原油產物）中的成 分重量。“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。 館分係指沸程分佈在〇· 101 MPa下介於204°c (400 T)和343°C (650T)之間的烴。餾分含量係藉由ASTM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E385，對於總氮的 D5 762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。 47 200535224 ^源可包括，但不限於烴（例如Ci至C4的烴，如甲烷、乙 ^丙烧、丁烧）、水’或其混合物。可進行質量均衡以估 计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。平板抗 碎強度係藉由ASTM法D4179測定。 几 LHSV”係指體積液體進料速率/觸媒總體積，其係以 小時（hr1)表示。觸媒總體積係藉由總和接觸區中的;有觸 媒體積來計算，如本文中所述者。 “液態混合物”係指包含在標準溫度和壓力（25。。，〇 MPa，後文稱為“STP，，）下為液態之—或多種化合物的組成 物，或是包含在STP下為液態的一或多種化合物與在STP 下為固怨的一或多種化合物之組合的組成物。 週期表係指2003年11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、 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。 微殘留奴（“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 200535224The mother gram catalyst is used (Mg of Mο〇3, the calculated weight of the metal in the catalyst is 0.067 grams per gram of catalyst. "Content" refers to the weight percentage or weight percentage based on the total weight of the substrate = The weight of ingredients in the matrix (such as crude feed, total product, or crude product). "Wtppm" means parts per million by weight. "Crude feed / total product mixture, means Mixtures contacted by catalysts. Inventory refers to hydrocarbons with a boiling range distribution between 204 ° C (400 T) and 343 ° C (650T) at 0.1101 MPa. The fraction content is determined by ASTM method D5307. "Heteroatom" means oxygen, nitrogen, and / or sulfur contained in the molecular structure of a hydrocarbon. Heteroatom content is determined by ASTM method for E385 for oxygen, D5 762 for total nitrogen, and D4294 for sulfur. "Base "Total nitrogen" refers to nitrogen compounds with a pKa of less than 40. Basic nitrogen ("bn") is determined by ASTM method D2896. "Hydrogen source" refers to hydrogen and / or compounds and / or when crude oil is added. Compounds that react in the presence of catalysts and catalysts to provide hydrogen to compounds in the crude feed. 47 200535 The source may include, but is not limited to, hydrocarbons (such as Ci to C4 hydrocarbons, such as methane, ethylene, styrene, butane), water, or mixtures thereof. Mass balance can be performed to estimate the amount of compounds in the crude feed The amount of net hydrogen provided. "Flat crushing strength" refers to the compressive force required to crush the catalyst. Flat crushing strength is determined by ASTM method D4179. A few LHSV "refers to the volume liquid feed rate / total catalyst Volume, which is expressed in hours (hr1). The total volume of the catalyst is calculated by summing the contact volume in the contact area, as described herein. "Liquid mixture" means included at standard temperature and pressure (25., 0MPa, hereinafter referred to as "STP,") is a composition of a liquid or a plurality of compounds, or a composition containing one or more compounds that are liquid under the STP and solid complaints under the STP A composition of one or more compounds. The periodic table refers to the periodic table specified by the International Union of Pure and Applied Chemistry (IUPAC) in November 2003. "Metals in the form of metal salts of organic acids refer to alkali metals, Alkaline earth metals, zinc, arsenic, chromium, or The metal content in the form of a metal salt of an organic acid is determined by ASTM method D1318. The micro-residual slave ("MCR") content refers to the amount of residual carbon left after evaporation and pyrolysis of the matrix. The MCR content is determined by the ASTM method Determined by D4530. "Naphtha" refers to hydrocarbon components with a boiling range distribution between 〇01 MPa and 38 ° C (100 ° F) and 200 ° C (392 ° F). Naphtha content Measured by ASTM method D5307. "Ni / V / Fe" means nickel, vanadium, iron, or a combination thereof. "Ni / V / Fe content" means the content of nickel, vanadium, iron, or a combination thereof. 48 200535224

Ni/V/Fe含量係藉由ASTM法D5708測定。 “Nm3/m3”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（一C〇2-)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值的測疋係由j· j· Heithaus見述於wrna/ (9/ Institute of Petroleum, V〇l. 48, Number 4585 February 1962, pp. 45-33 的 Measurement and Significance of AsphalteneThe Ni / V / Fe content is measured by ASTM method D5708. "Nm3 / m3" means standard cubic meters of gas per cubic meter of crude oil feed. "A non-carboxylic acid-containing organic oxygen compound refers to an organic oxygen compound that does not contain a carboxyl group (-CO2-). 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. "Non-condensable gas" means a gaseous component 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 the crude oil feed. The measurement of the P value is described by j. J. Heithaus in wrna / (9 / Institute of Petroleum, V. 48, Number 4585 February 1962, pp. 45-33 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® A922〇 儀器（Micr〇meritics Inc·’ Noixfoss Georgia，u.s a )可用來測定這些值。 殘留物係指具有沸程分佈高於538它（1〇〇〇。厂）的 成分，如ASTM法D5307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 )表不。TAN係藉由ASTM法D664測定。 VGO係指沸程分佈在〇 1〇l 下介於Μ)（65〇 49 200535224 T)和538 t (1000 T)之間的烴。VG〇含量係藉由—Μ 法D5307測定。 “黏度”係指在37.8 °C (100 °F)下的動黏度。黏度係 利用ASTM法D445測定。 在本申言青案的情況T，應瞭解如丨已試驗基質之性質 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。 原油可生產及/或乾餾自含有構造物的烴接著使其穩定 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⑼及/或分館以 生產具有特定沸程分佈（例如石腦油、餾分、VG0，及/ ::滑:由)的多成分：蒸德包括，但不限於常壓蒸館法及/或 ’壓瘵餾法。未瘵餾及/或未分餾的穩定原油在每克原、、由中 ?上包含數量至” 0.5克的成分之碳數大於4的成分。 疋原油的實例包括全原油、基 — 4餘原油、脫鹽原油、脫_ 洛餘原油’或其組合。“墓餘”孫 …餘係指已處理過的原油， 已移除至少一部分具有沸點在〇 •iU1 MPa 下低於 35t 1 —下為95T)的成分。典 (在 原油中具有含量最多為。.丨克，最多為：:由在母 Λ ± 兄蚨夕為0·〇5克，或最多Α 0·02克的這類成分。 马 若干穩定原油具有可容許稃定 “疋原/由藉由輸送載具（例如 50 200535224 管線、卡車，或船舶）輸送至習知處理設備的性質。其他原 油具有一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、輪送及/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0.3的TAN; b)至少10 cSt的黏度；c)最多為19的API 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0.0001克的Ni/V/Fe ; e)雜原子總含量為每克原_ 油中至少有0.005克的雜原子；f)《留物含量為每克原油 中至少有ο·οι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 〇·2克的殘留物’至少〇·3克的殘留物，至少〇·5克的殘留 物’或至少、0.9克的殘留物。於若干具體實例中，劣質原鲁 油可能具有在0.1或〇·3至2〇，〇·3或〇 5至1〇，或〇·4或 〇·5至5之範圍内的ΤΑΝ。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〇 〇〇5克，至少〇 〇1克， 或至少0.02克的硫含量。 於右干具體實例中，劣質原油具有包括，但不限於下 列的性質· a)至少〇·5 # Tan ; b)含氧量為每克原油進 料至4有G·’克的氧；e) ^瀝青f含量為每克原油進料 51 200535224 中至少有請克的（：5瀝青質；d) A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&gt; 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\ 克的金屬；或f)其組合。 劣質原油在每克劣質原油中可包含··至少〇〇〇1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90°c和20(Tc之間的烴；至少0·01克，至少〇 〇〇5克， 或至少0_001克之沸程分佈在O.lOi MPa下介於2〇(rc和3〇〇 °C之間的烴；至少0.001克，至少0.005克，或至少〇 〇1 克之彿程分佈在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，或至少〇·〇ι克之彿 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o.ioi MPa下 最多為100°C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100°C和200°C之間 的烴；至少0.001克，至少〇_〇〇5克，或至少0.01克之沸 程分佈在0.101 MPa下介於200°C和3 00°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；及至少〇·001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。 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0·005克，或至少0·01 52 200535224 克之沸程分佈在0.101 MPa下最多為i〇(rc的烴。典型而 言，劣質原油在每克劣質原油中具有最多為〇.2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克之沸程分佈在〇1〇1 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，或至少〇·〇ι克之沸程分佈至少為65〇 °C的烴。 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· Guif coast和 southern California、Canada Tar sands、Brazilian Santos and Campos basins、Egyptian Gulf of Suez、Chad、United Kingdom North Sea、Angola Offshore、Chinese Bohai Bay、"Peptization." "Aperture", "median pore size" and "pore volume" refer to the pore size, median pore size, and pore volume determined by ASTM method D4284 (mercury porosity method with a contact angle of 140). A micromeritics® A922〇 instrument (Micrômeritics Inc. 'Noixfoss Georgia, us a) can be used to determine these values. Residues refer to components with a boiling range distribution above 538 (1000. plant), such as the ASTM method Measured by D5307. SCFB refers to the standard cubic feet of gas in a barrel of crude oil feed. The surface area of the catalyst is determined by ASTM method D3663. TAN means that the total acid number 'is 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 0.001) (65049 200535224 T) and 538 t (1000 T). The VG0 content was determined by -M method D5307. "Viscosity" refers to the dynamic viscosity at 37.8 ° C (100 ° F). Viscosity is measured by ASTM method D445. In case T of this proposal, it should be understood that if the value of the properties of the tested substrate is outside the limits of the test method, the test method may be modified and / or recalibrated to test such properties. Crude oil can be produced and / or carbonized from hydrocarbons containing structures and 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 typically have not been lumped in processing facilities and / or branches to produce multi-components with specific boiling range distributions (eg, naphtha, distillates, VG0, and / :: slip: origin): steaming includes, but does not It is limited to the atmospheric distillation method and / or the 'autoclaving method. Undecreased and / or unfractionated stable crude oil contains components with a carbon number greater than 4 per gram of raw material, from middle to large, to 0.5 g. Examples of 疋 crude oil include whole crude oil, base-4 crude oil , Desalted crude oil, De_Luoyu crude oil 'or a combination thereof. "Tomb Yu" grandson ... Yu refers to processed crude oil, at least a part of which has been removed and has a boiling point below 35 t 1 at 95 U 1 MPa — 95 T below ) Ingredients. Code (the content in crude oil is up to .. g, at most :: from the mother Λ ± brother Xixi is 0. 05 grams, or at most A 0. 02 grams of such ingredients. Horse Some stable crude oils have properties that allow for the definition of "Karahara / delivery by transport vehicles (such as 50 200535224 pipelines, trucks, or ships) to conventional processing equipment. Other crude oils have one or more unfavorable disadvantages Appropriate nature. Inferior crude oil may be unacceptable for transportation vehicles and / or processing equipment, and therefore will give low economic value to the inferior crude oil. This economic value may be like the production and rotation of containers that are considered to contain inferior crude oil And / or processing costs are too The properties of inferior crude oil may include, but are not limited to: a) a TAN of at least 0, at least 0.3; b) a viscosity of at least 10 cSt; c) an API gravity of at most 19; d) total Ni / V / Fe The content is at least 20000 grams or at least 0.0001 grams of Ni / V / Fe per gram of crude oil; e) the total content of heteroatoms is at least 0.005 grams of heteroatoms per gram of crude oil; f) "Residue content is at least ο · οι grams of residue per gram of crude oil; g) c5 asphaltene content is at least 0.04 grams of C5 asphaltene per gram of crude oil; h) MCR content is at least MCR of 0.002 grams; i) metal content in the form of a metal salt of an organic acid is at least 0.0001 grams of metal per gram of crude oil; or ") a combination thereof. In several specific examples, inferior and inferior crude oil may contain at least 0.2 grams of residue 'at least 0.3 grams of residue, at least 0.5 grams of residue' or at least 0.9 grams per gram of inferior crude oil. Residues. In several specific examples, inferior raw lube oil may have a TAN in the range of 0.1 or 0.3 to 20, 0.3 or 0.5 to 10, or 0.4 or 0.5 to 5. In certain specific examples, inferior crude oil may have a sulfur content of at least 0.05 g, at least 0.01 g, or at least 0.02 g per gram of inferior crude oil. In the specific example of the right dry, inferior crude oil has the properties including, but not limited to the following: a) at least 0.5 # Tan; b) oxygen content is 4 G · 'g of oxygen per gram of crude oil feed; e ) ^ Bitumen f content is at least 5 grams of (: 5 asphaltenes) per gram of crude oil feed 51 200535224; d) A is at the desired viscosity (for example, for crude oil feeds with an API specific gravity of at least 10) &gt; 1 O cst); e) the metal content of the metal salt in the form of an organic acid is at least 20000 g of metal per gram of crude oil; or f) a combination thereof. Inferior crude oil may contain at least 0.0001 grams, at least 0.005 grams, or at least 0.01 grams of boiling range per gram of inferior crude oil between 90 ° C and 20 (Tc) at 0.001 Mpa Hydrocarbons; at least 0.01 grams, at least 0.05 grams, or at least 0-001 grams, hydrocarbons with a boiling range distribution between 0.10 MPa and 300 ° C at 0.1 MPa; at least 0.001 grams, At least 0.005 grams, or at least 0.001 grams of Buddha Cheng distribution hydrocarbons between 300 ° C and 400 ° C at 0.101 MPa; and at least 0.001 grams, at least 0.005 grams, or at least 0.005 grams of Buddha Cheng distribution Hydrocarbons between 400 ° C and 650 ° C at 0-101 MPa. 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 boiling range distribution at o.ioi MPa Hydrocarbons up to 100 ° C; at least 0.001 grams, at least 0.005 grams, or at least 0.001 grams of hydrocarbons with a boiling range distribution between 0.1 ° C and 200 ° C at 0.101 MPa; at least 0.001 grams, at least 〇 _〇05 grams, or at least 0.01 grams of hydrocarbons with a boiling range distribution between 200 ° C and 300 ° C at 0.101 MPa; at least 0.001 grams, at least 0.005 grams, or at least 〇1 grams of hydrocarbons with a boiling range distribution between 300 ° C and 400 ° C at 0 · 101 MPa; and at least 0.001 grams, at least 0.005 grams, or at least 0.01 grams of boiling range distribution at 0 · 101 MPa Hydrocarbons between 400 ° C and 650 ° C. In addition to higher boiling point components, several inferior crudes may contain at least 0.001 grams, at least 0.005 grams, or at least 0.01 52 200535224 grams of hydrocarbons with a boiling range distribution of up to 0.10 MPa at 0.101 MPa. Typically, inferior crudes have a content of such hydrocarbons of at most 0.2 g or at most 0.1 g per gram of inferior crude. Certain inferior crude oils 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 010 MPa per gram of inferior crude oils. Crude oil may contain at least 0 001 grams, at least 0.005 grams, or at least 0.005 grams of hydrocarbons with a boiling range distribution of at least 65 ° C. Examples of inferior crude oils that can be treated using the methods described herein include, but are not limited to, derived from Crude oil in the following regions of the world: us · Guif 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 Ind〇nesia 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。 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。故類原油產物可用較少或不用預處理精煉，藉此提高 53 200535224 和煉效率。預處理可包括脫硫、脫金屬及/或常壓蒸顧以移 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，原油進料的至少一種性質與該原油進料的同樣性質相 比可藉由忒原油進料與一或多種觸媒的接觸而改變。於若 干具體實例中，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 物提供相當少量氳的一或多種烴。 圖1為接觸系統1 〇〇的簡圖，其包含接觸區1 〇2。原 油進料經由導管104進入接觸區1〇2。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、噴霧反應 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1 〇 〇中，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 200535224 料的同樣性質相 比會改變至少 10% 〇 _ ^特疋具體實例中，接觸區中的觸媒體積在1〇至6〇 體積/° ’ 2G至5G體積％，或3G至4G體積％之接觸區中原 油進料總體積的銘m 、耗圍内。於若干具體實例中，觸媒和原油 進料的漿液在接p 在接觸£的母1〇〇克原油進料中可包含〇 〇〇1 至 1〇 克，〇 〇〇s 吞 &lt;：士 U5至5克，或〇·〇ι至3克的觸媒。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 obtained by processing crude oil feeds as described herein are generally suitable for transporting and / or processing crude oil products produced as described herein that have properties that are closer to the corresponding properties of West Texas Intermediate crude oil than crude oil feeds, or Crude oil feed is closer to the corresponding properties of Brent crude oil, thereby increasing the economic value of crude oil feed. Therefore, crude oil products can be refined with less or no pretreatment, thereby improving 53 200535224 and refining efficiency. Pretreatment may include desulfurization, demetallization, and / or atmospheric distillation to remove impurities. 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 crude oil feed compared to the same property of the crude oil feed can be changed by contacting the rhenium crude oil feed with one or more catalysts. In several specific examples, the contacting is performed in the presence of a hydrogen source. In several specific examples, the &apos; hydrogen source provides one or more hydrocarbons in a relatively small amount of tritium to compounds in the crude oil feed for reaction under specific contact conditions. FIG. 1 is a simplified diagram of a contact system 100, which includes a contact area 100. The crude oil feed enters the contact zone 102 via a 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 specific gravity, or these properties of the crude oil feed after contacting the crude oil feed with one or more catalysts. The combination will change at least 10% compared with the same properties of the crude oil feed 54 200535224. In the specific example, the contact area in the contact area is between 10 and 60 vol / ° '2G to 5G vol%, Or within 3 m to 4 G vol% of the contact zone, the total volume of crude oil feed volume is within m. In several specific examples, the slurry of the catalyst and the crude oil feed may contain 0.001 to 10 grams in the parent 100 grams of crude oil feed contacted with the 100,000 s. U5 to 5 grams, or 0.003 to 3 grams of catalyst.

^接觸區中的接觸條件可包括，但不限於溫度、壓力、 皇，、動原’由進料流動，或其組合。控制若干具體實例 、蜀條件以生產具有特性的原油產物。接觸區中的溫 又可刀佈在50至500。。，6〇至44〇。。，7〇至43〇。。，或8〇 至420 C的範圍。接觸區中的壓力可分佈在〇·ι至川MPa， 至12 MPa ’ 4至10 MPa，或6至8 MPa的範圍。原油進 料的LHSV通常分佈在〇·1至30 h·1，0.5至25 h·1，1至20 h ，I·5至15 h·1，或2至1〇 h·!的範圍。於若干具體實例 中LHSV至少為5 h-i，至少為n h-1，至少為15匕“，或 至少為20 hr1。^ The contact conditions in the contact zone may include, but are not limited to, temperature, pressure, temperature, motive force 'flowing from the feed, or a combination thereof. Several specific examples and conditions of Shu are controlled to produce characteristic crude oil products. The temperature in the contact area can be between 50 and 500. . , 60 to 44. . , 70 to 43. . , Or the range of 80 to 420 C. The pressure in the contact zone can be distributed in the range of 0. to MPa, to 12 MPa '4 to 10 MPa, or 6 to 8 MPa. The LHSV of the crude feed is usually distributed in the range of 0.1 to 30 h · 1, 0.5 to 25 h · 1, 1 to 20 h, 1.5 to 15 h · 1, or 2 to 10 h · !. In several specific examples, the LHSV is at least 5 h-i, at least n h-1, at least 15 d ", or at least 20 hr1.

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〇1至1〇〇,〇〇〇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 between 001 and 100,000.

Nm /m ’ 〇·5 至 l〇,〇〇〇 Nm3/m3, 1 至 8,000 Nm3/m3,2 至 5,000 Nm /m，5 至 3,000 Nm3/m3，或 1〇 至 8〇〇 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 虱。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 200535224 實例中，氫源（例如氫、曱烷或乙烷）可用來作為載送氣體 並且再循環通過接觸區。 氫源可與導管1 〇4中的原油進料並流或經由導管1 分別進入接觸區102。於接觸區102中，原油進料與觸媒 的接觸係產生含有原油產物，而在若干具體實例中含有氣 體的總產物。於若干具體實例中，載送氣體係與原油進料 及/或在導管106中與氫源結合。總產物可離開接觸區1〇2 經由導管110進入分離區108。 於分離區1 08中，原油產物和氣體可使用一般已知的 分離技術，例如氣-液分離，自總產物分離。原油產物可經 由導管112離開分離區108，接著輸送到輸送載具、管線、 儲存容器、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 氧化碳）、過量氣態氫源，及/或載送氣體。過量氣體可再 循環至接觸系統1〇〇，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^ 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丨之 具體實例的簡圖。在圖2八和2B中，接觸系统1〇〇包含接 觸區102和1丨4。圖3A和3B包含。接觸區1〇2、ii4、u6。 在圖2A和3A中，接觸㊣1〇2、114、⑴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1〇4進入接 56 200535224 觸區1 0 2。 於若干具體實例中’載送氣體在導管106中與氫源結 合並且以混合物的形式導人接觸區。於特定具體實例中， 士圖1 3A和3B所示者，氫源及/或載送氣體可經由導管 H)6及/或經由如導管1〇6，以原油進料流動相反的方向，與 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。Nm / m '0.5 to 10,000,000 Nm3 / m3, 1 to 8,000 Nm3 / m3, 2 to 5,000 Nm / m, 5 to 3,000 Nm3 / m3, or 10 to 800 Nm3 / m3 and The range of catalyst contact. 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 lice. The carrier gas can promote crude oil feed flow and / or hydrogen source flow in the contact zone. The carrier gas can also enhance mixing in the contact zone. In a number of specific 55 200535224 examples, a source of hydrogen (such as hydrogen, pinane, or ethane) can be used as a carrier gas and recycled through the contact zone. The hydrogen source may enter the contact zone 102 in parallel with the crude oil feed in the conduit 104 or via the conduit 1 respectively. In the contact zone 102, the contact of the crude oil feed with the catalyst produces a total product containing crude oil products, and in some specific examples gas. In several specific examples, the carrier gas system is combined with a crude oil feed and / or a hydrogen source in a conduit 106. The total product can leave the contact zone 102 and enter the separation zone 108 via the conduit 110. In the separation zone 108, crude oil products and gases can be separated from the total product using generally known separation techniques, such as gas-liquid separation. The crude product may leave the separation zone 108 via a conduit 112 and then be transported to a transport vehicle, pipeline, storage container, refinery, other processing zone, or a combination thereof. Gases may include gases generated during processing (e.g., hydrogen sulfide, carbon dioxide, and / or carbon monoxide), sources of excess gaseous hydrogen, and / or carrier gases. Excess gas can be recycled to the contact system 100, purified, and transferred to other processing areas, storage vessels, 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 contact systems including two or three contact areas. In FIGS. 2A and 2B, the contact system 100 includes contact areas 102 and 11-4. Figures 3A and 3B contain. Contact area 102, ii4, u6. In Figures 2A and 3A, the contacts ㊣102, 114, and ⑴ are depicted as individual contact areas in a reactor. The crude oil feed is connected to the contact zone 102 through the conduit 104. In several embodiments, the &apos; carrier gas is combined with a hydrogen source in the conduit 106 and directed into the contact area as a mixture. In certain specific examples, as shown in Figures 13A and 3B, the hydrogen source and / or carrier gas may be passed through the pipeline PD6 and / or via conduit 106, in the opposite direction of the crude oil feed flow, and Crude oil feeds each enter one or more contact zones. Addition of a hydrogen source and / or carrier gas in reverse to the flow of the crude oil feed can improve the mixing and / or contact of the crude oil feed with the catalyst.

在接駭102巾，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3A和 3B中，原料流係由接觸區n4流到接觸區116。At 102, the contact of the crude feed with the catalyst will generate a raw material stream. This raw material stream flows from the contact zone 102 to the contact zone 114. In Figures 3A and 3B, the feed stream flows from the contact zone n4 to the contact zone 116.

接觸區1〇2、&quot;4、116可包含-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1 14如3B所*，原料流係經由導管離開 114而進入接觸區116。The contact areas 102, &quot; 4, 116 may contain-or multiple catalysts. As shown in FIG. 2B, the raw material stream leaves the contact area 102 through the conduit 118 and enters the contact area 114 as shown in FIG. 3B. The raw material stream enters the contact area 116 through the conduit exit 114.

，、；、μ可在接觸區114及/或接觸區116與附加觸: 觸以生成總產物。總產物離開接觸區U4及，或接觸區 、、二由導&amp; 110進入分離區1〇8。原油產物及/或氣體係 自總產物。原油產物係經由導管ιΐ2離開分離區1〇8。 圖4為刀離區在接觸系統⑽上游之具體實例的簡| 劣質原油（蒸餘或非蒸餘者）係經由導管122進入分i 120。在分㈣m中，至少-部分的劣質原油係使] 項技術中已知的技術（例如喷佈、薄膜分離、減壓⑷ 生產原油進料。舉例而言，水可從劣質原油中至少部 57 200535224 離。於另一實例中，呈古、並,,;, Μ may be contacted with additional contact in the contact region 114 and / or the contact region 116 to generate a total product. The total product leaves the contacting zone U4 and, or the contacting zone &amp; 110, and enters the separation zone 108. Crude products and / or gas systems from total products. The crude product leaves the separation zone 108 via a conduit 2m. FIG. 4 is a simplified example of a specific example of the knife-off region upstream of the contact system. Inferior crude oil (distilled or non-distilled) enters the sub-i 120 through the conduit 122. In the tiller m, at least-part of the inferior crude oil is used in the technologies known in the art (such as spraying, membrane separation, decompression, production of crude oil feed. 200535224 Li. In another example, Chenggu, and

具有/弗程分佈低於95°C或低於i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 右干具體實例[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f原油中分離。於若干具體實例中， 至少-部分經過分離的成分係經由導t 124_開分離區 120° 由分離區 12 〇所j呈；丨^ 斤侍到的原油進料於若干具體實例中係 包含沸程分佈至少^⑽。c，或於若干具體實例中，沸程 分佈至”⑽之成分的混合物。典型而言，經過分離 的原油進料包含彿程分佈介於1GG至咖t，12G至_ C或200至800 c之成分的混合物。至少一部分的原油 、；斗纟導g 126離開分離區12〇進入接觸系統ι〇〇 (參見 々圖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12G可位於脫鹽單元的上游或下游。 處理之:灸，原油產物係經由導管112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。舉例而纟，原油產物可與具有不同黏度的 、 口藉此產生具有黏度介於該原油產物黏度與該原 ^ # n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/、忒原油TAN之間的產品。此摻合產品可適用於輸送 及/或處理。 —士圖5所不，於特定具體實例中，原油進料係經由導 管104進入接觸系統100,而至少一部分的原油產物經由 58 200535224Ingredients with a / Fr Cheng range below 95 ° C or below 1000 ° C can be at least partially separated from inferior crude oil to produce a crude feed. Yu Yougan Specific Example [At least a portion of naphtha and compounds that are more volatile than naphtha are separated from crude oil. In some specific examples, the at least-part of the separated components are presented by the separation zone 120 ° through the conduction zone 124 ° and the separation zone 120 °; ^^ The crude oil feed received by Jin Jin contains boiling in some specific examples. The process distribution is at least ^ ⑽. c, or in several specific examples, a mixture of components whose boiling range is distributed to "⑽". Typically, the separated crude oil feed contains a fossil distribution ranging from 1GG to 24C, 12G to _C, or 200 to 800c A mixture of components. At least a portion of the crude oil; 纟 g 126 leaves the separation zone 120 and enters the contact system ιOO (see the contact zone in Figures 1 to 3) for further processing to produce crude oil products. In several specific examples In the separation zone, 12G can be located upstream or downstream of the desalination unit. Treatment: moxibustion, crude oil products leave the contact system 100 through the conduit 112. In several specific examples, the crude oil product and the crude oil feed are the same or different. Blending. By way of example, crude oil products can have different viscosities to produce blended products with viscosities between the viscosity of the crude oil product and the original ^ # n. In another example, the raw and oil products can be blended. Blended with crude oils with different TANs, thereby producing a product with a TAN between the crude oil product and the rhenium crude oil TAN. This blended product can be suitable for transportation and / or processing.-Figure 5 does not apply to specific In a specific example, the crude oil feed enters the contact system 100 via a conduit 104, and at least a portion of the crude product passes through 58 200535224

導管128離開接觸系統100導入摻合區13〇。於摻合區13〇 中，使至少一部刀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13〇或這類摻合區的上游。混合系統可位於或接 近摻合區13G。摻合產品可符合精煉廠及/或輸送載具所指 疋的產品規格。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i34 離開摻合區1 30以進行輸送或處理。 在圖6中，劣質原油係通過導管122進入分離區 如先前所述使劣質原油分離以生成原油進料。原油進料去 著通過導f丨26進人接觸系統⑽。該劣f原油的至少逢 干成分係經由導管124離開分離區12〇。至少一部分的為 油產物係經由導管128離開接觸系統1〇〇進入摻合區The catheter 128 exits the contact system 100 into the blending zone 130. In the blending zone 13, 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 oil feed Materials, or mixtures thereof, to produce a blended product. The industrial production stream, crude oil feed, crude oil, or a mixture thereof is directed via a conduit 32 to the blending zone 130 or upstream of such a blending zone. The mixing system can be located at or near the blending zone 13G. The blended product may meet the product specifications of the refining plant and / or transport vehicle. 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 blending zone 1 30 for delivery or processing via conduit i34. In Figure 6, inferior crude oil is introduced into the separation zone through conduit 122. The inferior crude oil is separated to produce a crude feed as previously described. Crude oil is fed into the contact system through the guide f 丨 26. At least the dry component of the crude oil leaves the separation zone 120 via the conduit 124. At least a portion of the oil product leaves the contact system 100 through the conduit 128 and enters the blending zone.

其他工業生產液流及/或原油係直接或經由導管132進入赛 合區130與原油產物結合生成換合產品。摻合產品係經: 導管134離開摻合區13〇。 、= “ 體實例中，原油產物及/或摻合產品係輪送到 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㈣料、冑滑油或化 學品。加工可包括蒸餾及/或分館原油產物及/或摻人產口 以產，—或多_分。於㈠具體實例中，原油產:、: 合產扣，及/或一或多種餾分可加氫處理。 59 200535224 於若干具體實例中，原油產物具有TAN最多為9〇%， 最多為50%，最多為3〇%，或最多&amp; 1〇%之原油進料的 TAN。於若干具體實例中，原油產物具有TAN在丄至， 20至70%，30至60%，或4〇至5〇%之原油進料的tan之 範圍内。於特定具體實例中，原油產物具有最多為丨，最 多為0.5，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o.ool。於若干具體實例中，原油產物的ταν 可在0.001至0.5，〇·01至〇 2 ,或〇 〇5至〇丨的範圍内。 於若干具體實例中，原油產物具有總Ni/V/Fe含量最 多為90%，最多為50%，最多為1〇%，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 體貫例中具有總Ni/V/Fe含量在1至80%，10至70〇/〇，2〇 至60〇/〇,或30至50%之原油進料的Ni/V/Fe含量之範圍内。 於特疋具體實例中，原油產物在每克原油產物中具有在丄X W-7 克至 5 X 10-5 克，3 x 10-7 克至 2 χ 1〇-5 克，或 i χ 1〇_6 克至1 X 1〇-5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 體實例中，原油產物的總Ni/V/Fe含量為70至130%，80 至DO%或90至110%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5〇%，最多為1〇%，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 200535224 屬總含量在丨至80%，10至70%，2〇至6〇%，或3〇至5〇% 之原油進料中有機酸金屬鹽形態的金屬總含量之範圍内。 系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、 非酸和苯甲酸。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 鋅和鎘），第15欄金屬（例如砷），第6欄金屬（例如鉻），或 其混合物。 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中有 〇·00000〇ι 克至 0.00005 克，0.0000003 克至 0·00002 克， 或0.000001克至0·00001克的有機酸金屬鹽形態之金屬的 耗圍内。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%，80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。 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 120%，9〇至11〇%，或1〇〇至13〇%之原油進料的AH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9〇%， 最多為80〇/。，或最多為70%之原油進料的黏度。於若干具 體實例中，原油產物具有黏度在1〇至6〇%，2〇至5〇%， 或30至40%之原油進料的黏度之範圍内。於若干具體實 61 200535224 … 的4度最多為90%之原心 時此原油產物的API比重為7〇至13〇% 的黏度，同 90至11〇%之原油進料的Αρι比重。 至120%，或 於若干具體實例中，原油產物具 為9〇%，最多為50%，最多為1〇%，或厂里取夕 進料的雜原子總含量。於特定具體實例中，原、由2原油 雜原子總含量至少為1%，至少為3〇% 、為具有 至乂為99/。之原油進料的雜原子總含量。 於若干具體實财1油產物 ，最多為50%，最多為1〇%，或;了-最多為 的含硫量。於特定且體f ”、、。之原油產物 為1〇/，m 中’原油產物具有含硫量至少 進料的A;/曰Μ/”至少為80%，或至少為99%之原油 進料的3硫置。於若千且縣每 7〇至胸’⑼至丨游… 原油產物的含硫量為 硫量。 7°’或之原油進料的含 9〇。/，最ΓΑ、f實例中，原油產物的總含氮量可能最多為 二;;::，多為⑽，或最 至;:二。/特疋具體實例中，原油產物具有總含氮量 历 至少為3〇%，至少為8〇%，或至少$ 99%之 原油進料的總含氮量。 為JTt具體實例中’原油產物的驗性氮含量可能最多 ::/°，表多她’最多為爆最多為10%，或最多 :之原油進料的驗性氮含量。於特定具體 油產物具有驗性氮含量至少$ 1%，至少為鄕，至少= 62 200535224 80/〇 ’ 或至少 $ 99〇/ 於若干具體實例中進料的驗性氮含量。 90¾，最多為5〇0/ π ，原油產物的含氧量可能最多為 象原油進料的：氧？為3〇%，最多為㈣，或最多為 有含氧量至少ΑS於特定具體實例中，原油產物具 為99%之原油進 ‘、、二至少為8〇%’或至少 物的含氧量在於右干具體實例中’原油產 5〇0/之 W 8〇/〇 ’ 10 至 70%，20 至 6〇%，或 3〇 至Other industrial production fluids and / or crude oil enter the Saihe District 130 directly or via the conduit 132 to combine with crude oil products to produce swap products. The blended product passes through: the conduit 134 leaves the blending zone 130. , = "In the example, crude oil products and / or blended products are delivered to refineries and / or processing equipment. Crude oil products and / or blended products can be processed to produce industrial products such as transportation fuels and heating fuel , 或 oil or chemicals. Processing may include distillation and / or branch crude oil products and / or blended into the production port to produce, or more _ points. In the specific example of ㈠, crude oil production:,: combined production deduction, and / Or one or more fractions can be hydrotreated. 59 200535224 In some specific examples, crude oil products have a TAN of at most 90%, at most 50%, at most 30%, or at most & 10% of crude oil feed. In certain specific examples, the crude oil product has a TAN in the range of 20 to 70%, 30 to 60%, or 40 to 50% of the tan of the crude oil feed. In specific specific examples The crude oil product has a TAN of at most 丨, at most 0.5, at most 0.3, at most 0.2, at most 01, or at most 0.005. The TAN of the crude product is usually at least 0.0000. ι, more commonly, at least o.ool. In several specific examples, ταν of crude oil products can be In the range of 0.001 to 0.5, 0.001 to 〇2, or 005 to 〇 丨. In several specific examples, the crude oil product has a total Ni / V / Fe content of at most 90%, at most 50%, and at most The Ni / V / Fe content of the crude oil feed is 10%, at most 5%, or at most 3%. This crude product has a total Ni / V / Fe content of 1 to 80% in several specific examples, 10 to 70/0, 20 to 60/0, or 30 to 50% of the Ni / V / Fe content of the crude oil feed. In the specific example of the crude oil, the crude oil product is in each gram of crude oil product. Has a range of 丄 X W-7 grams to 5 X 10-5 grams, 3 x 10-7 grams to 2 χ 1〇-5 grams, or i χ 1〇_6 grams to 1 X 1〇-5 grams Total Ni / V / Fe content. In certain specific examples, this crude oil contains up to 2 X 10-5 grams of Ni / V / Fe. In several specific examples, the total Ni / V / Fe content of the crude product is Ni / V / Fe content of crude oil feed from 70 to 130%, 80 to DO%, or 90 to 110%. In some specific examples, the total metal content of the crude oil product in the form of a metal salt of an organic acid is at most 90%, at most 50%, up to 10%, or up to 5% organic in crude oil feed The total metal content in the form of an acid metal salt. In a specific specific example, the crude product has a metal salt in the form of an organic acid metal 200535224. The total content is in the range of from 80% to 10% to 10% to 20% to 30%. To 50% of the total metal content in the form of metal salts of organic acids in crude oil feeds. Organic acids used to form metal salts include, but are not limited to, carboxylic acids, thiols, imines, sulfonic acids, and sulfonic acids salt. Examples of carboxylic acids include, but are not limited to, naphthenic acid, non-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 zinc and cadmium), column 15 metals (such as arsenic), and column 6 Metal (such as chromium), or a mixture thereof. In a specific embodiment, the total content of the metal in the form of an organic acid metal salt per gram of crude product of the crude oil product is from 0.00000 g to 0.00005 per gram of crude product. Grams, 0.0000003 grams to 0.00000 grams, or 0.00001 grams to 0.00000 grams of metal in the form of a metal salt of an organic acid. In some specific examples, the total metal content of the metal salt in the form of an organic acid in a crude oil product is 70 to 130%, 80 to 120%, or 90 to 110% of the total metal content of the organic acid metal salt in the crude oil feed. In a specific embodiment, the contact between the crude oil feed and the catalyst produced under contact conditions The crude oil product has an API specific gravity of 70 to 130%, 80 to 120%, 90 to 110%, or 100 to 130% of the AH specific gravity of the crude feed. In certain specific examples, the crude product API weight ratio is 14 to 40, 15 to 3 'Or 16 to 25. In certain specific examples, the crude oil product has a viscosity of up to 90%, a maximum of 80 //, or a viscosity of up to 70% of the crude oil feed. In several specific examples, the crude oil product has Viscosity in the range of 10 to 60%, 20 to 50%, or 30 to 40% of the viscosity of crude oil feeds. At the time when the 4th degree of certain concrete 61 200535224… is at most 90% of the original heart The crude oil product has an API gravity of 70 to 130% viscosity, which is the same as the Aρι proportion of 90 to 110% of the crude oil feed. To 120%, or in some specific examples, the crude oil product has 90%, the maximum is 50%, the maximum is 10%, or the total heteroatom content of the feed in the factory. In a specific embodiment, the total heteroatom content of the crude oil and crude oil is at least 1%, at least 30%, and has The total heteroatom content of crude oil feed to 乂 is 99 /. For certain specific real oil products, the maximum is 50%, the maximum is 10%, or; the maximum sulfur content. The crude oil product of the body f ", ... is 10 /, and the crude oil product in m has a sulfur content of at least feed A; / Yue M /" is at least 80% , Or at least 99% of the 3 sulfur set of crude oil feed. In Ruoqian County, every 70 to 70% of the crude oil product ... The sulfur content of the crude oil product is the sulfur content. Containing 90%, the total nitrogen content of the crude oil product may be at most two in the examples of ΓΑ and f ;;:, most of ⑽, or the most;: 二。 / Special 中 In the specific example, the crude product has The total nitrogen content is at least 30%, at least 80%, or at least $ 99% of the total nitrogen content of the crude feed. The specific nitrogen content of the crude oil product in the JTt specific example may be the most :: / °, table more she's bursting up to 10%, or up to: the experimental nitrogen content of the crude oil feed. For certain specific oil products, the test nitrogen content is at least $ 1%, at least 鄕, at least = 62 200535224 80 / 〇 'or at least $ 99〇 / in several specific examples. 90¾, up to 50000 / π, the oxygen content of crude oil products may be at most like that of crude oil feed: oxygen? It is 30%, at most ㈣, or at most with oxygen content of at least AS. In a specific embodiment, the crude oil product has 99% of crude oil, '2, at least 80%, or at least oxygen content. In the specific example of the right stem, 'crude oil production 5000 / W 880 / 〇' 10 to 70%, 20 to 60%, or 30 to

肩、1產物/ #的含氧量之範圍内。於若干具體實例中， 原:由產曰物的㈣化合物總含量可能最多為·，最多為 :〇二取多為丨。％，或最多為5%之原油進料中㈣酸化合 於特定具體實例中，原油產物具有羧酸化合物總 3里至少為1%，至少為30%，至少為80%，或至少為99% 之原油進料中的羧酸化合物總含量。Shoulder, 1 product / # range of oxygen content. In some specific examples, the total content of the osmium compound in the original: from product may be at most ·, at most: 〇2 is taken as 丨. %, Or up to 5% of crude oil in the feedstock. In a specific embodiment, the crude product has at least 1%, at least 30%, at least 80%, or at least 99% of the total 3 carboxylic acid compounds. The total content of carboxylic compounds in the crude oil feed.

於若干具體實例中，可還原原油進料中的選定有機氧 化合物。於若干具體實例中，缓酸及/錢酸金屬鹽可在含 非羧酸有機氧化合物之前使其化學還原。原油產物中含緩 酸與非羧酸的有機氧化合物可使用一般已知的光譜法(例如 紅外線分析、質譜分析，及/或氣相層析法）藉由分析原油 產物而鑑別。 此原油產物於特定具體實例中具有含氧量最多為 9〇°/〇，最多為80%，最多為70%，或最多為5〇%之原油進 料的含氧量，而此原油產物的TAN最多為9〇%，最多為 70%，最多為50%，或最多為40%之原油進料的TAN。於 特定具體實例中，原油產物具有含氧量至少為1 %，至少 63 200535224 進料的含氧量， 為30%，至少為 為3 0%，至少為8〇〇/戋至 ~ 次主少為99。/〇之原油 而此原油產物具有ΤΑΝ至少為1%，至少 80%’或至少為99%之原油進料的ταν。 此外，原油產物可具有m酸及/或敌酸金屬鹽含量佔原 油進料最多為90%，最多為7〇0/导夕去 钩70%，取多為50%，或最多為 概，含非m酸有機氧化合物的含量是在7g i 13〇%，8( 至12〇%，或90至110%之原油進料中含非幾酸有機氧化 合物的範圍内。 於若干具體實例中，原油產物於其分子結構中包含每 克原油產物有0.05至0.15克或〇.〇9至〇 13克的氮。此原 油產物於其分子結構中可包含每克原油產物有〇_8至0.9 克或0.82至〇·88克的碳。原油產物之原子氫和原子碳的 比（H/C)可在70至130%，80至120%，或90至11〇%之原 油進料的原子H/c比之範圍内。在1〇至3〇%之原油進料 的原子H/C比之範圍内的原油產物之原子H/c比係顯示出 在過程中吸取及/或消耗的氫相當地少，及/或氫係現場生 產0 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 〇〇1克， 或0.001至0.5克之沸程分佈在0.101 MPa下最多為i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l〇〇°C和200°C之間的烴；至少0.001克，或o.ooi 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，或〇·〇〇1至0.5克之沸程分佈在0.101 64 200535224 MPa下介於300°C和400°C之間的烴；及至少〇·〇01克，或 0.001至0.5克之沸程分佈在0101 MPa下介於4〇(Γ(：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0 101 MPa下最多為1〇(rc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2001之間的烴。 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0 01克的石腦油。在其他具體實 例中，原油產物可具有石腦油含量為每克原油產物中最多 〇_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7〇至 130/。，80至120%，或90至ιι〇%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ι至Ο」 克’0.001至〇_3克，或〇 002克至〇 2的範圍内。 於特定具體實例中，原油產物具有VGO含量為70至 130/〇 80至120%，或90至ιι〇〇/0之原油進料的VG〇含 里於右干具體實例中，原油產物在每克原油產物中具有 0.00001至〇·8克，〇 〇〇1至〇 5克，或〇 至U克或 0.001至0·3克之範圍内的VG〇含量。 。於右干具體實例中’原、油產⑼具有歹曼留物含量為川至 曰 8〇至120/。，或90至11〇〇/0之原油進料的殘留物含 里此原，由產物可在每克原油產物中具有〇 〇〇〇〇1至〇·8 克0·〇001 至 〇·5 克，0.0005 至 〇·4 克，0.001 至 〇·3 克， 65 200535224 • 5至0.2克，“·〇1至〇1克之範圍 旦 於特定具體實例中，原油產 ^里。 量，同時此原油產物具有〇〉歷主:旦原油進料的⑽含 5/月貝含置最多為9〇0/，B7夕 為_，或最多為50%之原油進 質。二 定具體實例中，原』…I。於特 心丨T W /歷青質含量至 少為60%，或至少為70% ^ ° ’ 恭/由進枓的C5瀝青皙合吾，π 時原油產物的MCR含量在1〇至 、 °In several specific examples, selected organic oxygen compounds in a crude oil feed can be reduced. In several specific examples, the retarded acid and / or lauric acid metal salt can be chemically reduced before the non-carboxylic acid-containing organic oxygen compound. Crude products containing organic acids and non-carboxylic acids can be identified by analyzing crude products using generally known spectroscopic methods (such as infrared analysis, mass spectrometry, and / or gas chromatography). This crude oil product has an oxygen content of up to 90 ° / 〇, up to 80%, up to 70%, or up to 50% of the oxygen content of the crude oil feed in a specific embodiment. The TAN is at most 90%, at most 70%, at most 50%, or at most 40% of the TAN of crude oil feed. In specific examples, the crude oil product has an oxygen content of at least 1%, at least 63 200535224, and the oxygen content of the feed is 30%, at least 30%, and at least 800 / 戋 to ~ secondary Is 99. This crude product has a ταν of at least 1%, at least 80% ', or at least 99% of the crude oil feed. In addition, crude oil products can have m-acid and / or diacid metal salt content of up to 90% of the crude oil feed, up to 700/70% decoupling, up to 50%, or at most, including The content of non-acid organic oxygen compounds is within the range of 7 g i 13%, 8 (to 120%, or 90 to 110% of crude oil feed containing non-acid organic oxygen compounds. In several specific examples, The crude product contains from 0.05 to 0.15 grams or 0.09 to 0.013 grams of nitrogen per gram of crude product in its molecular structure. This crude product may contain from 0.8 to 0.9 grams per gram of crude product in its molecular structure Or 0.82 to 0.88 grams of carbon. The ratio of atomic hydrogen to atomic carbon (H / C) of the crude oil product may be 70 to 130%, 80 to 120%, or 90 to 11% of the atomic H of the crude oil feed. / c ratio range. The atomic H / c ratio of crude oil products within the range of 10 to 30% of the atomic H / C ratio of the crude oil feed shows comparable hydrogen absorption and / or consumption during the process Low ground, and / or hydrogen-based on-site production of crude oil products contains components within a certain boiling point range. In several specific examples, crude oil products include per gram of crude oil product: At least 0.001 g, or 0.001 to 0.5 g boiling range distribution at 0.101 MPa hydrocarbons up to 100 ° C; at least 0.001 g, or 0.001 to 0-5 g boiling range distribution at 0 · 101 Mpa Hydrocarbons between 100 ° C and 200 ° C; at least 0.001 g, or o.ooi to 0.5 g 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 hydrocarbons with a boiling range distribution between 0.101 64 200535224 MPa between 300 ° C and 400 ° C; and at least 0.0001 grams, or a boiling range of 0.001 to 0.5 grams Hydrocarbons distributed between 0 ° (° (° and 538 ° C) at 0101 MPa. In several specific examples, the crude oil product contains at least 0.001 grams of boiling range distribution per gram of crude oil product at a maximum of 0 101 MPa Hydrocarbons of 10 rc and / or hydrocarbons with a boiling range distribution of at least 0.001 g between 0.100 ° C and 2001 at 0.101 MPa. In several specific examples, crude oil products may be present in each gram of crude oil product. Contains at least 0.001 grams, or at least 0.01 grams of naphtha. In other specific examples, the crude product may have a naphtha content of up to 0-6 grams per gram of crude product , Or a maximum of 0.8 g. In several specific examples, the crude oil product has a distillate content of 70 to 130%, 80 to 120%, or 90 to 120% of the crude feed feed fraction. Crude oil product fractions The content per gram of crude oil product may be in the range of 0.001 to 0 "grams, '0.001 to 0-3 grams, or 0.0002 grams to 0. In a specific embodiment, the crude oil product has a VG of a crude oil feed having a VGO content of 70 to 130 / 〇80 to 120%, or 90 to ιι 00/0. In the specific example of the right, the crude oil product is The gram crude product has a VG0 content in the range of 0.00001 to 0.8 grams, 0.001 to 0.05 grams, or 0 to U grams or 0.001 to 0.3 grams. . In the specific example of Yougan, the raw materials of crude oil and oil have a remanent content of Sichuan to 80 to 120 /. Residues of crude oil feeds, or 90 to 1100/0, are included, and the product can have from 0.0001 to 0.8 g of 0.0001 to 0.5 per gram of crude oil product. Gram, 0.0005 to 0.4 grams, 0.001 to 0.3 grams, 65 200535224 • 5 to 0.2 grams, "· 〇1 to 〇1 grams range in the specific embodiment, crude oil production. The amount of this crude oil The product has 〇> calendar master: the crude oil feed containing 5 / month shells contains a maximum of 9000 /, B7 is _, or a maximum of 50% of crude oil feed. In the second specific example, the original " … I. Yu Texin 丨 TW / Li Qingqing content is at least 60%, or at least 70% ^ ° 'Gong / Yu Jin C5 asphalt Hehe, the MCR content of crude oil product at π is 10 to, °

含量之範_ H + 二=進料的MCR 主斯人曰 貝1 J甲減少原油進料的c5瀝 月貝含夏且同時保持相對穩定的mcr 料/總產物混合物的穩定度。 里了知加原油進The range of content _ H + 2 = the MCR of the feed. The shellfish 1 J A reduces the c5 leaching of crude oil feed. The scallop contains summer and at the same time maintains the stability of the mcr feed / total product mixture. Zhijia Crude Oil

—於若干具體實例中，可結4C5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 向黏度成分之間的數學關係。舉例而言，原油進料之。瀝 青質含量和原油進料之MCR含量的和可表示為s。原油產 物之C5瀝青質含量和原油產物之MCR含量的和可表示為 S’。可比較這些和(S，與S)以估算原油進料中高黏度成分的 淨減少量。原油產物的S，可在1至99%，1〇至9〇%，或2〇 至80〇/〇之S的範圍内。於若干具體實例中，原油產物之mcr 含量和C：5瀝青質含量的比在i.o至3 〇，1.2至2.〇，或13 至1 · 9的乾圍内。 於特定具體實例中，原油產物具有MCR含量最多為 9〇 /〇袁多為80%，最多為50%或最多為1〇0/。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 200535224 量在1至80%，Η)至7G%，2G至6()%，或3()至5〇%之原 油進料的MCR含量之範®内。原油產物於若干具體實例 中在每克原油產物中含有〇.()_至G」克，請5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·_001至〇 〇〇1克，或〇 〇〇〇〇1 至0.0001克的觸媒總量。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；〇降低的總Ni/V/Fe含量；d)降低 的硫、氧、氮，或其組合之含量；e)降低的殘留物含量； f)降低的I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 14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VGO)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 /、他成分的減少。因此，雖然使用較少的氫，但仍可 減少原油進料的TAN，因為較少量的這類氫同樣會用來減 67 200535224 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， 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、鉬、鎢、猛、錄、銖、鐵、始、 鎳、釕、、錄、锇、錶、翻，或其混合物。該觸媒在每 克觸媒中可具有至少0.0001克，至少0.001克，至少0.01 68 200535224 克或是在0.0001至0.6克，0.005至0·3克，〇·〇〇ι至〇 i 克，或0.01至〇_〇8克的第5至10攔金屬總含量。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攔元素。第15欄元素的實例包括磷。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丨至〇1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。 於特定具體貫例中，觸媒包含第6攔金屬。該觸媒在 每克觸媒中可具有至少0·0001克，至少〇 〇1克，至少〇 〇2 克及/或在0.0001至0.6克，0·001至0 3克，〇 〇〇5至〇 i 克，或0·01至0·08克的第6欄金屬總含量。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 欄金屬。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欄元素。 於若干具體實例中，觸媒包含第6攔金屬與第5攔及/ 或第7至10攔之一或多種金屬的組合。第6攔金屬與第5 搁金屬的莫耳比可在〇.丨至2〇，！至1〇，或2至5的範圍 内。第6攔金屬與第7至1〇攔金屬的莫耳比可在丨至， 1至10，或2至5的範圍内。於若干具體實例中，觸媒除 了第6攔金屬與第5欄及/或第7至1〇攔之一或多種金屬 的組合之外，還包含第15欄元素。於其他具體實例中， 觸，包^第6攔金屬和第1〇攔金屬。觸媒中第1〇攔金屬 總量與第6襴金屬總量的莫耳比可在1至1〇，或2至5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 200535224 欄金屬。觸媒中第丨0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 可包括耐火性氧化物，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_ =化紹、氧化鈦、氧化鍅、氧賴，或其混合物。载體可 ^ ^ ^ t ^ xe ^ ^ Criterion Catalysts and Technol〇gies LP (H〇USt〇n，丁_，U.S.A·)。多孔性碳基材料包括，但不 限於活性碳及/或多孔石墨。彿石的實例包括γ沸石卞弗 石、絲光沸石、ZSM_5沸石和鎮驗彿石。沸石可得 製造商，例如 Z“lyst (Valley FGrge，p_syivania，u s A 二 於若干具體實例中係製備載體以便使該載體具有至少 ’至少170 A，或至少180 A的平均孔徑。於特 =中，載體係藉由形成載體的水浆而製備。於若干且 例令，將酸添加至漿料以促進漿料的擠出 釋 :…所需要的量並藉由所需要的方法添加：= :出浆料期望的稠度。酸的實例包括，但不限於硝酸二 酉文、硫酸和鹽酸。 _ 乙 漿料可使用一般已知的銳 出和切宅aw成樁“觸媒擠出法和觸媒切割方法擠 心场成擠出物。該擠出物可在5至26G t或8儕5 70 200535224 至：35 t之範圍内的溫度下熱處理—段時間(例如… t=/或直到擠出物的濕度達到期望值為止。熱處理過 的擠出物可在800至ι2〇〇疒化 王ιαυ C或900至11〇〇 t之範圍内 的溫度下進一步執虛採以你士、曰+ τ— In several specific examples, the 4C5 asphaltene content and MCR content can be combined to produce a mathematical relationship between the viscosity components of the crude oil product compared to the high viscosity components in the crude oil feed. For example, crude oil is fed. The sum of the asphaltene content and the MCR content of the crude feed can be expressed as s. The sum of the C5 asphaltene content of the crude oil product and the MCR content of the crude oil product can be expressed as S '. These sums (S, and S) can be compared to estimate the net reduction in high viscosity components in the crude feed. The S of the crude product may be in the range of 1 to 99%, 10 to 90%, or 20 to 80/0. In several specific examples, the ratio of the mcr content to the C: 5 asphaltene content of the crude product is within the dry range of i.o to 30, 1.2 to 2.0, or 13 to 1.9. In a specific embodiment, the crude product has an MCR content of at most 90/0, and at most 80%, at most 50%, or at most 100 /. MCR content of crude oil feed. In some specific examples, the crude product has a range of mcr content 66 200535224 ranging from 1 to 80%, i) to 7G%, 2G to 6 ()%, or 3 () to 50% of the MCR content of the crude feed ® inside. The crude oil product contains, in several specific examples, 0.1 to 0.5 g of gram per gram of crude oil product, please 5 to 8 g, or 0.01 to 0.05 g of MCR. In several specific examples, the crude oil product contains more than 0 grams, but less than 0.01 grams, 0.001 to 0.0001 grams, or 0.0001 to 0.0001 grams of total catalyst per gram of crude oil products. the amount. 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 catalysts described herein to the crude oil product 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) reducing TAN; b) reducing viscosity; 〇 reducing total Ni / V / Fe content; d) reducing sulfur, oxygen, nitrogen, or combinations thereof; e) reducing F) reduced I 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 oil product may be selectively changed compared to the crude oil feed, while other properties are not changed or substantially unchanged. For example, it may be desirable to select only 14 to reduce the TAN in the crude feed without significantly altering the amount of other components such as sulfur, residues, Ni / V / Fe, or VGO. In this way, the hydrogen uptake during the contact can be "concentrated" according to the decrease in TAN, without reducing the other components. Therefore, although less hydrogen is used, the crude oil feed can still be reduced. TAN, because a smaller amount of this type of hydrogen will also be used to reduce the amount of other components in the crude oil feed. 67 200535224 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 reducing sulfur as well. The catalyst used in one or more embodiments of the present invention may include one or more bulk metals and / Or one or more metals on the carrier. The metal can be in the form of an element or a metal compound. The catalyst described herein can be introduced into the contact zone as a precursor and then become an active catalyst in the contact zone (for example When sulfur and / or sulfur-containing crude feeds come 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 article Examples include HDS3; HDS22; HDN60; C234; C311; C344; C411; C424; C344; C444; C447; C454; C448; C524; C534; DN110; DN120; DN130; DN140; DN190; DN18; DN800; DN3100; DN3110; DN3300; DN3310; RC400; RC410; RN412; RN400; RN420; RN440; RN450; RN650; RN5210; RN5610; RN5650; RM430; RM5030; Z; Z; Z; 703; Z623; Z; Z763, which is available from CRI International, Inc. (Houston, Texas, USA). 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 carrier. Columns 5 to 10 include, but are not limited to, hungry, chromium, molybdenum, tungsten, tungsten, iron, baht, iron, metal, nickel, ruthenium, iron, iron, watch, iron, or mixtures thereof. The gram catalyst may have at least 0.0001 grams, at least 0.001 grams, at least 0.01 68 200535224 grams, or 0.0001 to 0.6 grams, 0.005 to 0.3 grams, 0.0000 to 0 grams, or 0.01 to 〇_〇. 8 5 to 10 bar of total metal content. In some specific examples, the catalyst contains elements 15 to 10 in addition to metals 5 to 10. Examples of column 15 elements include phosphorus. The catalyst may have a total content of the 15th element in the catalyst of 0.000 to 0.001 grams per gram of catalyst, 0.00001 to 0.06 grams, 0.0005 to 0.003 grams, or 0 0001 To the range of 0.0001 grams. In a specific embodiment, the catalyst includes a sixth metal. The catalyst may have at least 0.0001 grams, at least 0.001 grams, at least 002 grams, and / or 0.0001 to 0.6 grams, 0.001 to 0.3 grams, and 0.005 grams per gram of catalyst. 〇i grams, or total column 6 metal content from 0.01 to 0.08 grams. In some specific examples, the catalyst contains 0.0001 to 2006 grams of the sixth column metal per gram of catalyst. In some specific examples, the catalyst includes elements in column 15 in addition to the metals in column 6. In some specific examples, the catalyst includes a combination of the sixth metal and the one or more metals of the fifth and / or the seventh to the tenth. The Mohr ratio of the 6th metal and the 5th metal can be between 〇. 丨 and 〇20! To 10, or 2 to 5. The molar ratios of the 6th metal to the 7th to 10th metal can be in the range of 1 to 10, or 2 to 5. In some specific examples, the catalyst includes elements in column 15 in addition to the combination of metal in column 6 and one or more metals in columns 5 and / or 7 to 10. In other specific examples, contacting the 6th metal and the 10th metal. The molar ratio of the total amount of the 10th metal in the catalyst to the total amount of the 6th metal can be in the range of 1 to 10, or 2 to 5. In a specific embodiment, the catalyst includes the 5th metal and the 1069 200535224 metal. The molar ratio of the total amount of metal in the catalyst to the total amount of metal in the fifth can be in the range of 1 to 10, or 2 to 5. In several specific examples, columns 5 to 10 of the metal system are incorporated or deposited on a support to form a catalyst. In some specific examples, a combination of 5th to 10th metal and 15th element is incorporated or deposited on a carrier to form a catalyst. In the specific example of metal and / or element loading, the weight of the catalyst includes all carriers, all metals and all elements. The support may be porous and may include refractory oxides, porous carbon-based materials, zeolites, or a combination thereof. Refractory oxides may include, but are not limited to, aluminum oxide, silicon oxide, silicon oxide, titanium oxide, hafnium oxide, oxygen oxide, or mixtures thereof. The carrier can be ^ ^ ^ t ^ xe ^ ^ Criterion Catalysts and Technologies LP (Hounton, Ding, U.S.A.). Porous carbon-based materials include, but are not limited to, activated carbon and / or porous graphite. Examples of buddhist stones include gamma zeolite, mordenite, mordenite, ZSM_5 zeolite, and vermiculite. Zeolites are available from manufacturers, such as Z "lyst (Valley FGrge, p_syivania, us A. In several specific examples, the carrier is prepared so that the carrier has an average pore size of at least 'at least 170 A, or at least 180 A. Ute = medium The carrier is prepared by forming a water slurry of the carrier. In several and ordinances, an acid is added to the slurry to promote the release of the slurry: ... the required amount and added by the required method: =: The desired consistency of the slurry. Examples of acids include, but are not limited to, divinyl nitrate, sulfuric acid and hydrochloric acid. _ B slurry can use commonly known sharp-out and cut-pile "catalyst extrusion method and catalyst The media cutting method squeezes the heart field into an extrudate. The extrudate can be heat treated at a temperature in the range of 5 to 26 G t or 8 侪 5 70 200535224 to: 35 t for a period of time (for example ... t = / or until extruded The humidity of the output reaches the desired value. The heat-treated extrudate can be further processed at a temperature in the range of 800 to ι200,00 ° C, or 900 to 1100t.

八，、恿理以形成具有平均孔徑至少A 150 A 的載體。 於特定具體實例中，載體包含γ氧化紹、θ氧化銘、5氧 化紹、CC氧化紹，或其混合物”氧化紹、靴化銘、α氧化 鋁，或其混合物的量於每克觸媒载體中可在〇〇〇〇1至&quot;9 克，〇顧至〇.5克，0·01至（U克的範圍内，或最多為〇1 · ^ ’其藉纟X射線繞射測定。於若干具體實例中，載體係 早獨含有或結合其他形態的氧化銘，Θ氧化紹含量於每克 載體中在(Μ至0.99克，〇_5至〇9克，或“至〇8克的 範圍内，其藉Φ X射線繞射測定。於若干具體實例中，載 體可切至少（Μ克，至少〇.3克，至少Q 5克，或至少U 克的Θ氧化鋁，其藉由χ射線繞射測定。 〇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 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。 於特定具體實例中，在浸潰金屬之前，使載體於4〇〇至12〇〇 C，450至1000 t，或6〇〇至9〇〇之範圍内的溫度下 進行熱處理。於若干具體實例中，浸潰助劑可在製備觸媒 71 200535224 '彳使用/文/貝助劑的實例包括擰檬酸成分、乙二胺四乙 酸（EDTA)、氨，或其混合物。 於特定呈興香/丨丄 、 〃 _貫例中’觸媒可藉由將第5至1 〇攔金屬添 加或推入已執虛拂士 …处理成形的載體混合物（“覆蓋”）而形成。在 一、、、处里成形的载體頂面上覆蓋金屬以具有實質或相對均 ::度的金屬通常會賦予觸媒有利的催化性質。在每次覆 盍五屬後熱處理已成形的載體會有改善觸媒催化活性的傾 向。使用覆蓋法製備觸媒的方法係見述於料Bhan的美 國專^#案公告案號200301 1 1391。 、# 1 〇搁金屬和載體可用適當的混合設備混合以形 =第5至1〇攔金屬/載體混合物。第5至1〇欄金屬/載體 混合物可伟η # $ 勺 田的混合設備混合。適當的混合設備實例 匕括滾同、固定殼或槽、研磨混合機(例如分批式或連續 γ π肯擊式此合機，以及能適當形成第5至1 〇欄金屬/載 j匕口物的任何其他一般已知混合器，或一般已知裝置。 :、U貫例中，使材料混合直到帛5至1 〇 ；)：闌金屬實 質上均勻分散在載體中為止。 於若干具體實例中，在結合載體與金屬之後，使觸媒 在 1 5 〇 5 7 ^ Π °r^ 、 c，200 至 740 °C，或 400 至 730 °c 的溫 度下進行熱處理。 於右干具體實例中，觸媒可在熱空氣及/或富氧空氣存 於’丨於400 c和1〇〇〇 °C之範圍内的溫度下進行熱 處理’以移除揮發性物f，以便使至少一部分的第5至1〇 攔金屬轉化成對應的金屬氧化物。 72 200535224 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。(：，低於400 °C或低於500 °C)之 範圍内的溫度下熱處理達1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1 〇攔金 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 6,290,841。 於特定具體實例中，Θ氧化鋁載體可結合第5至1〇攔 金屬以形成Θ氧化鋁載體/第5至1〇欄金屬混合物。㊀氧化 鋁載體/第5至10攔金屬混合物可在至少4〇〇它的溫度下 熱處理以形成具有中位孔徑至少為23〇 A之孔徑分佈的觸 媒。典型而言，這類熱處理在最高為12〇〇艺的溫度下進 行。 於若干具體實例中，載體（商品載體或如本文敘述所製 備之載體）可與受載觸媒及/或塊狀金屬觸媒結合。於若干 具體實例中，受載觸媒可包含第15攔金屬。舉例而言， 受載觸媒及/或塊狀金屬觸媒可壓碎成平均粒徑為丨至$ 〇 微米，2至45微米，或5至40微米的粉末。該粉末可與 載體結合以形成埋入金屬觸媒。於若干具體實例中，粉末 可與載體結合，然後使用標準技術擠出，以形成具有中位 孔徑在80至200 A或90至180 A，或12〇至13〇 A的範 圍内之孔徑分佈的觸媒。 73 200535224 使觸媒與載體接觸於若干 右卞具體實例中可容許至少一部 分的金屬存在於埋入金屬 ^ 中），而…主 *屬觸女某表面下方(例如埋入載體 者有更少的金屬。於若干呈'^存在於 金屬觸媒 、干具體實例中，在觸媒表面上具有 車父 &gt; 金屬者會由於在使用期 _主 更用期間谷許至少-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敍而移到觸媒表面。8. Eggs are cut to form a carrier having an average pore size of at least A 150 A. In a specific embodiment, the carrier contains γ oxide, θ oxide, 5 oxide, CC oxide, or a mixture thereof. The amount of the "oxide, boot chemical, α alumina, or mixture thereof" is per gram of catalyst. The body can be measured in the range of 0.0001 to &quot; 9 grams, 〇 to 0.5 grams, 0.01 to (U grams, or a maximum of 〇1. In a few specific examples, the carrier is alone or in combination with other forms of oxides, the content of Θ oxide in each gram of the carrier is between (M to 0.99 g, 0 to 5 to 9 g, or "to 0 g It is determined by Φ X-ray diffraction. In some specific examples, the carrier can be cut at least (M grams, at least 0.3 grams, at least Q 5 grams, or at least U grams of Θ alumina, by X-ray diffraction measurement. 〇 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 .; issued to Gabrielov 6 29〇841 et al; 5,744,025 to et al, and U.S. Patent Application Publication No. 20030111 to Bhan 391. In some specific examples, the carrier may be impregnated with metal to form a catalyst. In a specific embodiment, the carrier is allowed to be at 400 to 12000C, 450 to 1000 t, or 6 before impregnating the metal. The heat treatment is performed at a temperature ranging from 〇00 to 900. In several specific examples, the impregnation aid can be used in the preparation of the catalyst 71 200535224. Diaminetetraacetic acid (EDTA), ammonia, or mixtures thereof. In certain examples, the catalyst can be added or pushed to the 5th and 10th metal barriers. It is formed by processing the formed carrier mixture ("cover"). The top surface of the carrier formed in one, one, or the other is covered with metal to have substantial or relative uniformity: Metals that generally give catalysts a favorable catalyst Properties. The heat-treated formed support will tend to improve the catalytic activity of the catalyst after each coating of the five genus. The method of preparing the catalyst by the covering method is described in the US patent No. 200301 1 described by Bhan. 1391. # 1 〇 metal and carrier can be mixed with appropriate The equipment is mixed in the shape of the metal / carrier mixture from the 5th to the 10th. The metal / carrier mixture from the 5th to the 10th column can be mixed with the mixing equipment of the spoon field. Examples of suitable mixing equipment include rolling and fixed shells. Or tank, grinding mixer (e.g., batch or continuous gamma π striker, and any other generally known mixer capable of properly forming columns 5 to 10 of metal / knife load, or general Known device: In the U example, the materials are mixed until 帛 5 to 10;): the stopper metal is substantially uniformly dispersed in the carrier. In some specific examples, after the carrier and the metal are combined, the catalyst is made. The heat treatment is performed at a temperature of 1 5 005 7 ^ Π ° r ^, c, 200 to 740 ° C, or 400 to 730 ° c. In the specific example on the right, the catalyst may be heat-treated at a temperature in the range of 400 c and 1000 ° C with hot air and / or oxygen-enriched air to remove volatiles f, In order to convert at least a part of the 5th to 10th metal to the corresponding metal oxide. 72 200535224 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. (:, less than 400 ° C or less than 500 ° C)). A period of time ranging from 1 to 3 hours' to remove most volatile substances without converting the 5th to 10th metal into metal oxides. Catalysts prepared by this method are usually called Is "uncalcined, catalyst. When combined in this way to form a sulfide catalyst, the active metal can be substantially dispersed in the carrier. The preparation of such catalysts is described in the award to Gabrielov et al. U.S. Pat. No. 6,218,333 'and 6,290,841 to Gabrielov et al. In specific examples, a Θ alumina support can be combined with metals 5 through 10 to form a Θ alumina support / columns 5 through 10 Mixture. The alumina support / metal mixtures 5 through 10 can be heat treated at a temperature of at least 400 to form a catalyst having a pore size distribution with a median pore size of at least 230 A. Typically, this type of heat treatment At temperatures up to 12,000 The carrier (commercial carrier or carrier prepared as described herein) may be combined with a supported catalyst and / or a bulk metal catalyst in some specific examples. In some specific examples, the supported catalyst may include The 15th metal. For example, the supported catalyst and / or bulk metal catalyst can be crushed into a powder having an average particle size of 丨 to $ 0 microns, 2 to 45 microns, or 5 to 40 microns. The powder Can be combined with a carrier to form an embedded metal catalyst. In several specific examples, the powder can be combined with a carrier and then extruded using standard techniques to form a median pore size of 80 to 200 A or 90 to 180 A, or 12 Catalysts with a pore size distribution in the range of 0 to 13A. 73 200535224 Contacting the catalyst with the carrier in a number of specific examples allows at least a portion of the metal to be present in the buried metal ^), and ... Touch the surface of the female (for example, the person who embeds the carrier has less metal. In some specific examples, the metal catalyst exists on the surface of the catalyst, and the person who has the metal on the surface of the catalyst will cause _Guxu period Gu Xu at least- Sub-surface of the catalyst metal is moved extend invasion and Syria moved during the catalyst surface of the catalyst surface of the catalyst life and / or catalytic activity of metal may be contacted by contact with the crude oil feed medium.

'化戈混合觸媒成分於若干具體實例中會使第6欄 羊 體結構中第6搁金屬的結構順序變成埋入觸媒晶'Hua Ge's mixed catalyst composition will make the structure sequence of the 6th metal in column 6 in the sheep body structure into the embedded catalyst crystal

體結構中帛6攔金屬的實質隨機順序。第6攔金屬的順序 可使用粉纟X射線繞射法衫。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 射線、VO射光4中第6攔金屬波峰的順序而決^。從與X 射線、、凡射光邊中第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搁金屬。 舉例而曰，二氧化鉬與具有中位孔徑至少為丨8〇入的 氧化1呂載體可結合形成氧化铭/三氧化錮混合物。三氧化錮 具有明確圖案（例如明確的D1“及/或D·波峰）。氧 化鋁/第6欄二氧化物混合物可在至少538。〇(1〇〇〇卞）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D100波峰）的觸媒。 於右干具體實例中，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， 74 200535224 或其組合。觸媒可具有盥丨 ’ 〃孔搜相對的孔徑總量分佈。孔徑 分佈的中位孔徑可在3 〇至彳加π x 9 你 υ 主 100〇 A、50 至 500 A，或 60 至 A的範圍内。於若干具體實例中，每克觸媒中包含至 J 〇·5克γ氧化鋁的觸媒具有中位孔徑在6〇至2⑻人；9〇 至180人’ 100至140人，或12〇至130 Α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㊀氧 化鋁的觸媒具有中位孔徑在18〇至5〇〇人，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 A，至少為15〇人，至少為 180 A，至少為200人，至少為22〇人，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1〇〇〇人。 觸媒可具有中位孔徑至少為60 A或至少為90 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1 8〇 A，100至140 A，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 A、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 中位孔控在70至1 80 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 A，或25 A之中位 孔徑範圍内的孔徑。 於孔徑分佈之中位孔徑至少為180 A，至少為200 A， 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 A、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18〇至 500 A，2〇〇至400人，或230至300 A之範圍内的孔徑分 75 200535224 50 A、70 A， 佈，該孔徑分佈中至少60%的總孔數具有在 或90人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 / υ·3 cm3/g、 孔的孔體積可在0.3至〇·99 cm3/g，〇·4至〇.8 至少0.7 cm3/g或至少為〇·9 cm3/g。於特定具題實例中， cm3/g，或 0.5 至0.7 cm3/g的範圍内。 具有中位孔徑在90至1 80 A之範圍内的； 心祀冏的孔您分佈之觸The substantially random order of 帛 6 metal in the body structure. The 6th order of metal blocking can be used powder X-ray diffraction shirt. 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 with the rays of the catalyst and the VO light. The order of the 6th metal peak in 4 is determined ^. From the pattern widening and / or non-patterning related to the 6th metal in X-ray and light-emitting edges, it can be estimated that the 6th metal that is substantially randomly arranged in the crystal structure can be estimated. By way of example, molybdenum dioxide can be combined with an oxide carrier having a median pore size of at least 800 mm to form an oxide oxide / thorium oxide mixture. Hafnium trioxide has a well-defined pattern (such as a well-defined D1 "and / or D · wave peak). The alumina / column 6 dioxide mixture may be heat treated at a temperature of at least 538.0 ° (10000 °) to produce The X-ray diffraction spectrum does not show catalysts with molybdenum dioxide patterns (for example, without D100 peak). In the specific example of the right stem, the catalyst may be characterized by a pore structure. The parameters of various pore structures include, but are not limited to Pore size, pore volume, surface area, 74 200535224 or a combination thereof. The catalyst may have a total pore size distribution relative to the pore size. The median pore size of the pore size distribution may range from 30 to 彳 plus π x 9. 〇A, 50 to 500 A, or 60 to A. In some specific examples, the catalyst containing up to J 0.5 g of gamma alumina per gram of catalyst has a median pore size of 60 to 2 people. Pore size distribution in the range of 90 to 180 people, 100 to 140 people, or 120 to 130 A. In other specific examples, the catalyst containing at least 0.01 g of alumina per gram has a median Pore sizes between 180 and 500 people, between 200 and 300 people, or Pore size distribution in the range of 230 to 250 A. In some specific examples, the median pore size of the pore size distribution is at least 120 A, at least 150 people, at least 180 A, at least 200 people, at least 22 people , At least 23 A, or at least 300 A. This type of median pore size is typically up to 1,000 people. The catalyst can have a pore size distribution with a median pore size of at least 60 A or at least 90 A. In some specific examples, the catalyst has a pore size distribution with a median pore size ranging from 90 to 180 A, 100 to 140 A, or 120 to 130 A, and at least 60% of the total number of pores in the pore size distribution has 45 A, 35 people, or 25 people with a median pore size. In a specific embodiment, the catalyst has a pore size distribution with a median pore control in the range of 70 to 1 80 A, with at least 60 in the pore size distribution. % Of the total number of pores has a pore size in the range of 45 A, 35 A, or 25 A. Specific examples of median pore size in the pore size distribution of at least 180 A, at least 200 A, or at least 230 A In this pore size distribution, more than 60% of the total number of pores have a median pore size of 50 A, 70 A, or 90 A In some specific examples, the catalyst has a median pore diameter in the range of 180 to 500 A, 200 to 400 people, or 230 to 300 A. 75 200535224 50 A, 70 A, Cloth, at least 60% of the total number of pores in the pore size distribution has a pore size in the range of or 90 people's median pore size. In some specific examples, the pore volume of the pores may be at least The pore volume can range from 0.3 to 0.99 cm3 / g, 0.4 to 0.8 at least 0.7 cm3 / g or at least 0.9 cm3 / g. In specific examples, cm3 / g, or 0.5 to 0.7 cm3 / g. With a median pore diameter in the range of 90 to 1 80 A; the pores of your heart can be touched by your distribution

媒於若干具體實例中可具有至少為1〇〇m2/g，至少為上川 m2/g，至少為170mVg，至少為22〇1112仏或至少為17〇瓜％ 的表面積。這類表面積可在1〇〇至3〇〇 m2/g，至2川 m2/g，130 至 250 m2/g，或 170 至 22〇 m2/g 的範園内。 於特定具體實例中，具有中位孔徑在180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 mVg，至少為卯 m/g，至少為l00m2/g，至少為12〇m2/g，或至少為2川爪、 的表面積。這類表面積可在6〇至3〇〇 m2/g，90至280 m2/g， 100 至 270 m2/g，或 12〇 至 25〇 m2/g 的範圍内。In some specific examples, the medium may have a surface area of at least 100 m2 / g, at least Kamikawa m2 / g, at least 170 mVg, at least 2,201,112, or at least 170%. Such surface areas can range from 100 to 300 m2 / g, to 2 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 may have at least 60 mVg, at least 卯 m / g, at least 100m2 / g, and at least 12 〇m2 / g, or a surface area of at least 2 claws. Such surface areas can range from 60 to 300 m2 / g, 90 to 280 m2 / g, 100 to 270 m2 / g, or 120 to 250 m2 / g.

於特定具體實例中，觸媒係以成形形態，例如片粒狀、 圓柱狀，及/或擠出物存在。該觸媒典型而言具有在5〇至 N/cm ’ 60 至 4〇〇 N/cm，100 至 350 N/cm，200 至 300 /Cm或220至280 N/cm之範圍内的平板抗碎強度。 於右干具體實例中，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 International，In a specific embodiment, the catalyst exists in a shaped form, such as a pellet shape, a cylindrical shape, and / or an extrudate. The catalyst typically has flat shatter resistance in the range of 50 to N / cm '60 to 400 N / cm, 100 to 350 N / cm, 200 to 300 / Cm, or 220 to 280 N / cm. strength. In the specific example on the right, catalysts and / or catalyst precursors use techniques known in the technology (such as ACTICATTM, CRI International,

InC’）^,L化以形成金屬硫化物（在使用之前）。於若干具體實 例中，觸據7私 * j乾燥然後使其硫化。或者，觸媒可藉由觸媒 76 200535224 2包含含硫化合物之原油進料的接觸而在現場硫化。現場 敬化可在氫存在下使用氣態硫化氫，或液相硫化劑，例如 1機硫化合物（包括烷基硫、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。 於特疋具體實例中，第一類觸媒（“第一種觸媒，，）包含 與載體結合的第5 i 1G攔金屬，且具有中位孔徑在150 至2乃〇人之範圍内的孔徑分佈。第一種觸媒可具有至少1〇〇 :的表面積。第一種觸媒的孔體積可至少為0.5 cm3/g。 第種觸媒可具有丫氧化鋁含量在每克的第一種觸媒中至少 =〇·5克的γ氧化鋁，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0.0001至 ο·1、克之範圍内的第6攔金屬總含量。第一種觸媒能移除 =’由進料中的一部分Ni/V/Fe，移除造成原油進料之TAN 、 P刀成刀，移除原油進料中至少一部分的c5瀝青質， 、-原油進料中至少一部分的有機酸金屬鹽形態之金屬， Μ/ 口 §原油進料與第一種觸媒接觸時，其他性質（例 。2石爪里、VG〇含量、API比重、殘留物含量，或其組合） 月匕只表現出相當少量的變化。能選擇性地改變原油進料 、、貝而同日守只相當少量地改變其他性質可容許原油進料 進仃更有效地處理。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、、、&quot;口的第5至10欄金屬，具有中位孔徑在90至180 77 200535224 人之範圍内的孔彳见公欲 ^ 工布。泫弟二種觸媒的孔徑分佈中至少 60%的總孔數具有在 〒主乂 告接勰仡从 A之中位孔徑乾圍内的孔徑。在適 :料的同樣：ί油進料與第二種觸媒的接觸可生產與原油 n :相比’具有顯著改變之選定性質(例如ΤΑΝ) 口才，、性貝只有少量改變的原油產物。於若 例在接觸期間可存在氳源。 …體實InC ') ^, L to form metal sulfides (before use). In a number of specific examples, it is dried and then vulcanized. Alternatively, the catalyst may be vulcanized in situ by contacting Catalyst 76 200535224 2 crude oil feed containing sulfur compounds. On-site Jinghua can use gaseous hydrogen sulfide in the presence of hydrogen, or a liquid-phase vulcanizing agent, such as organic sulfur compounds (including alkyl sulfur, polysulfide compounds, mercaptans, and maple). % The external vulcanization system is described in US Patent No. 5,468,372 issued to Seamans et al. And 5,688,736 issued to Seamans et al. In the specific example, the first type of catalyst ("the first type of catalyst,") includes a 5 i 1G metal that is combined with a carrier, and has a median pore size in the range of 150 to 2 people. Pore size distribution. The first catalyst may have a surface area of at least 100: The pore volume of the first catalyst may be at least 0.5 cm3 / g. The first catalyst may have a first aluminum oxide content per gram of first. Among the catalysts, at least = 0.5 g of gamma alumina, and typically up to 0.099 g of alumina. The first catalyst has 0.0001 to ο · 1 per gram of catalyst in several specific examples. The total content of the 6th metal in the range of gram and gram. The first catalyst can be removed = 'from some Ni / V / Fe in the feed, remove the TAN and P knives that cause the crude oil feed and remove At least a part of the c5 asphaltene in the crude oil feed, the metal in the form of at least a part of the metal salt of the organic acid in the crude oil feed, M / mouth§ Other properties when the crude oil feed contacts the first catalyst (eg. 2 Stone claws, VG0 content, API specific gravity, residue content, or a combination thereof) The moon dagger showed relatively small changes. Selectively changing the crude oil feed, and only slightly changing other properties on the same date may allow crude oil feed to be processed more efficiently. In several specific examples, one or more of the first catalysts may be used in any order In certain specific examples, the second type of catalyst ("the second type of catalyst,") contains metals from columns 5 to 10 of the carrier, and has a median pore diameter of 90 to 180 77 200535224. Kong Kuo within the range of man sees public desire ^ cloth. At least 60% of the total number of pores in the pore size distribution of the two catalysts has a pore size within the range of the median pore diameter from A to 勰 仡. The same materials are suitable: The contact of the oil feed with the second catalyst can produce crude oil products that have significantly changed selected properties (such as TAN) compared to crude oil n :, and have only a few changes. A source of radon may be present during contact. … Physical

第二種觸媒可減少造成原油進料之TAN的至少—部八 :分’造成相對高黏度的至少—部分成分，及減少原油產 之至少-部分的Νί/·含量。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相比，其含硫量 :當少量改變的原油產物。舉例而言，原油產物可具有含 硫量為70%至130%之原油進料的含硫量。該原油產物與 原油進料相比，在顧分含量、彻含量，和殘留物含量方 面’也可能只表現出相當少量的變化。The second catalyst can reduce at least-part eight of the TAN that causes crude oil feed, at least part of the component that causes relatively high viscosity, and reduce at least-part of the NL / · content of crude oil production. In addition, the contact of the crude oil feed with the second catalyst can produce a crude oil product that has a lower sulfur content compared to the sulfur content of 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%. The crude oil product may also show only a relatively small change in the fraction content, content, and residue content compared to the crude feed.

旦於若干具體實例中，原油進料可具有相對低的驗心 含S (例如最多為50 wtppm)，但相對高的TAN、瀝青質含 里或有機酸金屬鹽形態的金屬含量。相對高的TAN (例 如至少為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q瀝青質含量的劣質原油在處理 期間與具有相對低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A瀝青質。於若 干具體實例中，減少I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 200535224 黏度。於特定具體實例中 用來處理本文中所述的原油=觸媒的一或多種組合當 物混合物的穩定性，增加觸媒，：’：提南總產物/原油產 最小淨吸取。 ”可〒’ ^供原油進料之氫的 於若干具體實例中， *使載體與第6欄金屬結合:生二第广媒”)可藉 前驅物可在一或多 ☆ 觸媒則驅物而獲得。觸媒In several specific examples, the crude oil feed may have a relatively low core content S (e.g., up to 50 wtppm), but a relatively high metal content in the form of TAN, asphaltenes, or metal salts of organic acids. A relatively high TAN (e.g., a TAN of at least 0.3) may make crude oil feed unacceptable for transportation and / or refining. Poor crude oils with relatively high q asphaltene content may show lower stability during processing than other crude oils with relatively low Cs asphaltene content. The contact of the crude oil feed with the second catalyst can remove the acidic constituents of the TAN and / or A asphaltenes from the crude feed. In some specific examples, reducing the I asphaltenes and / or the ingredients that cause TAN may reduce the viscosity of the crude oil feed / total product mixture compared to the viscosity of the crude oil feed. In specific examples, it is used to deal with the stability of one or more combination of crude oil = catalyst described in this article to increase the stability of the catalyst. ”可 〒 '^ In some specific examples of hydrogen for crude oil feed, * Combining the carrier with the metal in column 6: raw second medium” ”can be borrowed from precursors or one or more ☆ And get. catalyst

(例如低於482。〇的化合物的存在下在低於500 °C 未锻燒過的第三種觸媒。“又相=的時間以生成 至少100 〇C这）,士 D ，觸媒前驅物係加熱到 卜士 妗。於特定具體實例令，第=錄雜 每克觸媒中可具有G.G T^ 種觸媒在 0.008至G.G1克之範^ _克，請5至⑽克，或 當用來處理本文中所这的的第15攔元素含量。第三種觸媒 性和穩定性。二體=料時，可表現出顯著的活 種硫化合物的存在下在、U例中’觸媒前驅物係於一或多 第三種觸二=:。。的溫度下加熱。 成分，減少料之TAN的至少—部分 原油產物…二^ 原油進_三種觸媒;接及=原=物_。此外， 相比，其含硫量相當少進料的含硫量 最小淨吸取的原油產物。^具有原油進料之氯的相對 二為至聰之原油進料的含硫量。使用第三:二 所生產的原油產物與原油進料相比，“Π比重、餘八八 量、VGO含量，和殘留物含量方面，也可能只表現::： 79 200535224 少量的變化。降低原油進㈣tan 金屬、Ni/V/Fe含量，及黏产 文金屬鹽形態之 里及黏度且同時只少量改 餾分含量、VGO含量，和殘留曰 Η比重、 1茂自物含罝的能力办 物為各種處理設備所使用。 谷許原油產 第三種觸媒於若干具體實例中可降低 性的職含量，而同時保持原油進料/總產物的：二 ,。於特定具體實例中，第三種觸媒在每 ： 在〇.〇㈣至（M克，議至⑽克，或\中了具有 夕π闽‘ 凡υ·ϋ01至0.01克(For example, a third catalyst that has not been calcined at less than 500 ° C in the presence of a compound below 482. °. "Another phase = time to generate at least 100 ° C this), Shi D, catalyst precursor The material is heated to a pudding. In a specific example, the per-gram catalyst may have GG T ^ catalysts in the range of 0.008 to G. G1 grams of ^ _ gram, please 5 to ⑽ grams, or when used To deal with the content of the 15th element in this article. The third catalyst and stability. When the dimer = material, it can show a significant presence of live species sulfur compounds. The precursor is heated at the temperature of one or more of the third type == .. Composition, reducing at least the TAN of the material-part of the crude oil product ... two ^ crude oil into three kinds of catalysts; then ===== In addition, compared to its relatively low sulfur content, the feedstock has the smallest sulfur content of the net crude oil product. ^ The relative amount of chlorine with crude oil feed is the highest sulfur content of Cong ’s crude oil feed. Use a third : Compared with the crude oil feed, the produced crude oil product, "Π specific gravity, the remaining 88%, VGO content, and residue content, may also only Performance :: 79 200535224 Minor changes. The ability to reduce the tan metal, Ni / V / Fe content of crude oil, and the viscosity and viscosity of metal salts, and at the same time only change the distillate content, VGO content, and the specific gravity of residual tritium, and the content of tritium in natural materials. Materials are used by various processing equipment. Guxu crude oil production The third catalyst can reduce the content of the crude oil in several specific examples, while maintaining the crude oil feed / total product: two. In a specific specific example, the third catalyst is in the range of: 0.001 to (M gram, to gram to gram, or 中 πmin ‘where υ · ϋ01 to 0.01 gram

至:的第6攔金屬含量以及在〇 〇〇〇1至〇 〇5克，〇祕 量第或〇·001至0·01克之範圍内的第⑺欄金屬含 弟6和10攔金屬觸媒可促使減少至少一部分在3〇〇 至5〇〇 °C或350至450 ^之範圍内的溫度和〇]至ι〇 、 至8 MPa，或2至5 MPa之範圍内的壓力下造成 原油進料中之MCR的成分。 ,於特疋具體實例中，第四類觸媒（“第四種觸媒，，）包含To: the content of the 6th metal and the metal in the second column containing the 6th and the 10th metal catalysts in the range of 0.001 to 0.05 g, 0 to 0.001 g, or 0.001 to 0.01 g Can promote reduction of at least a portion of the crude oil feed at temperatures in the range of 300 to 500 ° C or 350 to 450 ^ and pressures in the range of 0] to ι〇, to 8 MPa, or 2 to 5 MPa Ingredients of MCR in the feed. In the specific example, the fourth type of catalyst ("the fourth type of catalyst,") contains

人^氧化鋁載體結合的第5欄金屬。第四種觸媒具有中位 孔k至少為1 80 A的孔徑分佈。於若干具體實例中，第四Column 5 metal bonded to alumina support. The fourth catalyst has a pore size distribution with a median pore k of at least 1 80 A. In several specific examples, the fourth

種觸媒的中位孔徑可至少為220人，至少為230人，至少為 2 5 0 A ’或至少為300人。該載體在每克載體中可包含至少 •克’至少〇·5克，至少〇·8克，或至少〇.9克的Θ氧化 1呂第四種觸媒於若干具體實例中可包含每克觸媒中最多 為0·1克的第5欄金屬，且每克觸媒中至少為0 0001克的 第5搁金屬。於特定具體實例中，第5欄金屬為釩。 於右干具體實例中，在與第四種觸媒接觸之後，原油 80 200535224 進料可與附加觸媒 〜 、妾觸。该附加觸媒可為下列一或多種 者·弟一種觸媒、第— ^ 第五種觸蛘、第弟二種觸媒、第四種觸媒、 。觸據二 觸媒、第七種觸媒、本文中所述的商 口口觸媒，或其組合。 於若干具體實例中，氯可在原油進料 觸期間於300至400 t^The median pore size of these catalysts can be at least 220 people, at least 230 people, at least 250 A 'or at least 300 people. The carrier may contain at least • grams of at least 0.5 grams, at least 0.8 grams, or at least 0.9 grams of Θ oxide 1 gram per gram of the carrier in several specific examples. The fourth catalyst may include per gram in several specific examples. The catalyst has at most 0.1 grams of the fifth column of metal, and each gram of the catalyst has at least 0 0001 grams of the fifth shelf metal. In a specific embodiment, the metal in column 5 is vanadium. In the specific example of the right stem, after contacting with the fourth catalyst, the crude oil 80 200535224 feed can be contacted with additional catalysts ~ and. The additional catalyst may be one or more of the following: a first catalyst, a fifth catalyst, a second catalyst, a fourth catalyst,. Catalyst two, catalyst seven, business catalysts described in this article, or a combination thereof. In some specific examples, chlorine may be between 300 and 400 t ^

U 320 至 380 C，或 330 至 370 °CU 320 to 380 C, or 330 to 370 ° C

n 類接觸所生產的原油產物可具有TAN 最多為90%’最多為8G%，最多為5()%，或最多$跳之 原'由進料的TAN。氫氣發生可在1至50 Nm3/m3，1〇至4〇Crude products produced by n-type contact may have a TAN of at most 90%, a maximum of 8G%, a maximum of 5 ()%, or a maximum of $ 0.1% of the original TAN from the feed. Hydrogen generation can range from 1 to 50 Nm3 / m3, from 10 to 4

Nm3/m3’或15至25 Nm3/m3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%，最多為观， 最多為观，最多為10%，或至少為1%之原油進料的總 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。第五種觸媒具有中位 孔徑至少為180 A，至少為220 A，至少為23〇 A，至少為 250 A，至少為300入，或最多為5〇〇A的孔徑分佈。該載 體在每克載體中可包含至少(M克，至少〇 5 t，或至少 〇·999克的θ氧化铭。於若干具體實例中，載體具有以氧化 鋁含量為每克觸媒中有低於O.i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》^克的第6'欄金 屬，且每克觸媒中至少為0.0001克的第6攔金屬。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31〇 81 200535224 至柳C，320至37〇 t，或33〇至36〇。〇的溫度下接 觸％，原油進料之氫的淨吸取可能相當地低（例如〇 〇1至 100 NmVm3，1 至 80 Nm3/m3，5 至 50 Nm3/m3，或 1〇 至 3〇 Nm3/m3)。原油進料之氫的淨吸取於若干具體實例中可在1 至 20 NmVW，2 至 15 Nm3/m3，或 3 至 1〇 Nm3/m3 的範圍Nm3 / m3 'or 15 to 25 Nm3 / m3. Crude products can have a total Ni / V / Fe content of up to 90%, up to 80%, up to meso, up to meo, up to 10%, or at least 1% of the total Ni / V of the crude feed / Fe content. In a specific embodiment, the fifth type of catalyst ("the fifth catalyst,") includes a column 6 metal in combination with a θ alumina support. The fifth catalyst has a median pore size of at least 180 A, at least 220 A, at least 230 A, at least 250 A, at least 300 A, or a maximum pore size distribution of 500 A. The carrier may contain at least (M g, at least 0.05 t, or Θ oxide at least 999 grams. In some specific examples, the carrier has an alumina content of less than Oi grams per gram of catalyst with alumina content. The catalyst contains per gram in some specific examples. The catalyst has at most ^ grams of the 6 'column metal, and each gram of the catalyst is at least 0.0001 grams of the 6th metal. In some specific examples, the 6th metal is molybdenum and / or tungsten. In the example 'when the crude oil feed and the fifth catalyst are contacted at a temperature of 31〇81 200535224 to Liu C, 320 to 37〇t, or 33.0 to 36.0%, the net absorption of hydrogen from the crude feed May be quite low (e.g. 001 to 100 NmVm3, 1 to 80 Nm3 / m3, 5 to 50 Nm3 / m3, or 10 to 30 Nm3 / m3) Net hydrogen feed oil in the suction range of a number of specific examples may be from 1 to 20 NmVW, 2 to 15 Nm3 / m3, or 3 to 1〇 Nm3 / m3 of

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TAN最多為9〇%，最多為80%，最多為5〇%，或最多為 ίο%之原油進料的TAN。原油產物的TAN可在〇 〇ι至〇 /， 〇·〇3至0.05，或〇 〇2至〇 〇3的範圍内。Inside. The crude oil product produced by contacting the crude oil feed with the fifth catalyst may have a TAN of up to 90%, a maximum of 80%, a maximum of 50%, or a maximum TAN of the crude feed. The TAN of the crude product may be in the range of 0.00 to 0 /, 0.003 to 0.05, or 002 to 2003.

於特定具體實例中，第六類觸媒（“第六種觸媒”）包含 〃 Θ氧化鋁載體結合的第5欄金屬和第6欄金屬。第六種 觸媒具有中位孔徑至少為18〇人的孔徑分佈。於若干具體 實例中，孔徑分佈的中位孔徑可至少為22〇人，至少為 入，至少為250 A，至少為3〇〇人，或最多為5〇〇人;該載 體在每克載體中可包含至少〇·；!克，至少〇·5克，至少I』 克至/ 〇·9克，或最多為〇·99克的㊀氧化銘。該栽體於 若干具體實例中可包含每克觸媒中最多為〇1克之第5欄 金屬和第6欄金屬的總量，且每克觸媒中至少為〇·_ι克 之第5攔金屬和第6攔金屬的總量。於若干具體實例中， 第6攔金屬總量與第5攔金屬總量的莫耳比可在至 ^至10，或2至5的範圍内。於特定具體實例巾，第5欄 金屬為飢而第6欄金屬為鉬及/或嫣。 。當原油進料與第六種觸媒在310至4〇〇它，32〇至37〇 ，或330至360 的溫度下接觸時，原油進料之氫的 82 200535224 及取可在-10 Nm3/m3 至 20 Nm3/m3，_7 Nm3/m3 至 10In a specific embodiment, the sixth type of catalyst (the "sixth type of catalyst") includes the fifth column metal and the sixth column metal combined with 〃 Θ alumina support. The sixth catalyst has a pore size distribution with a median pore size of at least 180 people. In several specific examples, the median pore size of the pore size distribution can be at least 22, at least 250 A, at least 300, or at most 500; the carrier is in each gram of carrier It may contain at least 0.0 g; at least 0.5 g, at least 1 g to / 0.9 g, or at most 0.99 g of arsenic oxide. In some specific examples, the plant may include the total amount of the 5th column metal and the 6th column metal per gram of the catalyst, and the 5th metal and the 5th column metal per gram of the catalyst at least Total amount of 6th metal. In some specific examples, the molar ratio of the total amount of the 6th metal to the total amount of the 5th metal may be in a range from ^ to 10, or 2 to 5. For specific examples, the metal in column 5 is hungry and the metal in column 6 is molybdenum and / or cyan. . When the crude oil feed is in contact with the sixth catalyst at a temperature of 310 to 400, 32 to 37, or 330 to 360, the hydrogen of the crude oil feed is 82 200535224 and can be taken at -10 Nm3 / m3 to 20 Nm3 / m3, _7 Nm3 / m3 to 10

Nm3/m3 ’或·5 Nm3/m3至5 Nm3/m3的範圍内。氫的負值淨 吸取為氫在現場產生的跡象。由原油進料與第六種觸媒接 觸所生產的原油產物可具有TAN最多為90%，最多為80%， 最多為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0·01至01，0 〇2至〇 〇5，或〇 〇3 至〇·〇4的範圍内。 在原油進料與第四種、第五種，或第六種觸媒接觸期 間氫的少量淨吸取會減少在生產輸送及/或處理可接受之原 油產物的加工期間氫的總需求。由於生產及/或輸送氫的成 本昂貴，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（“第七種觸媒，，）具有 第6攔金屬總含量在每克觸媒中有〇 〇〇〇1至〇 〇6克之第6 攔金屬的範圍内。第6欄金屬為鉬及/或鎢。第七種觸媒係 有利於生產具有TAN最多為90%之原油進料的ΤΑΝ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叙述一樣 地製造及/或使用。 遥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 200535224 煉所能接受。 按選擇順序配置兩種或更多種觸媒可控 性質改善順序。舉例而言，原油進 μ進枓的 s ? r 的 TAN、API 比 f、 至少-部分的c5瀝青質、至少一部分的鐵、至 鎳’及/或至少一部分的鈒能在減少原油進料中至少八 的雜原子之前減少。 丨刀 配置及/或選擇觸媒於好具體實例中可提高觸媒“ 及/或原油進料/總產物混合物的穩定性。在加工Nm3 / m3 'or · 5 Nm3 / m3 to 5 Nm3 / m3. Negative net uptake of hydrogen is an indication that hydrogen is generated on site. The crude oil product produced by contacting the crude oil feed with the sixth catalyst may have a TAN of at most 90%, at most 80%, at most 50%, at most 10%, or at least 1% of the crude feed. TAN. The TAN of the crude product may be in the range of 0.01 to 01, 002 to 0.05, or 003 to 0.04. The small net uptake of hydrogen during the contact of the crude feed with the fourth, fifth, or sixth catalyst will reduce the overall hydrogen demand during processing to produce and / or process acceptable crude oil products. Since the cost of producing and / or transporting hydrogen is expensive, minimizing the amount of hydrogen used in the process will reduce the overall processing cost. In a specific embodiment, the seventh type of catalyst ("the seventh type of catalyst,") has a total content of the sixth metal in the sixth metal metal per gram of the catalyst. Within the range. The metal in column 6 is molybdenum and / or tungsten. The seventh catalyst is a crude oil product that is beneficial for the production of TAN with a TAN crude oil feed of up to 90%. The first, second, and third Other specific examples of the fourth, fifth, sixth, and seventh catalysts can also be manufactured and / or used as described elsewhere herein. The catalyst and control operating conditions of this application can be selected remotely. Allows the production of crude oil products with altered TAN and / or selected properties compared to the crude oil feed, while other properties of the crude oil feed are not significantly changed. The resulting crude oil products may have enhanced properties compared to the crude oil feed and are therefore more Conveying and / or refined 83 200535224 Refinery acceptable. Configure two or more catalyst controllable property improvement orders in the order of choice. For example, tan, API ratio f, At least-part of c5 asphaltenes, at least part of镍 to nickel 'and / or at least a part of the plutonium can be reduced before reducing at least eight heteroatoms in the crude oil feed. 丨 knife configuration and / or selection of catalysts can improve the catalyst "and / or crude oil feed in good specific examples Stability of the feed / total product mixture. In processing

觸媒哥命及/或原油進料/她產W ^ 選計/、、，心屋物混合物的穩定性可容許名 觸系統在不更換接觸區中觸媒的情況下，運轉至少3個°， 至少6個月，或至少i年。The catalyst brother's life and / or crude oil feed / her production W ^ Choice / ,,, the stability of the heart-wood object mixture can allow the name touch system to run at least 3 ° without changing the catalyst in the contact area , At least 6 months, or at least i years.

—選定觸媒可在原油進料的其他性f改變之前， :油進料中至少一部分的卿Fe，至少一部分的。瀝 質，至少一部分的有機酸金屬鹽形態之金屬，至少一部 造成TAN的成分，至少一部分的殘留物，或其組合減； 並且同時在加工期間保持原油進料/總產物混合物的穩定 (例如保持高於1.5的原油進料p值）。或者，^瀝青質⑴ 及/或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 加工期間保持原油進料/總產物混合物的穩定性。 於若干具體實例中，第—種觸媒（上述者）可配置在一 連串觸媒的上⑭。第_種觸媒的此種配置可容許移除高分 子里Θ染物、金屬污染物，及/或有機酸金屬鹽形態之金屬， 並且同日寸保持原油進料/總產物混合物的穩定性。 84 200535224 第一種觸媒於若干具體實例中係容許移除原油進料中 至少一部分的Ni/V/Fe，移除酸性成分，移除造成系統中 其他觸媒壽命減短的成分，或其組合。舉例而[與原油 進料相比，減少原油進料/總產物混合物中至少一部分的&amp; 瀝青質會抑制配置於下游之其他觸媒的堵塞，因此會增加5 接觸系統在沒有補充觸媒的情況下仍可運轉的持續時^。 移除原油進料中至少—部分@ Ni/V/Fe於若干具體實例中 可牦加配置在第一種觸媒後面之一或多種觸媒的壽命。-The selected catalyst may be at least a part of Fe, at least a part of the oil feed before the other properties f of the crude feed are changed. Leachate, at least a portion of the metal in the form of a metal salt of an organic acid, at least a portion that causes TAN, at least a portion of the residue, or a combination thereof; and at the same time maintain the stability of the crude oil feed / total product mixture during processing (e.g., Keep the crude p-value above 1.5). Alternatively, the asphaltene and / or API specific gravity can be gradually reduced by the contact of the crude oil feed with the selected catalyst. The ability to progressively and / or selectively change the properties of the crude oil feed can allow the crude oil feed to be maintained during processing. Stability of the feed / total product mixture. In some specific examples, the first catalyst (the above) can be arranged on the top of a series of catalysts. This configuration of the first catalyst allows removal of Θ dyes, metal contaminants, and / or metals in the form of metal salts of organic acids in high molecules, and maintains the stability of the crude oil feed / total product mixture on the same day. 84 200535224 The first catalyst in several specific examples allows the removal of at least a portion of Ni / V / Fe in crude oil feeds, the removal of acidic components, the removal of components that reduce the life of other catalysts in the system, or combination. For example, [compared with crude oil feed, reducing at least a portion of the crude oil feed / total product mixture &amp; asphaltenes will inhibit the clogging of other catalysts arranged downstream, so it will increase 5 contact systems in the absence of supplementary catalyst For the duration of the case ^. Remove at least part of the crude oil feed @ Ni / V / Fe in several specific examples. The life of one or more catalysts configured behind the first catalyst can be increased.

弟一種觸媒及/或第三種觸媒可配置在第一種觸媒的下 游。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3 &amp;里，降低含氧量，及/或降低有機酸金屬鹽形 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，與原油進料 的個別性f相比，其具有降低的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 月貝3里，降低的黏度，或其組合，且同時在加工期 ::保持原油進料/總產物混合物的穩定性。第二種觸媒可並 如配置，第二種觸媒係位於第三種觸媒上游，或者反過來 、使氫輪运至特定接觸區的能力會傾向於使接觸期間氳 :使用減至最小量°結合在接觸期間促使氫氣發生的觸媒 贫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 200535224 進料的同樣性質相比之下@、丄a 才，第四種舖拔、 下原油產物的選定性質。舉例而 。弟四種觸媒可與第一種觸媒 媒、第五種觸媒、第H甘 弟-種觸媒、弟二種觸 以改變原油谁次弟七種觸媒曰併使用 、、由進料的复定性質’而同時只有選擇量地改變原 油進枓的其他性皙， 文你 定性。可選_、 5 5，保持原油進料/總產物的穩 量，同時3Γ的财及7或數目使氫的淨吸取減至最小 二=持原油進料/總產物的穩定性。氯的最小 係使原油進料的殘留物含量、v⑻含量、㈣One kind of catalyst and / or the third kind of catalyst can be arranged downstream of the first kind of catalyst. Further contact of the crude oil feed / total product mixture with the second catalyst and / or the third catalyst can further reduce the TAN, lower the Ni / v / Fe content, lower 3 &amp; mile, lower the oxygen content, and / Or reduce the organic acid metal salt-shaped metal content. ~ 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, which has a reduction compared to the individuality f of the crude oil feed. TAN, reduced sulfur content, reduced oxygen content, reduced metal content in the form of metal salts of organic acids, reduced 3 mils, reduced viscosity, or a combination thereof, and at the same time during the processing period: Stability of the feed / total product mixture. The second catalyst can be configured as such, the second catalyst is located upstream of the third catalyst, or in turn, the ability to transport the hydrogen wheel to a specific contact zone tends to minimize the contact period 氲: use is minimized The amount of catalyst combined with the catalyst that promotes the occurrence of hydrogen during the contact period. The catalyst that absorbs a relatively small amount of hydrogen during the contact period can be used to change the same properties as the crude oil 85 200535224 feed. Selected properties of crude oil products. For example. The four catalysts can be used with the first catalyst, the fifth catalyst, the H Gandi-catalyst, and the second two catalysts to change the crude oil. The complex nature of the raw materials, and at the same time, only the selected quantity can change the other properties of crude oil. Optional _, 5 and 5, to maintain the stability of the crude oil feed / total product, while the 3Γ and 7 or the number minimize the net absorption of hydrogen. Two = hold the stability of the crude oil feed / total product. The minimum amount of chlorine is the residual content, v⑻ content,

比重，或其組合保持 PI 内，而原％ 、 。、原油進料之個別性質的範圍 円而原油產物的TAN及/哎黏谇田夕4 ΤΔΜ η , 袁黏度取多為90%之原油進料 的ΤΑΝ及/或黏度。 卄 減少原油進料之氫 、、4 m：八Τ次取Τ生產具有與原油進料之 沸點分佈類似的沸程分佈 ΤΛΧΤ , ，、席油進料之TAN相比降低 tan的原油產物 降低 的原子H/Ph A ㈣料H/C也可m由進料 皁子Η/e有相當少量的改變。 特疋接觸區中的氫氣發生The specific gravity, or a combination thereof, remains within PI, while the original%,. The range of the individual properties of crude oil feeds. The TAN of crude oil products and / or the viscosity of Tianxi 4 τΔΜη, the Yuan viscosity is mostly 90% of the TAN and / or viscosity of crude oil feeds.卄 Reduce the hydrogen of crude oil feed, 4 m: Eight T-times take T production to have a boiling range distribution similar to the boiling point distribution of crude oil feed ΤΛχΤ, compared to the tan of the crude oil feed to reduce the tan crude oil product. The atomic H / Ph A feed H / C can also be changed slightly by the feed soap Η / e. Hydrogen generation in special contact area

接觸區及/或容許選擇性減少“：：風選擇性添加至其他 實 原油進料的性質。於若干具體 游:㈣可配置在本文中所述的附加觸媒上 期門私？ 5 ;1於其間。11可在原油進料與第四種觸媒接觸 ==生’可將氫輸送至包含附加觸媒的接觸區 达可與原油進料的流動反向 ^ ^ 、右卞具體實例中，虱的輸 廷可與原油進料的流動同向。 舉例而言，在堆疊社爐φ ^ Β， ee ^ 、構中U見如圖2B)，氫可在接觸 間於一接觸區中(例如圖2”的接觸㈣2)生成，氫可 86 200535224 以原油進料流動知 中的接觸區114)。於朴千n輸送至附加接觸區（例如圖2b 料的流動同向。或者右在^體實例中’氯流動可與原油進 ^接㈣戸,次者’在堆登結構中（參見如圖3B)，氫可 在接觸J間於一接_ ^ _ 成。氯源可以原油進料li 中的接觸區1〇2)生 I由進枓流動相反的方向輸 觸區（例如在圖3B巾π斤 、主弟附加接 氫由導管卿添加至接觸區 ::原油進料流動相同的方向輸送至第二附加接觸區 歹口、: 3B中’使氫經由導管1⑽添加至接觸區116)。 使用；第干-體實例中’第四種觸媒與第六種觸媒係並聯 使用，弟四種觸媒係位 ^i 於弟/、種觸媒上游，或者反過來也 yK合第四種觸媒與附加觸媒可在原油進料之氫的少 $淨吸取的情況下，降彳 降低TAN，降低Ni/V/Fe含量，及 降低有機酸金屬鹽形態的旦„ 一 二 J复屬3里。氫的少ϊ淨吸取可容 终原油產物的其他#彳 、 貝/、原油進料的同樣性質相比之下只 有少量改變。 5干〃體實例中，兩種不同的第七種觸媒可合併使 用在上存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 具有等於或大於上游的第七 ' 種觸媒中弟6搁金屬總含量， :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 200535224 進料的同樣性質相比之下只有少量改_如 API比重、殘留物含量、v(j〇入旦， ”’、子3里、 改變）。 3里，或其組合的相當少量 原油進料與上游和下游的第七種 有TAN最多為90〇/，田夕认 牧啊Γ生產具 或至少二1 最多為5°%，最多為1。%， 為/°之原油進料的tan之原油產物 實例中，/§、、山、在企丨y、右干具體 ^進#的TAN可藉由與上游和下游 媒之接觸而逐漸降低(例如，原油進料與 盈原油進料i日μμ目士 /、 ”的接觸以生成 ”原油進枓相比具有改變性質的初 產物與附加觸媒的接觸係產生盘 L接者初原油 性質的斥％ ^i /、初原油產物相比具有改變 原油產物）。漸進式降低TAN的能力可在加 幫靖原油進料/總產物混合物的穩定性。 期間 觸條US具體實例中’觸媒選擇及/或觸媒順序與控制接 == 及/或原油進料流率)的結合可幫助減少原 、曰八物的^的吸取’在加工期間幫助保持原油進料7總產物 ^物的穩定性，並且與原油進料的個別性質相比，改變 物!&quot; 一或多種性質。原油進料/總產物混合物的穩定 史塑a又到來自原/由進料/總產物混合物之各種相分離的 ^。相分離可能由例如原油進料/總產物混合物中原油進 :及/或原油產物的不溶性，原油進料/總產物混合物之瀝 月貝的絮凝，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-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 200535224 產物混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，原油進料可能含有 於加工一開始可溶於原油進料的成分。當原油進料的性質 (例如tan、mcr、C5瀝青質、p值，或其組合）改變時，、 這些成分可能會有變得較不易溶於原油進料/總產物混合物 的傾向。於若干實例中’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 相：傾向於減短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，可能需要重複處理原油進料/總產 物混合物以生產具有期望性質的原油產物。 。在加工期間，可監測原油進料/總產物混合物的p值， 可二估製耘、原油進料，及/或原油進料/總產物混合物的 ^疋典型而5 ’最多為1.5 # P值係表示原油進料之癱 遞青質的絮凝通常會發生。如果p值一開始至少為&quot;，· 而此等P值在接觸期間會增加或相當穩定，那麼這表示原 ^進料在接觸期間相當穩定。原油進料/總產物混合物的穩 疋：’如P值所評估者’可藉由控制接觸條件，藉由觸媒 的選擇，#由觸媒的選擇性排序，或其組合而加以控制。 此種控制接觸條件可包括控帝J LHSV、溫度、壓力、氫的 吸取、原油進料流率，或其組合。 ;若干具體貫例中，控制接觸溫度以便移除C5瀝青質 89 200535224 及/或其他遞青皙，并m 士， 、並同日守保持原油進料的MCR含量。Μ 由氫的吸取及/或鲈古从从 里稽 f 次啟同的接觸溫度降低MCR含量可能會導 成Z相二其可能會降低原油進料/總產物混合物的穩定 3或夕種觸媒的壽命。控制接觸溫度和氮的吸取並 曰本文中所述的觸媒可容許降低q瀝青質而同時只相當 少量地改變原油進料的MCR含量。 ;右干Ί實例中’控制接觸條件以便使-或多個接 觸區中的溫度可為^ g 土Contact area and / or allow selective reduction ":: the nature of wind selective addition to other real crude oil feeds. In a few specific tour: ㈣ Can be configured in the additional catalyst described in this article? In the meantime, 11 can be in contact with the fourth catalyst in the crude oil feed = = 'can produce hydrogen to the contact zone containing additional catalyst Dak and the flow of crude oil feed in the opposite direction ^ ^, in the specific example, The loss of lice can be in the same direction as the flow of crude oil feed. For example, in the stacking furnace φ ^ Β, ee ^, U see Figure 2B), hydrogen can be in a contact zone between contacts (for example Figure 2 "contact ㈣ 2) is generated, hydrogen can 86 200535224 contact zone 114) in the flow of crude oil feed. Yu Qianqian n transported to the additional contact zone (for example, the material flows in the same direction as in Figure 2b. Or in the example of the right side, 'chlorine flow can be connected with crude oil, and the second time' is in the stacking structure (see the figure) 3B), hydrogen can be contacted between contact J. The chlorine source can be contacted in the crude oil feed li. 102) I is fed into the contact area from the opposite direction of the flow (for example, in Figure 3B). The π kg and the younger brother ’s additional hydrogen are added to the contact zone by the conduit pipe: the crude oil feed flows in the same direction to the second additional contact zone gate, and in 3B, the hydrogen is added to the contact zone 116 via the conduit 1). Use; in the example of the stem-body, 'the fourth catalyst is used in parallel with the sixth catalyst system, and the four catalyst systems are located at the upstream of the younger /, or vice versa yK and the fourth These catalysts and additional catalysts can reduce the TAN, reduce the TAN, reduce the Ni / V / Fe content, and reduce the organic acid metal salt morphology in the case of less net absorption of hydrogen from crude oil feed. Belongs to 3. The same properties of other crude oil feedstocks that can absorb the final crude oil product with little absorption of hydrogen are only slightly changed in comparison. 5 In the dried carbohydrate example, two different seventh Catalysts can be used in combination with the seventh catalyst used in the storage, rather than the seventh catalyst downstream, which can have a total metal content of the sixth block in the range of 0.0001 to 0.006 grams per gram of catalyst The seventh downstream catalyst may have a total metal content equal to or greater than that of the seventh seventh upstream catalyst per gram of the seventh downstream catalyst: at least 0.02 grams per gram of the first catalyst The 6th column of the 6 block metal is always contained. In several specific examples, the seventh catalyst upstream and the seventh catalyst downstream The upside down. The ability to use a relatively small amount of catalytically active metals in the seventh catalyst downstream can allow other properties of the crude oil product to be slightly changed compared to the same properties of the crude oil 87 200535224 feed, such as API specific gravity, residue Material content, v (j〇 入 Dan, "', 3 miles, change). 3, or a combination of a relatively small amount of crude oil feed and the seventh upstream and downstream have a TAN of up to 90 //, Tian Xi recognized Mu Γ production tools or at least two 1 up to 5 °%, up to 1. %, In the example of the crude oil product of tan which is a crude oil feed of / °, the TAN of / §, ,, shan, in the enterprise, and right dry concrete ## can be gradually reduced by contact with upstream and downstream media ( For example, the contact between the crude oil feed and the surplus crude oil feed μμμ // ”to produce a“ crude oil feed ”. The contact between the primary product with the changed properties and the additional catalyst produces a plate L with the properties of primary crude oil. Rejection% ^ i /, compared with the crude oil product has a changed crude oil product). The ability to progressively reduce the TAN can contribute to the stability of the Jing crude feed / total product mixture. The combination of 'catalyst selection and / or catalyst sequence and control connection (== and / or crude oil feed flow rate) in the specific example of the US during the period can help reduce the absorption of raw materials and raw materials during processing. The stability of the total product of the crude oil feed 7 is maintained, and compared to the individual properties of the crude oil feed, changes are made to one or more properties. Stability of the crude feed / total product mixture. The sulphur a is again separated from the various phases from the original / by the feed / total product mixture. Phase separation may be caused by, for example, crude oil feed in the crude oil feed / total product mixture: and / or insolubility of the crude oil product, flocculation of crude oil in the crude oil feed / total product mixture, precipitation of components of the crude oil feed / total product mixture, Or a combination thereof. The concentration of crude oil feed and / or total product in the crude oil feed / total product mixture may vary during a certain number of contact periods. When the total product concentration in the crude feed / total 88 200535224 product mixture changes due to the formation of crude products, the solubility of the crude feed ingredients and / or total product components in the crude feed / total product mixture will tend to change. For example, a crude feed may contain ingredients that are soluble in the crude feed at the beginning of processing. When the properties of the crude oil feed (such as tan, mcr, C5 asphaltenes, p-values, or a combination thereof) change, these ingredients may have a tendency to become less soluble in the crude oil feed / total product mixture. In several instances, the &apos; crude feed and total product may form two phases and / or become insoluble with each other. Changes in solubility may also cause the crude feed / total product mixture to form two or more phases. Due to the flocculation of asphaltenes, · changes in the crude oil feed and total product concentration, and / or the composition of the Shen Dian form two phases: tend to reduce the life of one or more catalysts. In addition, process efficiency may be reduced. For example, it may be necessary to repeatedly process the crude feed / total product mixture to produce a crude product with the desired properties. . During processing, the p-value of the crude oil feed / total product mixture can be monitored, and the value of the raw material, crude oil feed, and / or crude oil feed / total product mixture can be estimated, and 5 'is up to 1.5 #P value This means that flocculation of paracyanidin in crude oil feeds usually occurs. If the p-values are at least &quot; at the beginning, and these P-values increase or are fairly stable during the contact, then this means that the original feed is fairly stable during the contact. Stability of the crude feed / total product mixture: 'As assessed by the P value' can be controlled by controlling the contact conditions, by the choice of catalyst, #by the selective ordering of the catalyst, or a combination thereof. Such controlled contact conditions may include Kontron J LHSV, temperature, pressure, hydrogen uptake, crude oil feed flow rate, or a combination thereof. In some specific examples, the contact temperature is controlled in order to remove C5 asphaltenes 89 200535224 and / or others, and the average MCR content of the crude oil feed is maintained. Μ The reduction of MCR content by the hydrogen absorption and / or the reduction of contact temperature from the contact time of the F. may lead to the Z phase. It may reduce the stability of the crude feed / total product mixture Life. Controlling the contact temperature and nitrogen uptake and the catalysts described herein may allow for the reduction of q asphaltenes while at the same time changing the MCR content of the crude oil feed to a relatively small amount. ; In the right drying example, the conditions of the contact are controlled so that the temperature in the contact area or regions may be ^ g soil

▲ 又』為相異者。不同溫度下的操作可容許選擇 性=變原油進料性質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。第一接 觸’皿度為帛接觸區中的溫度。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接 觸區中的飢度。第一接觸溫度可在100至420 °c的範圍内， 第二接觸溫度可在與第一接觸溫度相差2〇至1〇〇艽，％▲ Another "is different. Operation at different temperatures may allow selectivity = change the nature of the crude feed 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 first degree of contact is the temperature in the contact area. Other contact temperatures (e.g., second temperature, third temperature, fourth temperature, etc.) are the levels of starvation in the contact area disposed behind the first contact area. The first contact temperature may be in the range of 100 to 420 ° C, and the second contact temperature may be 20 to 100 ° C different from the first contact temperature,%

至90 C，或40至60 °C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Cs瀝青質含量與原油進料的 TAN及/或C5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 °c，第二接觸溫度可為300 °c。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 90 200535224 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1 〇 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（：5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。 f施例1.擊備觸嫫載艚。 載體係利用585克的水和8克的冰硝酸將576克的氧 化鋁（Criterion Catalysts and Technologies LP，MichiganTo 90 C, or 40 to 60 ° C. In some specific examples, the second contact temperature is greater than the first contact temperature. Having different contact temperatures can reduce the TAN and / or Cs asphaltene content in the crude oil product to the ratio of the TAN and / or C5 asphaltene content of the crude oil feed, if any, between the first and the first When the two contact temperatures are the same or different from each other by 10, the TAN and / or c5 asphaltenes are reduced to a greater extent. For example, the first contact area may include a first catalyst and / or a fourth catalyst, and the second contact area may include other catalysts described herein. The first contact temperature may be 350 ° c, and the second contact temperature may be 300 ° c. The contact of the crude oil feed with the first catalyst in the first contact zone and / or with the fourth catalyst at a higher temperature before contacting with other catalysts in the second contact zone 90 200535224 This results in more tan and / or (: 5) reductions in tan and / or c5 asphaltenes in the same crude feed when the first and second contact temperatures differ by less than 10 ° C in the crude feed. Reduction of asphaltenes. Examples The following presents non-limiting examples of carrier preparation, catalyst preparation, and a system with selected catalyst configurations and controlled contact conditions. FExample 1. Prepared for contact loading. The carrier system uses 585 Grams of water and 8 grams of glacial nitric acid will make 576 grams of alumina (Criterion Catalysts and Technologies LP, Michigan

City，Michigan，U.S.A·)研磨35分鐘製備。所得到的研磨 混合物係透過1.3 1^1〇匕61^模板擠出，於90至125 °C之 間乾燥，接著在918 °C下煅燒，得到650克具有中位孔徑 為I82 A的取燒載體。將此锻燒載體放入Lin(jb erg爐中。 使爐溫於1 · 5小時過程中升到1 〇 〇 〇至η 〇 〇。〇，然後保持 在此範圍内2小時以生產載體。此載體在每克載體中包含 0.0003克的γ氧化鋁，0.0008克的α氧化紹，〇〇2〇8克的谷 氧化鋁，和0.9781克的θ氧化鋁，其藉由χ射線繞射測定。 此載體具有110 m2/g的表面積和0·821 cm3/g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 A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。 200535224 飢觸媒係以下列方式_ , _ ^ 卜 』万式製備。由實施例1所述之方法製 的氧化銘載體用飢浸潰溶液浸潰，其藉由結合Μ克的 :一 82克的去離子水而製備。該溶液的ρΗ值為2•幻。 氧化鋁載體(1〇〇 g)係利用釩浸潰溶液浸潰，以偶然攪 =化2小日守，於125 °C下乾燥數小時，接著在48〇它 70 2 ^ ^所得觸媒在每克觸媒中含有0.04克的釩， =餘部分為載體。此鈒觸媒具有中位孔徑&amp; 35() A的孔徑 布〇·69 cm /g的孔體積，和i 1〇 m2/g的表面積。此外，_ 釩觸媒的孔徑分佈中有66·7%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5攔觸媒。City, Michigan, U.S.A.) was prepared by milling for 35 minutes. The obtained grinding mixture was extruded through a 1.3 1 ^ 61 die template, dried at 90 to 125 ° C, and then calcined at 918 ° C to obtain 650 g of sintered with a median pore size of I82 A. Carrier. This calcined support was put in a Linberger furnace. The temperature of the furnace was raised to 1000 to η 〇 over the course of 1.5 hours, and then kept in this range for 2 hours to produce a support. This The carrier contained 0.0003 g of gamma alumina, 0.0008 g of alpha alumina, 0.0002 g of alumina, and 0.9781 g of theta alumina per gram of the carrier, which were determined by X-ray diffraction. The carrier has a surface area of 110 m2 / g and a total pore volume of 0.82 cm3 / g. This carrier has a pore size distribution with a median pore size of 232 A, and 66.7% of the total pore size in the pore size distribution is within 85 A. Pore size within the range of pore size. This example illustrates how to prepare a carrier with a pore size distribution of at least 180 people and containing at least 0.1 g of Θ alumina. 200535224 The catalyst was prepared in the following manner. The oxide carrier prepared by the method described in Example 1 was impregnated with a starvation solution, which was prepared by combining M grams of: 82 grams of deionized water. The pH value of the solution was 2 • magic. Oxidation The aluminum support (100 g) was impregnated with a vanadium impregnation solution and accidentally stirred for 2 hours. It is dried at 125 ° C for several hours, and then the catalyst obtained at 48 ° C 70 2 ^ ^ contains 0.04 g of vanadium per gram of catalyst, and the remainder is the carrier. This rhenium catalyst has a median pore diameter &amp; 35 () The pore volume of A is 0.69 cm / g, and the surface area of i 10m2 / g. In addition, 66.7% of the pore size distribution of the vanadium catalyst has a total number of pores in A Pore size in the range of potential pore size. This example illustrates the preparation of a fifth catalyst with a pore size distribution with a median pore size of at least 23A.

俊JUL觸媒。 翻觸媒係以下列方式製備。由實施例1所述之方法製 備的氧化鋁載體用鉬浸潰溶液浸潰。此鉬浸潰溶液係藉由 結合 4.26 克的（ΝΗ4)2Μ〇207、6·38 克的 Mo〇3、1.12 克的 30% Η2〇2、〇·27克的單乙醇胺（MEA)，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。 氧化鋁載體（100克）係利用鉬浸潰溶液浸潰，以偶然授 動老化2小時，於125 °C下乾燥數小時，接著在480 〇c 92 200535224 下煅燒2小時。所得觸媒在每克觸媒中含有〇〇4克的銦， 其餘部分為載體。此鉬觸媒具有中位孔徑為25〇人的孔徑 分佈’ 0.77cmVg的孔體積，和U6m2_表面積。此外， 翻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23〇人之孔徑 分佈的第6欄觸媒。 免^例4·~數備具有中位少為23〇 A之孔徑分 目/釩觸媸。 銦/釩觸媒係以下列方式製備。由實施例i所述之方法 製備的氧化鋁載體用如下製備的鉬/叙浸潰溶液浸潰。第一 種溶液係藉由結合2· 14克的（ΝΗ4)2Μ〇2〇7、3 21克的M〇〇3、 .56克的30/〇過氧化氫（h2〇2)、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v〇s〇4與4〇克的去 離子水而製造。使第—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82 mi以產生鉬/釩浸 潰溶液。將氧化㈣鉬/飢浸潰溶液浸潰，以偶然授動老化 J時於I25 C下乾燥數小時，接著在48〇 下锻燒2 小時。所得觸媒在每克觸媒中含有〇〇2克的飢和〇〇2克 的鉬，其餘部分為載體。此鉬/釩觸媒具有中位孔徑為3⑻人 的孔徑分佈。 此實施例說明製備具有中位孔徑至少為23〇人之孔徑 93 200535224 分佈的第6欄金屬和第5攔金屬觸媒。 __愿三種觸媼的轰觸。 、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_gnd，stanf〇rd atenals’ Aliso Viejo，CA)而形成。咸信此種碳化矽如果 有的话，在本文中所述的操作條件下具有低的催化性質。Jun Jul catalyst. The catalyst was prepared in the following manner. The alumina support prepared by the method described in Example 1 was impregnated with a molybdenum impregnation solution. This molybdenum impregnation solution was prepared by combining 4.26 g (NΗ4) 2MO207, 6.38 g Mo03, 1.12 g 30% Η202, 0.27 g monoethanolamine (MEA), and 6.51 Grams of deionized water are prepared as 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 pH of this solution was 5.36. Adjust the solution volume to 82 mL with ionized water. The alumina carrier (100 g) was impregnated with a molybdenum impregnation solution, aged by accident for 2 hours, dried at 125 ° C for several hours, and then calcined at 480 ℃ 92 200535224 for 2 hours. The obtained catalyst contained 0.001 g of indium per gram of the catalyst, and the remainder was a carrier. This molybdenum catalyst has a pore volume with a median pore size of 25 mm and a pore volume of 0.77 cmVg, and a surface area of U6m2. In addition, 67.7% of the total pore number in the pore size distribution of the flip-flop catalyst has a pore size within the range of% A median pore size. This example illustrates the preparation of a column 6 catalyst having a pore size distribution with a median pore size of at least 23 people. Exemption Example 4 · ~ Data preparation has a pore size mesh / vanadium contact with a median of less than 230 A. The indium / vanadium catalyst was prepared in the following manner. The alumina support prepared by the method described in Example i was impregnated with a molybdenum / syllable immersion solution prepared as follows. The first solution was obtained by combining 2.14 grams of (ΝΗ4) 2MO207, 3 21 grams of M03, .56 grams of 30 / 〇hydrogen peroxide (h2O2), 0.14 Monoethanolamine (mea) is produced as a slurry with 3.28 grams of deionized water. This slurry was heated to 65 C until the solids were dissolved. The heating solution was allowed to cool to room temperature. The second solution was made by combining 3.57 grams of VS04 and 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 82 mi to produce a molybdenum / vanadium immersion solution. The molybdenum oxide / hungry immersion solution was impregnated, aged by accidental induction, and dried at I25 C for several hours, and then calcined at 48 ° C for 2 hours. The obtained catalyst contained 0.02 g of hunger and 0.02 g of molybdenum per gram of catalyst, and the remainder was a carrier. This molybdenum / vanadium catalyst has a pore size distribution with a median pore size of 3 mm. This example illustrates the preparation of a column 6 metal and a 5th metal catalyst with a median pore size of at least 230 persons. __ May the three tumbling touches. The tube reactor equipped with a temperature measuring sleeve in the center is equipped with a thermocouple to measure the temperature of the entire catalyst bed. This catalyst bed is formed by filling the space between the temperature measuring sleeve and the inner wall with a catalyst and silicon carbide (20_gnd, stanford atenals' Aliso Viejo, CA). It is believed that this silicon carbide, if any, has low catalytic properties under the operating conditions described herein.

在將混合物放入反應器的接觸區部位之前，使所有觸媒與 等體積量的碳化矽摻合。 、 ^反應器的原油進料流動係由反應器的頂部至反應器的 底^ &lt;化_係配置在反應器的底部作為底部載體。底部 的觸媒/碳切混合物（42咖3)係§己置在該碳化石夕上方以形 成底部接觸區。底部觸媒具有巾位隸為Μ A的孔徑分 2該孔徑分佈中冑66·7%的總孔數具有纟2q A之中位孔 k fc圍内的孔徑。該底部觸媒在每克觸媒中含冑G O%克 勺鉬和0.025克的鎳’其餘部分為氧化鋁載體。Prior to placing the mixture in the contact zone of the reactor, all catalysts were blended with an equal volume of silicon carbide. The crude oil feed flow of the reactor is from the top of the reactor to the bottom of the reactor, and is arranged at the bottom of the reactor as a bottom carrier. The catalyst / carbon-cut mixture at the bottom (42c3) has been placed above the carbonized fossil to form the bottom contact area. The bottom catalyst has a pore size of 2 μA. 2 The total number of holes in this pore size distribution is 66.7%. The bottom catalyst contains 胄 G O% grams of molybdenum and 0.025 grams of nickel 'per gram of catalyst and the rest is an alumina carrier.

。中間的觸媒/石反化矽混合物。6⑽”係配置在底部接觸 區上方以形成中間接觸區。中間觸媒具有中位孔徑為％ a. Catalyst / Stone Reverse Silica Mixture in the middle. "6⑽" is arranged above the bottom contact area to form an intermediate contact area. The intermediate catalyst has a median aperture of% a

的孔從分佈’該孔徑分佈中有66.7%的總孔數具有在24 A 之中位孔徑範圍向&amp; π &quot; 圍内的孔徑。該中間觸媒在每克觸媒中含有 • 02克的錄和古 •克的翻，其餘部分為氧化紹載體。 品項邵的觸媒/碳化石夕混合物（42 cm3)係配置在中間： Q上方以形成頂部接觸區。頂部觸媒具有中位孔徑為 的孔控分佈，在各古 母克觸媒中含有〇_〇4克的鉬，其餘部^ 94 200535224 要為γ氧化銘載體。 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1小時過程中提高到2〇4（4〇〇) 並且保持在204 下2小時。保持在2〇4 °c下之後，接 觸區以每小時10 °C (50 T)的速率逐漸提高到316 (600 °F)。使接觸區保持在316 °C下一小時，於1小時過 程中逐漸升到370 X： (700 T)並且保持在370它下兩小 時。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它 (200 ρ)下，於烘箱中加熱12至24小時以生成具有摘要 於表1，圖7之性質的原油進料。將原油進料饋入反應器 頂部。原油進料係流過反應器的預熱區、頂部接觸區、中 間接觸區、底部接觸區和底部載體。原油進料係於氫氣存 在y與每一種觸媒接觸。接觸條件如下··氫氣與供應至反 應器之原油進料的比率為328 NmVm3 (2〇〇〇 scfb)，lhsv 為lh ，及壓力為69 MPa (1〇14·7㈣）。三個接觸區係加 熱至370。(： （700 T)並且保持在37〇 1下5〇〇小時。三The distribution of pores is 66.7% of the total number of pores in the pore size distribution. The pores have pore sizes within a range of 24 A from the median pore size to &amp; π &quot;. The intermediate catalyst contains • 02 grams of Lu and Gu • grams per gram of catalyst, and the rest is an oxide carrier. The item Shao's catalyst / carbon fossil evening mixture (42 cm3) is arranged in the middle: above Q to form the top contact area. The top catalyst has a pore-controlled distribution with a median pore size of. The ancient catalyst contains 0.14 g of molybdenum, and the rest ^ 94 200535224 is a gamma oxide carrier. 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 in the contact zone was increased to 204 (400) over a period of 1 hour and held at 204 for 2 hours. After being held at 204 ° C, the contact zone gradually increased to 316 (600 ° F) at a rate of 10 ° C (50 T) per hour. Keep the contact zone at 316 ° C for one hour, gradually increase to 370 X: (700 T) over 1 hour and keep it at 370 for two hours. Allow the contact area to cool to ambient temperature. The crude oil from the Mars rig in the Gulf of Mexico was filtered, and then heated at 93 ° (200 ρ) in an oven for 12 to 24 hours to produce a crude oil feed having the properties summarized in Table 1, Figure 7. The crude feed is fed to the top of the reactor. The crude oil feed flowed through the preheat zone, top contact zone, middle contact zone, bottom contact zone, and bottom support of the reactor. The crude oil feed was contacted with each catalyst in the presence of hydrogen. The contact conditions were as follows: The ratio of hydrogen to the crude oil feed to the reactor was 328 NmVm3 (200 scfb), lhsv was lh, and the pressure was 69 MPa (1014 · 7 Torr). Three contact zones were heated to 370. (: (700 T) and held at 3701 for 5000 hours. Three

個接觸區的溫度係接著以下列順序增加和保肖·· Μ C F) 500小時，接著為388 °C (730卞）500小時， 95 200535224 接著為 390 °c (734 °F ) 1800 小時，接著為 394 °C (742 °F ) 2400 小時。 總產物（換言之為原油產物和氣體）離開觸媒床。將總 產物導入氣液相分離器。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。原油產物係定 期分析以測定原油產物成分的重量百分率。所列結果為成 分之實測重量百分率的平均值。原油產物性質係摘要於圖 7的表1中。 如表1所示，原油產物在每克原油產物中具有〇 〇〇75 克的含硫量’ 0·255克的殘留物含量，0.0007克的含氧量。 原油產物具有MCR含量與I瀝青質含量的比率為ι·9及 〇·〇9的TAN。鎳和飢的總量為22_4 wtppm。The temperature of each contact zone was then increased in the following order and Baoshao ·· M CF) for 500 hours, followed by 388 ° C (730 卞) for 500 hours, 95 200535224 followed by 390 ° c (734 ° F) for 1800 hours, then 394 ° C (742 ° F) for 2400 hours. The total products (in other words, crude oil products and gases) leave the catalyst bed. The total product was introduced into a gas-liquid 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 products are periodically analyzed to determine the weight percent of crude oil product components. The results listed are averages of the measured weight percentages of the components. Crude product properties are summarized in Table 1 of FIG. As shown in Table 1, the crude oil product had a sulphur content of 0.075 grams per gram of crude oil product and a residue content of 0.255 grams and an oxygen content of 0.0007 grams. The crude product had TANs with a ratio of MCR content to I asphaltene content of ι · 9 and 〇09. The total amount of nickel and hunger is 22-4 wtppm.

觸媒哥命係藉由測量加權平均床溫度（“WABT”）對原: 進料的運轉時間而決定。觸媒壽命可能與觸媒床的溫度; 關咸^當觸媒壽命減短時，WABT會增加。圖8為本』 施例中所述用於改善接觸區中的原油進料之對時丨 (t )的圖不。曲線130係表示三個接觸區的平均WABt : 原油進料與頂部、中間，和底部觸媒接觸之運轉時間的; 數於大多數的運轉時間過程中，接觸區的WABT僅改! 约20 C。從相當穩定的Wabt來看，可判斷觸媒的催 活性並未受到影響。典型而言，3〇〇〇至35〇〇小時的中丨 工廠運轉時間與1年的工業操作相關。 此實施例說明在控制接觸條件的情況下，使原油進; 96 200535224 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90至1 80 A範圍内之孔徑分佈， 該孔徑分佈中至少60〇/〇的總孔數具有在45 A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i 之原油進料的該等性質。 _ t ^ Μ Ai_有中位孔徑介於 Qn 总圍内之孔徑的兩種觸嫫之接觸。 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所述者相同。每_種觸媒係與等體積的碳 混合。 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。該反應器係以下列方式由底部填充至頂部。碳：石夕· 係配置在反應器的底部作為底部載體。底部的觸媒/碳化石夕 混合物（80…係配置在該碳化石夕上方以形成底部接觸 區。底部觸媒具有中位孔徑$ m A的孔徑分佈，該孔和 分佈中有66.7%的總孔數具有在32 A之中位孔徑以： 徑。該底部觸媒在每克觸媒中包纟〇11克的師⑽ 的鎳，其餘部分為載體。 · 見 頂部的觸媒/碳化石夕混合物（80 cm3)係配置在底部接觸 97 200535224 =:佈形成:::接觸:。頂部觸媒具…孔徑為㈣ 之…-二Γ:有66.7%的總孔數具有… 克的鎳和0.12克的二：部觸媒在每克觸媒中包含0·03 在第-接觸區上：:填充二分為氧化銘。W F 、工位並且作為預熱區。觸媒床係 :邱：二叫爐’其包括對應於預熱區、兩個接觸區，及 底&quot;卩載體的四個加熱區。The catalyst's life is determined by measuring the weighted average bed temperature ("WABT") versus the operating time of the feed. The catalyst life may be related to the temperature of the catalyst bed; Guan Xian ^ When the catalyst life is shortened, WABT will increase. FIG. 8 is a diagram (t) of improving the pairing of crude oil feed in the contact zone described in the embodiment. Curve 130 represents the average WABt of the three contact zones: the running time of the crude oil feed in contact with the top, middle, and bottom catalysts; during most of the running time, the WABT in the contact zone changed only! About 20 C . From the relatively stable Wabt, it can be judged that the catalytic activity of the catalyst was not affected. Typically, between 3,000 and 35,000 hours of operation are associated with one year of industrial operation. This example shows that under the condition of controlling the contact, the crude oil is allowed to enter; 96 200535224 is in 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 in the range of 90 to 1 80 A Pore size distribution, the total pore number of at least 60/0 in this pore size distribution has additional catalyst contact with a pore size in the 45 A median pore size range 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 These properties of the crude oil feed from 0% to i. _ t ^ Μ Ai_ There are two types of contacts that have a median pore diameter within the pore diameter of Qn. The reactor equipment (except the number and content of the contact zones), the catalyst-forming sulfide method, the method for isolating the total product, and the method for analyzing the crude product are the same as those described in Example 5. Each catalyst is mixed with an equal volume of carbon. 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. Carbon: Shi Xi is arranged at the bottom of the reactor as a bottom carrier. The catalyst / carbonite mixture at the bottom (80 ... is arranged above the carbonite to form the bottom contact area. The bottom catalyst has a pore size distribution with a median pore size of $ m A, and 66.7% of the pores and distributions have a total The number of pores has a median pore diameter of 32 A. The diameter of the bottom catalyst is 0.001 g of nickel in the catalyst per gram of catalyst, and the rest is the carrier. The mixture (80 cm3) is arranged at the bottom to contact 97 200535224 =: cloth formation :: contact: the top catalyst ... the hole diameter is ㈣ ...-two Γ: there is 66.7% of the total number of holes with ... grams of nickel and 0.12 The second gram: The catalyst contains 0.03 per gram of the catalyst. On the first contact area :: Filled with two divided oxidized inscriptions. WF, station and as a preheating zone. Catalyst bed system: Qiu: Second call The furnace 'includes four heating zones corresponding to a preheating zone, two contact zones, and a bottom &quot; carrying carrier.

r具有摘要於表2,圖9之性質的BS-4原油（Venezuela) 糸供給入反應器頂部。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:與每-種觸媒接觸。接觸條件如下：氯氣與供應至 反應器之原/由進料的比率為16〇 (1〇〇〇 scfb)， [HSV為1 h ’及壓力為6 9 Mpa 〇〇14 7 _)。兩個接觸 區係加熱至260 °C (5〇〇卞）並且保持在260。(： （500 T) 下287小日寸。兩個接觸區的溫度係接著以下列順序增加和r A BS-4 crude oil (Venezuela) with the properties summarized in Table 2 and Figure 9 was fed to the top of the reactor. Crude oil feeds flow through the preheat zone, top contact zone, bottom contact zone, and bottom carrier of the reactor. The crude oil feed is based on the presence of hydrogen: in contact with each catalyst. The contact conditions were as follows: the ratio of chlorine gas to the original / source feed to the reactor was 160 (1000 scfb), [HSV was 1 h ', and the pressure was 69 Mpa 0014 7 _). The two contact zones were heated to 260 ° C (500 ° F) and maintained at 260. (: 287 small inches at (500 T). The temperature of the two contact zones is then increased in the following order and

保持：270 °C (525 T)190 小時，接著為 288 t (55〇 τ) 216小時，接著為315 °C (600 T ) 360小時，接著為343 °C (650 °F ) 120小時，以達到丨173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 API比重。該原油產物在每克原油產物中含有〇.〇〇23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 200535224 180 A範圍内之孔徑分Hold: 270 ° C (525 T) for 190 hours, followed by 288 t (55〇τ) for 216 hours, then 315 ° C (600 T) for 360 hours, and then 343 ° C (650 ° F) for 120 hours. Reached a total operating time of 173 hours. The total product left the reactor and was separated as described in Example 5. Crude products have an average TAN of 0.42 and an average API specific gravity of 12.5 during processing. This crude product contained 0.0023 g of sulfur, 0.0034 g of oxygen, 0.441 g of VGO, and 0.378 g of residue per gram of crude product. Additional properties of the crude product series are shown in Table 2 of FIG. This example shows a crude oil feed with a median pore size between 90 and 98 200535224 180 A.

命広^ 承得觸以生產原油產物，JL 人原油進料的性質相比，且 八 八旦β，、有降低的丁AN，降低的Ni/V/FeDestiny ^ Chengde touch to produce crude oil products, compared to the properties of JL human crude oil feed, and have a lower denier β, reduced Ding AN, reduced Ni / V / Fe

八曰&amp; 原，由產物的殘留物含量和VGO 含…料和職之原油進料的個別性質。 反應器設備(除了接觸區的數目和内容以外）、觸媒、 總產物分離法、原油產物分析 :、 實施例6所述者相同。 觸料成、化物法係與 具有摘要於表3，圖1〇之柯哲f 口之1的原油進料（BC-10原油） 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。接觸條件如下··氫 氣與供應至反應器之原油進料的…8〇 Nm3/m3 (5〇〇 SCFB)，LHS^ 2 y，及壓力為 69 奶（ι〇ΐ47 ㈣。 兩個接觸區係逐漸加熱i 343(65〇。&quot;。總運轉時間 為1 0 0 7小時。 原油產物在加工期間具有016的平均tan和16 2的 平均API比重。該原油產物含有i 9卿㈣㈣，6糾啊 的納，0.6 wtppm的鍅，知 1^ f和3 wtPPm的鉀。該原油產物在 每克原油產物中含有0.0033克的硫，G.⑽2克的Λ，Ο」％ 克的VGO，和〇·401克的殘留物。原油產物的額外性 列於圖10的表3中。 、Μ 此實施例顯示使原油進料與具有孔徑分佈在9〇至ΐ8〇 Α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 ’降低的總約、鈉、鋅，和鉀含量，而原油產物的 99 200535224 含硫量、VGO含量和殘留物含量為76%、94%和103%之 原油進料的個別性質。 1_施例8至11._星油進料與四種觸媒系統在各種接 Μ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 分析係與實施例5所述者相同。除另有說明外，所有觸媒 係以2份碳化矽對1份觸媒的體積比與碳化矽混合。通過 母個反應裔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 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。 於實施例8中，未煅燒過的鉬/鎳觸媒/碳化矽混合物（48 cm )係配置在底部接觸區中。該觸媒在每克觸媒中包含 〇·146克的钥，〇·〇47克的鎳，和〇〇21克的磷，其餘部分 為氧化鋁載體。 山包含具有中位孔徑為18〇 Α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。該鉬觸 媒具有每克觸媒中含0·04以目的總含#，其餘部分為包含 每克載體中至少為〇·5〇克γ氧化鋁的載體。 於實施例9中，未煅燒過的鉬/鈷觸媒/碳化矽混合物（48 100 200535224 cm3)係配置在兩個接觸區中。 〇·143克的鉬，0.043克的鈷 為氧化鋁載體。 该未煅燒過的鉬/鈷觸媒包含 和0.021克的磷，其餘部分 錮觸媒/碳化矽混合物(12 cm3)係配置在頂部接觸區 中。該鉬觸媒與實施例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 觸媒係與碳化石夕混合並配置在兩個接觸區中⑽⑽3)。The original &amp; raw material is composed of the residual content of the product and the individual properties of the VGO-containing crude oil feedstock. Reactor equipment (except for the number and content of contact zones), catalyst, total product separation method, crude oil product analysis :, the same as described in Example 6. The feedstock formation, chemical reaction system, and crude oil feed (BC-10 crude oil) with Kezhe port 1 as summarized in Table 3, Figure 10, were fed into the top of the reactor. Crude oil feeds flow through the preheat zone, top contact zone, bottom contact zone, and bottom carrier of the reactor. The contact conditions are as follows: · Hydrogen and crude oil supplied to the reactor ... 80Nm3 / m3 (500SCFB), LHS ^ 2y, and pressure of 69 milk (ι〇ΐ47㈣). Two contact zones Gradually heat i 343 (65 0. &quot;. The total operating time is 10 7 hours. The crude product has an average tan of 016 and an average API specific gravity of 16 2 during processing. The crude product contains i 9 9, 6 纠Ah Na, 0.6 wtppm osmium, 1 ^ f and 3 wtPPm of potassium. This crude product contains 0.0033 grams of sulfur per gram of crude product, G. 2 grams of Λ, 0 "% of VGO, and 〇 · 401 grams of residue. The additionality of the crude product is shown in Table 3 of Figure 10. This example shows that the crude feed was contacted with a selected catalyst having a pore size distribution in the range of 90 to ΐ80A. To produce crude oil products with reduced TAN ', reduced total sodium, sodium, zinc, and potassium content, while the crude oil product's 99 200535224 sulfur content, VGO content, and residue content are 76%, 94%, and 103% Individual properties of crude oil feed. 1_Examples 8 to 11._ Star oil feed and four catalyst systems under various conditions Each reactor equipment (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 described in Example 5. Unless otherwise stated, all catalysts are mixed with silicon carbide in a volume ratio of 2 parts silicon carbide to 1 part catalyst. The crude oil feed flow through the parent reactor is from the top of the reactor to the bottom of the reactor. The silicon carbide system is arranged at the bottom of each reactor as a bottom carrier. Each reactor has a bottom contact area and a top contact area. After the catalyst / carbide carbide mixture is placed in the contact area of each reactor, the silicon carbide system is It is arranged above the top contact zone to fill the empty space and serves as a preheating zone for each reactor. Each reactor is charged into a Lindberg furnace, which includes four heatings corresponding to the preheat zone, two contact zones, and the bottom carrier In Example 8, an uncalcined molybdenum / nickel catalyst / silicon carbide mixture (48 cm) was arranged in the bottom contact zone. The catalyst contained 0.146 g of key per gram of catalyst, 0.007 g of nickel And 〇21g of phosphorus, the rest is alumina support. A molybdenum catalyst / silicon carbide mixture (12 cm3) containing a catalyst with a pore size distribution of a median pore size of 18OA is arranged in the top contact zone. The molybdenum catalyst has a total content of 0.04 for each gram of the catalyst, and the remainder is a carrier containing at least 0.50 g of gamma alumina per gram of the carrier. In Example 9, it was not calcined. The used molybdenum / cobalt catalyst / silicon carbide mixture (48 100 200535224 cm3) was arranged in two contact areas. 0.1143 g of molybdenum and 0.043 g of cobalt were used as alumina support. The uncalcined molybdenum / cobalt catalyst contained and 0.021 g of phosphorus, and the remaining hafnium catalyst / silicon carbide mixture (12 cm3) was arranged in the top contact area. The molybdenum catalyst is the same as that in the top contact region of Example 8. In Example 10, the molybdenum catalyst system as described in the top contact region of Example 8 was mixed with the carbonized carbide and arranged in the two contact regions (3).

;實轭例11中，未锻燒過的鉬/鎳觸媒/碳化矽混合物 (48 cm )係配置在底部接觸區中。該未锻燒過的翻/錄觸媒 在每克觸媒中包含〇·〇9克的錮，〇〇25克的鎳，和。別克 的石4，其餘部分為氧化鋁載體。 翻觸媒7碳化@混合物（12⑽3)係配置在頂部接㈣ 中。该鉬觸媒與實施例8之頂部接觸區者相同。 過濾來自Mars鑽臺（Gulf〇fMexic〇)的原油，接著在9 ? (200卞)下，於烘箱中加熱12至24小時以生成用於負In the actual yoke example 11, an uncalcined molybdenum / nickel catalyst / silicon carbide mixture (48 cm) was arranged in the bottom contact area. The unfired ripping / recording catalyst contained 0.09 g of gadolinium, 0.25 g of nickel, and 1 g of the catalyst. Buick Stone 4, the rest is alumina support. Fancatalyst 7Carbonization @ Mixture (12⑽3) is arranged in the top joint. The molybdenum catalyst is the same as that in the top contact region of Example 8. Filter the crude oil from the Mars rig (Gulf〇fMexic〇), and then heat in an oven at 9? (200 卞) for 12 to 24 hours to generate

軛例8至1 1之具有摘要於表4 ’圖&quot;之性質的原油進料。 =原油進料供給人此等實施例的反應器頂部。原油進料痛 …、£ 頂邛接觸區、底部接觸區和底部截 體。原油進料&gt;f系；^ _ g 、、飞乳存在下與母一種觸媒接觸。每 施例的接觸條件如下· # &quot; t 貝 干女下·虱氣與接觸期間之原油進料的比 為160 NmVm3 (1〇〇〇 Scfb)，及每個系統的總壓力為6( 3 (1014.7 PS1)。在接觸的前200小時期間，LHSV為2 ( h·1，而接著在剩下的接觸時間LHSV降低至ι 〇…。所右 接觸區的溫度為^ c (650 °F)接觸500小時。在5〇( 101 200535224 小時後，所有接觸區的溫度係控制如下：使接觸區的溫度 升到354 °C (670 T )，保持在354 °C下200小時；升到 3 66 °C (690 °F)，保持在 366 °C 下 200 小時；升到 371。〇 (700 °F)，保持在 371 °C 下 1000 小時；升到 385 〇c (725 F)’保持在385 C下200小時：然後升到3 99 °C (750 °F ) 的最終溫度並保持在399 r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11所生產之原油產物性質的平均值係列於w i i的表5 中0 Μ㈣研ς ,g、〉田座欺 Ρ值（“Ρ”）對運轉時間（“t”）的圖示。原油進料且有至少 的p值。曲線14〇、142、144，和146係表示藉由使肩 :科個別與實施例8至n的四種觸媒系統接 到The yoke examples 8 to 11 are crude oil feeds having the properties summarized in Table 4 &apos; Figure &quot;. = The crude oil feed is supplied to the top of the reactor in these examples. Crude oil feed pain ..., top contact area, bottom contact area, and bottom frustum. Crude feed &gt; f series; ^ _ g, contact with a catalyst in the presence of flying milk. The contact conditions for each example are as follows: # &quot; t Begheimer's · The ratio of lice gas to the crude oil feed during contact is 160 NmVm3 (100 Scfb), and the total pressure of each system is 6 (3 (1014.7 PS1). During the first 200 hours of the contact, the LHSV was 2 (h · 1, and then the remaining contact time LHSV decreased to ι 〇... The temperature of the right contact zone was ^ c (650 ° F) Contact for 500 hours. After 5 0 (101 200535224 hours, the temperature of all contact zones is controlled as follows: the temperature of the contact zone is raised to 354 ° C (670 T), maintained at 354 ° C for 200 hours; raised to 3 66 ° C (690 ° F), held at 366 ° C for 200 hours; rose to 371 ° (700 ° F), kept at 371 ° C for 1000 hours; rose to 385 ° c (725 F) 'kept at 385 200 hours at C: then rose to a final temperature of 3 99 ° C (750 ° F) and maintained at 399 r for 200 hours to reach a total contact time of 23,000 hours. Crude oil products are regularly analyzed to determine TAN, crude oil Feed hydrogen uptake, P value, VGO content, residue content, and oxygen content. Average of properties of crude oil products produced in Examples 8 to 11 The value series are shown in Table 5 of Wii, 0, g, g,> P, P, P ("P") vs. running time ("t"). Crude oil is fed with at least p value. Curve 14 〇, 142, 144, and 146 indicate that by using the shoulder: Ke individual and the four catalyst systems of Examples 8 to n

原*油產物之P值。對於實施例…。的觸 J 達到·小時的原油產物之p值剩下至少 ;P value of crude oil product. For the examples ... The p value of the crude oil product that reaches J hours is at least left;

例11中，多數運轉時間的P值大於1&gt;5。在實 轉（2300小時）結束時 ^ U 之P值來看，η 值為Μ。從母個試驗的原油產 可推斷在每個試驗中原 持相當穩定(例如原油進料、…中原油進枓於接觸期間 了實施…的：值::之有:^^^ 分的每個試驗中均保持J當固定。，原油產物…在大 圖13為氫氣存在下四種觸媒系統的原油進料之氫的: 102 200535224 吸轉時間（“t，，）的圖示。曲線i48、i5〇、i52、 15)係表示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。原油進料之氫的淨吸取 在2300小時的運轉期間係於7至48 至_ Β)的範圍内。如圖13所示，原油進料之氫的淨吸取在 每個試驗中相當固定。 圖μ為實施例8至η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⑺的圖 示。於四個試驗的每一個之中，原油產物具有殘留物含量 為88至9G%之原油進料的殘留物含量。曲線156、158、16〇、 1 62係表不藉由使原油進料個別與實施例8至U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Υ 原^產物的殘留物含量在大部分的每個試驗中均保持相當 團15為實施例8至In Example 11, the P value of most of the operating hours was greater than 1> 5. At the end of the real revolution (2300 hours), the value of ^ U is η and the value of η is M. It can be inferred from the crude oil production in each of the tests that the original was fairly stable in each test (for example, crude oil feed, ... crude oil feed was carried out during the contact period): value :: of: ^^^ points for each test In both cases, J is fixed. Crude oil products ... In Figure 13 is the hydrogen of the crude oil feeds of the four catalyst systems in the presence of hydrogen: 102 200535224 Graphic representation of the suction turn time ("t ,,". Curve i48, i50, i52, 15) represent the net uptake of hydrogen obtained by contacting the crude oil feed individually with each of the catalyst systems of Examples 8 to η. The net uptake of hydrogen by crude oil feed is at 2,300 hours of operation The period is in the range of 7 to 48 to _B). As shown in Figure 13, the net uptake of hydrogen from the crude oil feed is fairly constant in each test. Figure μ shows each catalyst system from Examples 8 to η A graphical representation of the residual content ("R") of crude oil products as a function of operating time, expressed in weight percent. In each of the four tests, the crude oil product had a crude oil content of 88-9G% Residue content of the feedstock. Curves 156, 158, 160, and 62 show that by using crude oil The residue content of the crude oil product obtained by contacting with the catalyst systems of Examples 8 to U. As shown in Figure M, the residue content of the original product remained equivalent to 15 in most of each test as an example. 8 to

…一 q&gt;由屋衫 PI比重改變（“Δ ΑΡΙ，，）對運轉時間（“t，，）的圖示。曲線b 1 66、1 68、170係表示藉由使原油進料個別與實施例8 11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 之範圍内的黏度。每個原油產物的Αρι比重係增加工$ 4.1度。增加的API比重係對應於21 7至22·95範圍内 原油產物之API比重。此範圍内的ΑΡΙ比重為11〇至u 之原油進料的API比重。 圖1 6為實施例8至11的每個觸媒系統之以重量百 103 200535224 率表示的原油產物之含氧量(‘‘〇，)對運轉時間(“r)的圖 不。曲線172、174、176、178係、表示藉由使原油進料個 別與實施例8纟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。 母個原油產物在每個試驗期間具有含氧 中0.0014至0.0015克的範圍内。如圖 量為每克原油產物 1 6所示，原油產物... a q &gt; Graphical representation of the change in the specific gravity of the shirt PI ("Δ ΑΡΙ ,," versus the operating time ("t ,,)". Curves b 1 66, 1 68, and 170 represent the specific gravity of the Alp of the crude oil product obtained by contacting the crude oil feed individually with the catalyst system of Example 8-11. In each of the four tests, each crude oil product had a viscosity in the range of 58.3 to. The specific gravity of Aρm for each crude oil product is increased by $ 4.1 degrees. The increased API specific gravity corresponds to the API specific gravity of crude oil products in the range of 21 7 to 22 · 95. Within this range, the API specific gravity of the crude oil feed is from 110 to u. Fig. 16 is a graph of the oxygen content ("0,") of the crude oil product expressed in terms of weight percent 103 200535224 for each catalyst system of Examples 8 to 11 versus operating time ("r). Curves 172, 174, 176, and 178 represent the oxygen content of the crude oil product obtained by contacting the crude oil feed individually with the catalyst system of Examples 8 to 11. Each crude oil product has the most oxygen content of the crude oil feed. The parent crude oil product has a range of 0.0014 to 0.0015 grams of oxygen in each test period. As shown in the figure, the crude oil product is 16 per gram of crude oil product.

的含氧量在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 期間減少。0為在這些實施射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它（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 Nm3/m3 (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 °C (750 T)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25.4 wt%。 於實施例9中，反應條件為：371 °C (700 V )，壓 力為6.9 MPa (1014.7 psi)，及氫和原油進料的比率為ι6〇 Nm3/m3 (1〇〇〇 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 °C (750 T)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%。 原油進料MCR含量中此等降低的增加係顯示未煅燒 104 200535224 過的第6和10攔金屬觸媒於較高溫度下比未煅燒過的第6 和9攔金屬觸媒更能促使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氳的淨吸 取。Μ的原油產物性f最多為7()%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。The oxygen content remains fairly constant after a contact time of 200 hours. The relatively constant oxygen content of the crude oil product shows a reduction in the selected organic oxygen compounds during the contact. 0 means that the TAN is also reduced in these implementations, so it can be inferred that at least a portion of the carboxylic acid-containing organic oxygen compounds have a more selective decrease than non-carboxylic acid-containing organic oxides. In Example 11, the reaction conditions were 371 (700 mbar), pressure was 6.9 MPa (1014.7 psi), and the ratio of hydrogen to crude oil feed was 160 Nm3 / m3 (1000 SCFB). Based on the weight of the feed, the reduction in mcr content in the crude feed was 17.5 wt. /. . At a temperature of 399 ° C (750 T), at the same pressure and the ratio of hydrogen and crude oil feed, the reduction in MCR content of crude oil feed was 25.4 wt% based on the weight of the crude oil feed. In Example 9, the reaction conditions were: 371 ° C (700 V), the pressure was 6.9 MPa (1014.7 psi), and the ratio of hydrogen to crude oil feed was ιο 60 Nm3 / m3 (1000 SCFB). The reduction in MCr content of the crude oil feed was 17.5% by weight based on the crude oil feed weight. At a temperature of 399 ° C (750 T), at the same pressure and the ratio of hydrogen and crude oil feed, the reduction in MCR content of crude oil feed was 19 wt% based on the weight of the crude oil feed. The increase in these reductions in the MCR content of the crude oil feed shows that the 6th and 10th metal catalysts that have not been calcined 104 200535224 are more capable of promoting MCR content at higher temperatures than the 6 and 9th metal catalysts that have not been calcined The reduction. These examples show that crude oil feeds with relatively high TAN (0.8 TAN) or catalyst contact systems produce crude products while maintaining the stability of the crude feed / total product mixture and have a net uptake of relatively small amounts of 氲. The crude oil product f of M is at most 7 ()% of the same nature of the crude oil feed: at the same time, the selected properties of the crude oil product are within the same range of the 20-30% crude oil feed.

八體而。如表4所示，每個原油產物係以最多為44 Nm /m (275 SCFB)的原油進料之氫的淨吸取生產。這類產 $具有平均TAN最多為原油進料的4%，平均總Nl/V含量 曰夕為6 1 /〇之原油進料的總Ni/V含量，而同時保持高於3 的原油進料之P值。每個原油產物的平均殘留物含量為$ 8 至90%之原油進料的殘留物含量。每個原油產物的平均 VGO含量為115至117%之原油進料的vG〇含量。每個原 ’由產物的平均API比重為&quot;〇至117%之原油進料的API 比重’而每個原油產物的黏度最多為45%之原油進料的黏 度。 ~~愿A進料在最小i‘消耗詈的_、巧下 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 數目和内谷以外)、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切混合。每個反應器的原油進料流 105 200535224 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， 反化石夕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 油進料於氳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13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。 實知例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16〇 Nm3/m3 (1〇〇〇 SCFB)，LHSv為1 h 1，及壓力為6·9 Mpa (1〇14·7 psi)。接觸區係於一段時間 過程中逐漸加熱至343 °C (650 T)並且保持在343 °C下 120小日才’以達到360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 U中’氫的淨吸取為_1〇·7 Nm3/m3 (_65 scFB)，原油產物 /、有6.75的tan。於實施例Η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 在〇·3至〇·5之範圍内的TAN。於實施例14中，在原油進 料與1目/飢觸媒的接觸期間，氫的淨吸取在-0.05 Nm3/m3至 106 200535224 0.6 Nm /m3 (_〇 36 SCFB 至 4 〇 SCFB)的範 眾油產物 具有在0.2至〇·5之範圍内的TAN。 k接觸期間氫的淨吸取值來看，估計在原油進料與飢 觸媒接觸期間，氫係以10.7Nm3/m3 (65 ScFB)的速率發/生 接觸期間的氫氣發生與習知製程中所用的氫量相比，可六 許在製程中使用較少的氫來改善劣質原油的性質。接觸2 間需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/釩觸媒的接觸係生產具有低於由 單獨錮觸媒所生產之原油產物的TAN之TAN的原油產物。 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 分析係與實施例5所述者相同。除另有說明外，所有觸媒 係以2份碳化矽對丨份觸媒的體積比與碳化矽混合。每個 反應為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 個反應為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 200535224 於實施例1 5中 置在底部接觸區中 法製備的鉬觸媒。 頂部接觸區中。 ’附加觸媒/碳化石夕混合物（45 cm3)係配 ’該附加觸媒為藉由實施例3所述之方 飢觸媒/ ¼化石夕混合物（1 5 cm3)係配置在 ； 】6中附加觸媒/碳化石夕混合物（30 cm3)係酉己 置在底部接觸區中，該附加觸媒為藉由實施例3所述之方 法製備的銦觸媒。飢觸媒/碳化石夕混合物（M 係配置在 頂部接觸區中。 於實施例17 +，附加觸媒/碳化石夕混合物（30 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/ 飢觸媒。㈣媒/碳化石夕混合物（3〇 cm3)係配置在頂部接觸 區中。 於貫施例 18 中 ’ Pyrex® (Glass w〇rks c〇rp⑽ti⑽，New York，U.S.A·)小珠（30 cm3)係配置在每個接觸區中。 用於實施例15至18之具有摘要於表5,圖17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 ^，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 °F)並且保持在343 °C下以達到14〇〇 小時的總運轉時間。 108 200535224 這些實施例顯示於氫源存名 一、 轧，厚仔在下，原油進料與具有中位 孔徑為3 5 0 A之孔徑分你的楚《如 刀师的弟5欄金屬觸媒與結合具有中 位孔徑在250至300 A範圚肉夕了丨斤、 固内之孔徑分佈的附加觸媒接觸 以生產原油錢’其與原油進料之同樣性質相比具有改變 的性質’而該原油產物的其他性質與原油進料之同樣性質 相比只有少量改變。士士 在加工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17所示，實施例15至17的原 油產物具有TAN最多為15%之原油進料的tan。實施例Η · 至1 7中所生產的原油產物與原油進料的同樣性質相比， 分別具有最多為44%的總Ni/V/Fe含量，最多為5〇%的含 氧量，及最多&amp; 75%的黏度。此外，實施例15至Η中所 生產的原油產物分別具有Αρι比重為1 〇〇至i 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矛口 API比重相比，係生成具有增加 々占度和降低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。 _UjJt料在各種LHSV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 、.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(1014.7psi)，及接觸區的溫度為371 °C (700 F )達總運轉時間。於實施例1 9中，接觸期間的LHSV於 109 200535224 t1增加到12 Ir1 ’保持在12 h_1下48 保持在20.7 Ir1下96 一段時間過程中由 小時，接著使LHSV增加到20.7 h·1， 小時。 於貫施例19中，分析原油產物以測定在LHSVa 12h-i 和20.…時限期間的TAN、黏度、密度、⑽含量、 物含1、雜原子含量’及有機酸金屬鹽形態的金屬含 罝。原油產物性質的平均值示於表6,圖18。 如表6’圖18所示，實施例19的原油產物與原油進 枓的TAN和黏度相比具有降低的⑽和降低的黏度，而 原油產物的ΑΡΙ比重為⑽至&quot;G%之原油進料的趟比 重。MCR含量與c5瀝青質含量的重量比至少為15。職 含量與〇5瀝青質含量的和比原油進料之職含量與^遞 青質含量的和減少。從MCR含量與c5瀝青質含量的重量 比及職含量與C5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、納、鋅㈣的總含量最多&amp; 6G%的原油進料之相同 金屬的總含量。原油產物的含硫量為8〇至9〇%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 為1 h·1的製程相比，使通過接觸區的lHSV大於^， 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 弁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 200535224 備）進行。 料在各種拯觸溫彦下的接觸i 接觸系統和觸媒係與實施例6所述者相同。將具有列 於图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。Eight bodies. As shown in Table 4, each crude product was produced with a net uptake of hydrogen from a crude feed of up to 44 Nm / m (275 SCFB). This type of production 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 Nl / V content of 6 1/0, while maintaining a crude oil feed above 3 Of the P value. The average residue content of each crude oil product is $ 8 to 90% of the residue content of the crude feed. The average VGO content of each crude product is from 115 to 117% of the vGO content of the crude feed. The average API specific gravity of each raw product is &quot; API specific gravity of crude oil feed &quot; from 0 to 117%, and the viscosity of each crude oil product is at most 45% of the viscosity of the crude oil feed. ~~ May A feed the catalyst with the smallest i 'consumption, and the catalyst with the lower pore size distribution in Examples 12 to 14, each reactor equipment (except the number of contact zones and inner valleys), each The catalyst formation sulfide 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 carbon. Crude feed stream for each reactor 105 200535224 The kinetics runs from the top of the reactor to the bottom of the reactor. The silicon carbide system is arranged at the bottom of each reactor as a bottom carrier. Each reactor contains a contact zone. After the catalyst / silicon carbide mixture was placed in the contact area of each reactor, the reverse fossils were arranged above the top contact area to fill the vacancies and serve as a preheating area for each reactor. Each reactor was charged into a Lindberg furnace, which included three heating zones corresponding to a preheating zone, a contact zone, and a bottom carrier. Feed the crude oil in contact with each catalyst in the presence of radon. The catalyst / silicon carbide mixture (40 cm3) was placed over the silicon carbide to form the contact area. The catalyst used in Example 12 was the vanadium catalyst prepared in Example 2. The catalyst used in Example 13 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 Known Examples 12 to 14 are as follows: the ratio of hydrogen to the crude oil feed to the reactor is 160 Nm3 / m3 (100 SCFB), the LHSv is 1 h 1, and the pressure is 6.9 Mpa (1014 · 7 psi). The contact zone is gradually heated to 343 ° C (650 T) over a period of time and maintained at 343 ° C for 120 hours' to achieve a total operating time of 360 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 U, the net absorption of hydrogen is -10.7 Nm3 / m3 (_65 scFB), and the crude product has a tan of 6.75. In Example VII, the net uptake of hydrogen is in the range of 2.2 to 3.0 Nm3 / m3 (13.9 to 18.7 sCFB), and the crude product has a TAN in the range of 0.3 to 0.5. In Example 14, during the contact between the crude oil feed and the 1 mesh / hungry catalyst, the net absorption of hydrogen was in the range of -0.05 Nm3 / m3 to 106 200535224 0.6 Nm / m3 (_〇36 SCFB to 4 〇SCFB). Many oil products have a TAN in the range of 0.2 to 0.5. From the perspective of the net hydrogen absorption during the contact, it is estimated that during the contact between the crude oil feed and the catalyst, the hydrogen system generated / generated hydrogen at the rate of 10.7 Nm3 / m3 (65 ScFB) during the contact and used in the conventional process. Compared with the amount of hydrogen, you can use less hydrogen in the process to improve the properties of inferior crude oil. Contacting 2 with less hydrogen will tend to reduce the cost of processing crude oil. In addition, the contact of the crude oil feed with the molybdenum / vanadium catalyst is to produce a crude oil product having a TAN that is lower than the TAN of the crude oil product produced by the plutonium catalyst alone. The analysis of each reactor equipment (except for the number and content of contact zones), each catalyst formation sulfide method, each total product separation method, and each crude product analysis system is the same as described in Example 5. Unless otherwise stated, all catalysts were mixed with silicon carbide in a volume ratio of 2 parts silicon carbide to 1 part catalyst. The crude oil feed flow for each reaction is from the top of the reactor to the bottom of the reactor. The silicon carbide system is arranged at the bottom of each reactor as a bottom carrier. Each reaction has a bottom contact area and a top contact area. After the catalyst / silicon carbide mixture was placed in the contact area of each reactor, the silicon carbide system was arranged above the top contact area to fill the voids and serve as a preheating area for each reactor. Each reactor was charged into a Lindberg furnace, which included four heating zones corresponding to a preheating zone, two contact zones, and a bottom carrier. In each example, a vanadium catalyst was prepared as described in Example 2 and used with an additional catalyst. 107 200535224 In Example 15, a molybdenum catalyst prepared by placing in a bottom contact zone. In the top contact area. 'Additional catalyst / carbon fossil evening mixture (45 cm3) is formulated' The additional catalyst is the square catalyst / ¼fossil evening mixture (1 5 cm3) described in Example 3; [6] The additional catalyst / carbide carbide mixture (30 cm3) was placed in the bottom contact area. The additional catalyst was an indium catalyst prepared by the method described in Example 3. Hungry catalyst / Carbonite evening mixture (M is arranged in the top contact area. In Example 17+, the additional catalyst / carbonite fossil evening mixture (30 cm3) is arranged in the bottom contact area, the additional catalyst It is the molybdenum / hungry catalyst prepared as in Example 4. The catalyst / carbonite mixture (30 cm3) is arranged in the top contact zone. In Example 18, 'Pyrex® (Glass Works c. rp⑽ti⑽, New York, USA.) Beads (30 cm3) are arranged in each contact zone. The crude oil (Santos Basin, Brazil) system used in Examples 15 to 18 having the properties summarized in Table 5, and FIG. 17 It is fed into 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. The crude oil feed is in contact with each catalyst in the presence of hydrogen. The contact conditions were as follows: the ratio of hydrogen to the crude oil feed to the reactor was 160 Nm3 / m3 (100 SCFB) for the first 86 hours and 80 Nm3 / m3 (500 SCFB) for the remaining time limit, and the LHSV was i ^, and the pressure is 6.9 MPa (1014 · 7 psi). The contact zone gradually changes over a period of time. Heated to 343 ° C (650 ° F) and kept at 343 ° C to achieve a total operating time of 14,000 hours. 108 200535224 These examples are shown in the hydrogen source name I. Rolling, Houzi below, crude oil feed With a median aperture of 3 5 0 A, you will be divided into "The 5th column metal catalyst of the knife master's brother with a median aperture of 250 to 300 A. The range of meat is fine. The distributed additional catalyst is contacted to produce crude oil, which has changed properties compared to the same properties of the crude oil feed, and the other properties of the crude oil product are only slightly changed compared to the same properties of the crude oil feed. During this period, a relatively small amount of hydrogen uptake by the crude oil feed was observed. Specifically, as shown in Table 5 ′ and FIG. 17, the crude oil products of Examples 15 to 17 had a tan of tan with a maximum of 15% of the crude oil feed. Example Η · Compared with the same properties of the crude oil feed, the crude oil products produced in to 17 have a total Ni / V / Fe content of up to 44%, an oxygen content of up to 50%, and a maximum of &amp; 75% viscosity. In addition, the crude oil produced in Examples 15 to Η The raw materials have API gravity of crude oil feed with Aρι specific gravity of 1000 to i. In contrast, the crude oil product produced under non-catalytic conditions (Example 18) and the viscosity of the crude oil feed have a specific API gravity phase. The ratio produces a product with an increase in tritium content and a decrease in the specific gravity of the API. From the viewpoint of increasing the viscosity and reducing the% specific gravity of API, it can be inferred that coking and / or polymerization of the crude oil feed has been initiated. _UjJt material contact under various LHSV. The contact system and the catalyst system are the same as those described in the sixth embodiment. Crude feeds are listed in Table 6 in Figure 18. The contact conditions are as follows: The ratio of hydrogen to the crude oil feed to the reactor is 160 Nm3 / m3 (1000 SCFB), the pressure is 6.9 MPa (1014.7 psi), and the temperature in the contact zone is 371 ° C (700 F). Total running time. In Example 19, the LHSV during the contact period was increased at 109 200535224 t1 to 12 Ir1 'Keeped at 12 h_1 48 Kept at 20.7 Ir1 96 During a period of time, the LHSV was increased to 20.7 h · 1, hour . In Example 19, the crude oil product was analyzed to determine the TAN, viscosity, density, hafnium content, content 1, heteroatom content ', and metal content of organic acid metal salt form during the time period of LHSVa 12h-i and 20 .... Alas. The average values of the properties of the crude oil products are shown in Table 6 and Figure 18. As shown in Table 6 ′ and FIG. 18, the crude oil product of Example 19 has a lower viscosity and a lower viscosity than the TAN and viscosity of crude oil, and the crude product has an API with a specific gravity ranging from ⑽ to &quot; G%. Proportion of material expected. The weight ratio of MCR content to c5 asphaltene content is at least 15. The sum of the post content and the 05 asphaltene content is lower than the sum of the post content and crude green content of the crude oil feed. From the reduction of the weight ratio of the MCR content to the c5 asphaltene content and the sum of the work content and the C5 asphaltene, it can be inferred that the asphaltenes, rather than the components with a tendency to form coke, will decrease. Crude oil products also have a total content of potassium, sodium and zinc rhenium of up to &lt; 6G% of the same metal in the crude oil feed. The crude product has 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 ^ compared to a process with 1 h · 1 to produce crude products with similar properties. The ability to selectively change the properties of crude oil feeds at liquid space velocities greater than 100 h allows the contact method to be performed in a container that is smaller in size than a commercially available container. The smaller container size can accommodate the treatment of inferior crude oil at production sites with size restrictions (eg offshore facilities 110 200535224). The contact system and catalyst system are expected to be the same as those described in Example 6 under various conditions. 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.

頂部接觸區的接觸條件如下·· LHSV為丨h-i ;頂部^ 觸區的溫度為260 °C (500 °F);氫和原油進料的比率j 160 Nm /m3 (looo SCFB” 及壓力為 6 9 Mpa (1〇14 7 ㈣） 底部接觸區的接觸條件如下：LHSV為丨:底部^ 觸區的溫度為315 &lt;t (6〇〇 τ);氫和原油進料的比率^ 160 Nm /m (looo SCFB);及壓力為 6 9 Mpa (i〇i4 7 c 總產物離開底部接觸區並導入氣液相分離器。於氣择 相：離器中，將總產物分離成原油產物和氣體。原油產本 係定期分析以測定TAN和q瀝青質含量。The contact conditions at the top contact zone are as follows: LHSV is hi; the temperature at the top ^ contact zone is 260 ° C (500 ° F); the ratio of hydrogen and crude oil feed j 160 Nm / m3 (looo SCFB "and pressure 6 9 Mpa (1〇14 7 ㈣) The contact conditions at the bottom contact zone are as follows: LHSV is 丨: the bottom ^ temperature of the contact zone is 315 &lt; t (60〇τ); the ratio of hydrogen and crude oil feed ^ 160 Nm / m (looo SCFB); and a pressure of 6 9 Mpa (i〇i4 7 c) the total product leaves the bottom contact zone and is introduced into a gas-liquid phase separator. In a gas phase selective: separator, the total product is separated into crude oil products and gases Crude oil production is regularly analyzed to determine TAN and q asphaltene content.

運轉期間所得到之原油產物性質的平均值列於表7， 圖心原油進料具有9.3的TAN及C5&gt;歷青質含量為每身 原油進料中有0.055克的C5瀝青質。原油產物具有〇.7的 :均TAN &amp; C5瀝青質的平均含量為每克原油產物中有 39克的c5》歷青質。原油產物的C5瀝青質含量最多為7&quot; 之原油進料的c5瀝青質含量。 原油產物中钾和鈉的總含量最多4 53%之原油進料中 料的ί::總含量。原油產物的TAN最多為10%之原油進 4的TAN。在接觸期間係保持15或更高的p值。 111 200535224 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。(：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q瀝青質含量比原油進料之 瀝青質含量更為降低。 5 此外，使用控制溫差會使有機酸金屬鹽形態的金屬含 置降低的更多。舉例而纟，在每個實施例具有相當固定的 原油進料/總產物混合物之穩定性（如p值所測定者）的情況 下實把例20之原油產物的鉀和納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。 使用較低溫度的第—接觸區可容許移除高分子量化合 物(例如C5瀝青質及/或有機酸金屬鹽），其會有形成聚合物 及/或具有柔軟性及/或黏性的物理性f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類 化合物在它們堵塞和被覆觸媒之前被移除，藉此增加配置 在第-接觸區後面於較高溫度下操作的觸媒壽命。The average value of the properties of the crude oil products obtained during the operation is shown in Table 7. The Tuxin crude oil feed has a TAN and C5 of 9.3 and a Cyanite content of 0.055 grams of C5 asphaltene per crude oil feed. The crude oil product has an average content of 0.7: TAN & C5 asphaltenes of 39 grams of c5 cyanocyanine per gram of crude oil product. The C5 asphaltene content of the crude oil product is at most 7 &quot; the c5 asphaltene content of the crude oil feed. The total content of potassium and sodium in crude oil products is up to 4 53% of the total ί :: in the crude oil feed. The TAN of the crude product is at most 10% of the TAN of the crude oil. A p-value of 15 or higher was maintained during the contact. 111 200535224 As shown in Examples 6 and 20, it has a contact temperature 50 below the second (bottom in this example) zone. (: The first (top in this example) contact temperature will tend to reduce the q asphaltene content of the crude oil product more than the asphaltene content of the crude oil feed. 5 In addition, the use of controlled temperature differences will cause organic acid metal salts The metal content of the morphology is reduced even more. For example, in the case where each example has a fairly constant stability of the crude oil feed / total product mixture (as determined by the p value), the crude oil of Example 20 is actually used. The reduction in the total potassium and sodium content of the product is much greater than the reduction in the total potassium and sodium content of the crude product of Example 6. The use of a lower temperature first contact zone may allow the removal of high molecular weight compounds such as C5 asphaltenes and / or Organic acid metal salt), which tends to form polymers and / or compounds with soft and / or sticky physical properties (such as gums and / or tars). Removing these compounds at lower temperatures can Such compounds are allowed to be removed before they clog and cover the catalyst, thereby increasing the life of the catalyst disposed at the higher temperature behind the first contact zone.

貫紹列2L_浮體形式之觸谭的桩覦。Guan Shao's 2L_ floating body form touches Tan's post.

本申請案之塊狀金屬觸媒及/或觸媒100克的原J 進料中含0.0001 $ s古+ 至5克或〇·02至4克的觸媒）於若干具磨 實例中可用原油進料使其懸浮並且打列條件下反應：溫 又在至425 c 〇85至797 °F)的範圍内，壓力在〇·：; 至1 0 MPa的範屋I内，菸与、広i β 阖内及虱源和原油進料的比率為16至1600The bulk metal catalyst of this application and / or catalyst 100 grams of the original J feed contains 0.0001 $ s ancient + to 5 grams or 0.02 to 4 grams of catalyst) crude oil available in several grinding examples The feed is suspended and reacted under the conditions of the train: the temperature is in the range of 425 c (0.885 to 797 ° F), and the pressure is in the range of 0 :: to 10 MPa in the Fan House I. β pupae and lice and crude feed ratios from 16 to 1600

Nm3/m3達一段日车M ju 0 y 、0 。在足以生產原油產物的反應時間之 後’原油產物係接用八触^ 更用刀離§又備，如過濾器及/或離心機，和 觸媒及/或殘留的原、;隹斗 ’、/進枓刀離。原油產物與原油進料相比 112 200535224 可具有改變的TAN，鐵、鎳，及/或釩的含量，及降低的c 瀝青質含量。 ’ 熟習該項技術者鑑於本說明書應顯而易見本發明之各 種態樣的進一步修飾和替代具體實例。因此，本說明書僅 視為說明及用以達到教示熟習該項技術者實施本發明的一 般方法之目的。應瞭解本文中所表示和敘述的本發明之形 悲係作為具體實例的範例。可取代本文中所圖示和敘述的 元件和材料，可顛倒本發明的部分和程序，可單獨使用本 發明的某些特徵，以上全部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。 【圖式簡單說明】 圖式簡單說曰月 對於一習該項技術者而言，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2A和2B為包含兩個接觸區的接觸系統之具體實例 的簡圖。 圖3 A和3 B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 200535224 簡圖。 圖7為使原油進料與二種觸媒接觸的具體實例之原油 進料與原油產物的代表性質列表。 圖8為使原油進料與一或多種觸媒接觸的具體實例之 加權平均床溫度對運轉時間的圖示。 / 9為使原油進料與兩種觸媒接觸的具體實例之原油 進料與原油產物的代表性質列表。 圖10為使原油進料與兩種觸媒接觸之具體實例的原油 進料與原油產物之代表性質的另一個列表。 圖11為使原油進料盘m猫 竹一四種不同觸媒系統接觸的具體實 到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1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 的原油進料之氫的淨吸取對運轉時間的圖示。 例圖14為使原油進料與四種不同觸媒系統接觸的具體實 乂重里百勿率表不的原油產物之殘留物含量對運轉時 间的圖示。 圖15為使原油進料與四種不同觸女某系統接觸之具體實 的原油產物之API比重改變對運轉時間的圖示。 例之圖16為使原油進料與四種不同觸媒系統接觸的具體實 圖：Μ重量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 200535224 進料與原油產物的代.所 的鉬觸媒和釩觸媒，：貝人列I ’忒觸媒系統包含各種量 統，以及破璃珠。…。έ釩觸媒和銷/釩觸媒的觸媒系 圖1 8為在各種液艚办 觸媒接觸的且體實例之//_下使原油進料與—或多種 圖19H 進料與原油產物的性質列表。 實例之原、'由、“種接觸溫度下使原油進料進行接觸的具體 原油進料與原油產物的性質列表。 =本發明容許各種修飾與替代形式，但其特定具體 二例係错由圖示中的實例表示。該等圖示可能未按比例繪 ^應瞭解其圖示和詳細說明並非用來將本發明限制在所 揭不的特定形式’但相反地’則意圖涵蓋落入如後附申請 專利範圍所限定之精神與範疇内的所有修飾、等效物和 代物。 【主要元件符號說明】 100 :接觸系統 1()2 :接觸區 104 ： ^ ψ 106 ;導管 106’ ··導管 108 :分離區 110 :導管 112 :導管 114 :接觸區 11 6 :接觸區 115 200535224 1 18 :導管 1 2 0 ·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:氳的淨吸取對運轉時間之曲線 1 56-1 62 :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Nm3 / m3 reaches a segment of the sunken car M ju 0 y, 0. After a reaction time that is sufficient to produce crude oil products, 'crude oil products are connected with eight touches ^ more with a knife § and prepared, such as filters and / or centrifuges, and catalysts and / or residual raw materials; / Into the knife away. Crude oil products compared to crude oil feed 112 200535224 may have altered TAN, iron, nickel, and / or vanadium content, and reduced c asphaltene content. It will be apparent to those skilled in the art that further modifications and substitutions of various aspects of the invention will be made in light of the present specification. Therefore, this description is only to be used as an illustration and for the purpose of teaching a person skilled in the art to implement the general method of the present invention. It should be understood that the aspect of the invention shown and described herein is an example of a specific example. Can replace the elements and materials illustrated and described in this article, can reverse parts and procedures of the present invention, can use some features of the invention alone, all of which should be familiar with the technology after the benefits of the description of the invention This is obvious. 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. [Brief description of the drawings] For the person skilled in the art, the advantages of the following detailed descriptions of the present invention will become apparent after referring to the drawings. Among them: Figure 1 is the contact system A simplified diagram of a specific example. Figures 2A and 2B are simplified 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. Fig. 6 is a schematic diagram of a specific example of a combined separation zone, contact system, and blending zone. Fig. 7 is a list of representative properties of a crude oil feed and a crude oil product for a specific example of contacting a crude oil feed with two catalysts. Figure 8 is a graphical representation of weighted average bed temperature versus operating time for a specific example of contacting a crude oil feed with one or more catalysts. / 9 is a list of representative properties of crude oil feeds and crude oil products for specific examples of contacting crude oil feeds with two catalysts. Fig. 10 is another list of representative properties of a crude oil feed and a crude oil product for a specific example of contacting a crude oil feed with two catalysts. Figure 11 is a list of actual crude oil feeds and crude oil products brought into contact with the crude oil feed tray m cat bamboo four or four different catalyst systems. Figure 12 is a graphical representation of the p-value of crude oil products versus operating time for specific examples of contacting a crude feed with four different catalyst systems. Figure 13 is a graphical representation of the net uptake of hydrogen for a specific crude oil feed versus operating time by contacting the crude oil feed with four different catalyst systems. Example Figure 14 is a graphical representation of the residual content of crude oil products as a function of operating time for contacting crude oil feeds with four different catalyst systems. Figure 15 is a graphical representation of the change in API specific gravity of a crude oil product in contact with four different systems for a particular system, as a function of operating time. For example, Figure 16 is a detailed actual diagram of contacting the crude oil feed with four different catalyst systems: the oxygen content of the crude oil product expressed as M weight percentage versus the operating time. Figure 17 is the contact of the crude oil feed with the catalyst system. Specific examples of crude oil 114 200535224 feed and crude oil products. Molybdenum catalysts and vanadium catalysts: Beirenlie I '媒 catalyst system contains a variety of systems and broken glass beads. …. The catalysts of the vanadium catalyst and the pin / vanadium catalyst are shown in Figure 18. The various examples of liquid catalysts are used to contact crude oil feeds and / or various examples. Figure 19H Feeds and crude oil products List of properties. The examples of the original, 'you,' contact list of the properties of the specific crude oil feed and crude oil products at which the crude oil feed is brought into contact. = The present invention allows various modifications and alternative forms, but the specific two specific examples thereof are incorrect. The illustrations shown in the illustrations may not be drawn to scale ^ It should be understood that the illustrations and detailed descriptions are not intended to limit the present invention to the specific form disclosed, but to the contrary, are intended to cover the following. All modifications, equivalents, and substitutes within the spirit and scope defined by the scope of the applied patent are attached. [Description of the main component symbols] 100: Contact system 1 () 2: Contact area 104: ^ ψ 106; Catheter 106 '... 108: separation zone 110: catheter 112: catheter 114: contact zone 11 6: contact zone 115 200535224 1 18: catheter 1 2 0Separation zone 122: catheter 124: catheter 126: catheter 128: catheter 130: blending zone 132: Duct 134: Duct 136: Curve of weighted average bed temperature (WABT) vs. operating time 140-146: P value of crude oil product vs. operating time 148_ 154: Net absorption of radon versus operating time 1 56-1 62: Residues of crude oil products Material content versus operating time curve 164-170: API gravity of crude oil product versus operating time curve 172-178: Oxygen content of crude oil product versus operating time curve

Claims (1)

200535224 十、申請專利範圍： 1.一種生產觸媒之方法，其包括·· 吏載體_或夕種金屬結合以形成載體/金屬渑八 其中該載體包含㊀氧化銘，該-或多種金屬包括週期：！， 攔的-或多種金屬’週期表第6攔之—或多種金屬的^ e 多種化合物，或其混合物； 或 ;至少400 t的溫度下熱處理0氧化鋁載體/金屬混合 物；及產生觸媒’纟中該觸媒具有中位孔徑至 Μ。A200535224 10. Scope of patent application: 1. A method for producing a catalyst, which includes a carrier or a combination of metals to form a carrier / metal. The carrier contains an oxide oxide, and the-or multiple metals include a cycle :! ,-Or more metals '6th of the Periodic Table-or more compounds of metals, or mixtures thereof; or; heat treatment of at least 400 t alumina support / metal mixture; and the production of catalysts' This catalyst has a median pore diameter to M. A 的孔徑分佈’其藉由astm法D4282測定。 2·如申請專利範圍第1項之方法，其中該孔徑分佈的 中位孔徑最多為5〇〇 A。 3·如申請專利範圍帛i或2項之方法，其中該孔徑分 布中孔的孔體積至少為〇·3 em3/g或至少為咖3化。 ^ 4·如申請專利範圍第1至3項中任一項之方法，其中 該觸媒的表面積至少為6〇 mVg或至少為9〇 。 5.如申請專利範圍第丨至4項中任一項之方法，其中 該一或多種金屬另外包含週期表第5攔的一或多種金屬， 或夕種第5攔金屬的一或多種化合物，週期表第7至1〇 攔的一或多種金屬，一或多種第7至丨〇欄金屬的一或多 種化合物’或其混合物，加上載體。 6_如申請專利範圍第1至5項中任一項之方法，其中 遠一或多種金屬另外包含釩、鈷、鎳，或其混合物。 7·如申請專利範圍第丨至6項中任一項之方法，其中 違一或多種金屬另外包含週期表第1 5攔的一或多種元素 117 200535224 及/或一或多種第15欄元素的—或多種化合物加上載體。 8.如申請專利範圍帛！至7項中任—項之方法，其中 該載體的㊀氧化紹含量為每克載體中含至少（M克，’至少、〇 3 克，或至少0.5克的Θ氧化鋁。 · 9·如申請專利範圍第…項中任一項之方法，並中 ^體另外包含δ氧化紹及/心氧化紹’其藉由乂射 測定。 9項中任一項之方法，其中 〇 · 1克α氣化無的α氧化|呂 10·如申請專利範圍第1至The pore size distribution is determined by the astm method D4282. 2. The method according to item 1 of the patent application range, wherein the median pore size of the pore size distribution is at most 500 A. 3. The method according to the scope of application for patents (i) or (2), wherein the pore volume of the pores in the pore size distribution is at least 0.3 em3 / g or at least 3 μm. ^ 4. The method according to any one of claims 1 to 3, wherein the surface area of the catalyst is at least 60 mVg or at least 90. 5. The method according to any one of claims 1-4, wherein the one or more metals further comprise one or more metals of the fifth block of the periodic table, or one or more compounds of the fifth block of the metal, One or more metals in columns 7 to 10 of the periodic table, one or more compounds of one or more metals in columns 7 to 10 ', or mixtures thereof, plus a support. 6_ The method according to any one of claims 1 to 5, wherein the one or more metals further comprise vanadium, cobalt, nickel, or a mixture thereof. 7. The method according to any one of claims 1-6, wherein one or more of the metals in violation of one or more of the elements in column 15 of the periodic table 117 200535224 and / or one or more of the elements in column 15 -Or more compounds plus a carrier. 8. If you apply for a patent scope! The method of any one to seven items, wherein the tritium oxide content of the carrier is at least (M g, 'at least, 0 3 g, or at least 0.5 g of θ alumina per gram of the carrier. The method of any one of the scope of the patent, and the intermediate additionally includes δ oxide and / cardiac oxide, which are determined by radiography. The method of any one of 9 items, wherein 0.1 g of α gas Alpha-free oxidation | Lu 10 · If the scope of patent application is 1 to 该載體也具有每克載體中最多為 含量。 u.如申請專利範圍第1至10項中任一項之方法， 中該方法尚包括使載體/金屬混合物與水結合以形成糊 物’及擠壓此糊狀物。 ’ 12. —種觸媒，其可藉由申請專利範圍第丨至η 任一項之方法獲得。 、 ^ 一種觸媒，其包含：The carrier also has a maximum content per gram of carrier. u. The method according to any one of claims 1 to 10, wherein the method further comprises combining the carrier / metal mixture with water to form a paste &apos; and extruding the paste. 12. A catalyst, which can be obtained by a method according to any one of the scope of application for patents η to η. , ^ A catalyst comprising: 夕週期表第6欄的-或多種金屬，週期表第6搁之 夕種孟屬的一或多種化合物，或其混合物； 具有Θ氧化鋁含量為每克載體中含至少〇1克㊀ 的載體，其藉由X射線繞射測定；及 其中該觸媒具有中位孔徑至少為23〇 A的孔徑八 其藉由ASTM法D4282測定。 刀， 14_一種觸媒，其包含： 週期表第5欄的-或多種金屬，週期表第5襴之一或 118 200535224 多種金屬的-或多種化合物，或其混合物； 週』表第6欄# $多種金屬，週期表第6欄之一或 多種金屬的-或多種化合物，或其混合物； ^ 具有Θ氧化紹含量為每吞番蛐士人 巧母克栽體中含至少〇·1克Θ氧化鋁 的載體，其藉由X射線繞射測定；及 其中該觸媒具有中位孔徑至少為230 Α的孔徑分佈， 其藉由ASTM法D4282測定。 # 15.如中請專利範㈣14項之觸媒，其中該至少一種 第5攔金屬為飢。 &amp;如申請專利範圍第12至15項中任—項之觸媒盆 中-或多種第6攔的金屬為錮及/或鎢。 ’、 17.—種生產原油產物之方法，其包括： 使原油進料與-或多種觸媒接觸以生產含有原油產物 的總產物，其中該原油產物在25。〇和〇 ι〇ι购下為液 態混合物，該原油進料具有至少〇3的總酸值（tan)，該至 少一種觸媒具有令位孔徑至少為180 A的孔徑分佈，其藉 由ASTM》去D4282 ;則定，該觸媒具有包含㊀氧化紹和週期 表f 6夕攔的-或多種金屬，週期表第6搁之一或多種金屬 的一或多種化合物，或其混合物的孔徑分佈；及 控制接觸條件以便使該原油產物具有TAN最多為9〇% 之原油進料的TAN，其中TAN係藉由ASTM法DM4測定。 I8·如申請專利範圍第17項之方法，其中該原油產物 的TAN最多為5〇%，最多為3〇%，或最多$ 1()%之原 料的TAN。 &lt; 119 200535224 9 · 士申π月專利範圍弟1 7項之方法’其中兮历、山立 Τ β原油產物 勺 TAN 在 1 至 8〇%，2〇 至 7〇0/〇，3〇 至 6〇0 次40至50% 之原油進料的TAN之範圍内。 2〇·如申請專利範圍第17至19項中任一項之方法，其 中該原油產物的TAN在0.001至〇·5，〇·〇ι至〇， a 土 至〇_1的範圍内。 〆· 21·如申請專利範圍第17至20項中任一項之方法，盆 中該原油進料的TAN在0.3至20，0·4至1〇，戍〇 5至 的範圍内。 22·如申請專利範圍第I?至21項中任一項之方法，其 中該中位孔徑至少為230 Α。 、 23 ·如申請專利範圍第17至22項中任一項之方法，其 中使該原油進料在位於或連接到近海設備的接觸區中進r 接觸。 丁 24_如申請專利範圍第17至23項中任一項之方法，其 中接觸包括於氳源存在下進行接觸。 25·如申請專利範圍第17至24項中任一項之方法，其 中°亥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。 26·種原油產物或摻合物，其可藉由申請專利 17至25項中任-項之方法獲得。 、種生產運輸用燃料、加熱用燃料、潤滑油或化學 品之方法，其肖；An T* tfc* 申#專利範圍第26項之原油產物 120 200535224 28. 如申請專利範圍第27項之方法，其中該加工包括 使該原油產物或摻合物蒸顧成為一或多種镏分。 29. 如申請專利範圍第26或27項之方法，其中該加工 包括加氫處理。 十一、圖式： 如次頁-Or more metals in column 6 of the periodic table, one or more compounds of the genus Mons, or mixtures thereof in the sixth table of the periodic table; a carrier having a Θ alumina content of at least 0.01 g of ㊀ per gram of carrier , Which is measured by X-ray diffraction; and wherein the catalyst has a pore diameter with a median pore diameter of at least 23A, and it is measured by ASTM method D4282. Knife, 14_ a catalyst comprising: column 5 or more metals of the periodic table, one of the 5th period of the periodic table or 118 200535224 multiple metals-or multiple compounds, or mixtures thereof; column 6 of the week table # $ Multiple metals, one or more of the metals in column 6 of the periodic table-or multiple compounds, or mixtures thereof; ^ has a content of Θ oxide of at least 0.1 g per swallow of the master ’s gram plant. The carrier of Θ alumina, which is measured by X-ray diffraction; and wherein the catalyst has a pore size distribution with a median pore diameter of at least 230 A, which is measured by ASTM method D4282. # 15. The catalyst of item 14 of the patent is requested, wherein the at least one fifth metal is hunger. &amp; In the case of any of the items 12 to 15 in the scope of the patent application-the metal in the sixth or more kinds of thorium is thorium and / or tungsten. '. 17. A method of producing a crude oil product, comprising: contacting a crude oil feed with-or catalysts to produce a total product containing a crude oil product, wherein the crude oil product is at 25. 〇 and 〇ι〇ι are purchased as a liquid mixture, the crude oil feed has a total acid value (tan) of at least 0 3, the at least one catalyst has a pore size distribution of at least 180 A, by ASTM " Go to D4282; it is determined that the catalyst has a pore size distribution of arsenic oxide and metal or metals of the periodic table f6, one or more compounds of one or more metals of the periodic table 6, or a mixture thereof; and The contact conditions were controlled so that the crude product had a TAN of a crude oil feed with a TAN of up to 90%, where TAN was determined by ASTM method DM4. I8. The method according to item 17 of the patent application scope, wherein the TAN of the crude oil product is at most 50%, at most 30%, or at most $ 1 ()% of the raw TAN. &lt; 119 200535224 9 · Shishen π month patent scope method of 17 items' where Xi Li, Shan Li T β crude oil product spoon TAN is 1 to 80%, 20 to 70/100, 30 to Within the TAN range of 60 to 40 crude oil feeds. 20. The method according to any one of claims 17 to 19, wherein the TAN of the crude oil product is in the range of 0.001 to 0.5, 0.00 to 0, and a to 0. 21 · 21 · According to the method of any of claims 17 to 20 of the scope of patent application, the TAN of the crude oil feed in the basin is in the range of 0.3 to 20, 0.4 to 10, and 戍 5 to. 22. The method according to any one of claims 1 to 21 in the patent application range, wherein the median aperture is at least 230 A. 23. A method as claimed in any one of claims 17 to 22 in which the crude oil feed is brought into contact in a contact zone located or connected to an offshore facility. Ding 24_ The method according to any one of claims 17 to 23, wherein contacting includes contacting in the presence of a source. 25. The method of any one of claims 17 to 24 of the scope of patent application, wherein the method further comprises combining the crude oil product with crude oil of the same or different crude oil feed to form a blend. 26. Crude oil products or blends, which can be obtained by any one of the methods of claims 17 to 25. 2. A method for producing transportation fuel, heating fuel, lubricating oil or chemicals; An T * tfc * Application # 26 crude oil product of patent scope 120 200535224 28. Method of patent scope 27 Wherein the processing includes steaming the crude oil product or blend into one or more fractions. 29. The method of claim 26 or 27, wherein the processing includes hydrotreating. Eleven, schema: as the next page 121121
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Families Citing this family (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BRPI0405565A (en) * 2003-12-19 2005-08-30 Shell Int Research Methods of Producing a Transportable Fuel and Crude Oil Product, Heating Fuel, Lubricants or Chemicals, and Crude Oil Product
US8070937B2 (en) 2003-12-19 2011-12-06 Shell Oil Company Systems, methods, and catalysts for producing a crude product
CA2604012C (en) * 2005-04-11 2013-11-19 Shell Internationale Research Maatschappij B.V. Method and catalyst for producing a crude product having a reduced mcr content
KR20070120594A (en) * 2005-04-11 2007-12-24 쉘 인터내셔날 리써취 마트샤피지 비.브이. Systems, methods, and catalysts for producing a crude product
WO2007112782A1 (en) * 2006-04-04 2007-10-11 Shell Internationale Research Maatschappij B.V. A process for reducing the total acid number (tan) of a liquid hydrocarbonaceous feedstock
US20080083650A1 (en) * 2006-10-06 2008-04-10 Bhan Opinder K Methods for producing a crude product
WO2009073442A2 (en) * 2007-11-28 2009-06-11 Saudi Arabian Oil Company Process to reduce acidity of crude oil
BRPI0704443B1 (en) 2007-11-30 2018-09-11 Petroleo Brasileiro S/A Petrobras system and process for separating spent catalyst suspensions and hydrocarbons formed in a multi-reaction upstream fluid catalytic cracking unit
US7862708B2 (en) 2007-12-13 2011-01-04 Exxonmobil Research And Engineering Company Process for the desulfurization of heavy oils and bitumens
KR100931036B1 (en) * 2008-03-18 2009-12-10 한국화학연구원 Catalyst for Hydrocracking of Crude Oil and Hydrocracking Method Using the Same
BRPI0911062B1 (en) * 2008-04-10 2018-06-05 Shell Internationale Research Maatschappij B.V. CATALYTIC SYSTEM, METHOD FOR TREATMENT OF RAW FEED AND CATALASIDOR UNDERSTANDING HYDROGENATION METALS AND A SUPPORT
US8114806B2 (en) * 2008-04-10 2012-02-14 Shell Oil Company Catalysts having selected pore size distributions, method of making such catalysts, methods of producing a crude product, products obtained from such methods, and uses of products obtained
EP2628780A1 (en) * 2012-02-17 2013-08-21 Reliance Industries Limited A solvent extraction process for removal of naphthenic acids and calcium from low asphaltic crude oil
JP2013057075A (en) * 2012-11-19 2013-03-28 Shell Internatl Research Maatschappij Bv Lowering process of total acid number (tan) of liquid hydrocarbon quality feedstock
US11788017B2 (en) 2017-02-12 2023-10-17 Magëmã Technology LLC Multi-stage process and device for reducing environmental contaminants in heavy marine fuel oil
US10655074B2 (en) 2017-02-12 2020-05-19 Mag{hacek over (e)}m{hacek over (a)} Technology LLC Multi-stage process and device for reducing environmental contaminates in heavy marine fuel oil
US10604709B2 (en) 2017-02-12 2020-03-31 Magēmā Technology LLC Multi-stage device and process for production of a low sulfur heavy marine fuel oil from distressed heavy fuel oil materials

Family Cites Families (119)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US587636A (en) * 1897-08-03 Blacking-brush and dauber
US2850435A (en) * 1956-02-06 1958-09-02 Pure Oil Co Method of removing high molecular weight naphthenic acids from hydrocarbon oils
US2921023A (en) * 1957-05-14 1960-01-12 Pure Oil Co Removal of naphthenic acids by hydrogenation with a molybdenum oxidesilica alumina catalyst
US3025231A (en) * 1959-06-03 1962-03-13 Texaco Inc Catalytic hydrogenation of heavy oils such as shale oil
NL275200A (en) 1961-07-31
GB1115122A (en) * 1965-08-23 1968-05-29 Universal Oil Prod Co Hydrotreatment of alkyl aromatic hydrocarbons
US3488716A (en) 1967-10-03 1970-01-06 Exxon Research Engineering Co Process for the removal of naphthenic acids from petroleum distillate fractions
US3547585A (en) * 1968-11-26 1970-12-15 Universal Oil Prod Co Combination of a hydrocarbon conversion process with a waste water treating process
US3576737A (en) * 1969-03-25 1971-04-27 Chevron Res Vanadium removal from hydrocarbons
GB1232173A (en) * 1969-11-18 1971-05-19
US3696027A (en) * 1970-01-12 1972-10-03 Chevron Res Multi-stage desulfurization
GB1364238A (en) * 1970-08-04 1974-08-21 Topsoe H F A Process for the hydrodesulphurisation of heavy hydrocarbon oils
US3712861A (en) * 1970-10-19 1973-01-23 Mobil Oil Corp Upgrading a hydrocarbon utilizing a catalyst of metal sulfides dispersed in alumina
US3730876A (en) * 1970-12-18 1973-05-01 A Sequeira Production of naphthenic oils
US3766054A (en) * 1970-12-23 1973-10-16 Mobil Oil Corp Demetalation of hydrocarbon charge stocks
US3684688A (en) * 1971-01-21 1972-08-15 Chevron Res Heavy oil conversion
US3876532A (en) * 1973-02-27 1975-04-08 Gulf Research Development Co Method for reducing the total acid number of a middle distillate oil
US3948759A (en) * 1973-03-28 1976-04-06 Exxon Research And Engineering Company Visbreaking a heavy hydrocarbon feedstock in a regenerable molten medium in the presence of hydrogen
US3902991A (en) * 1973-04-27 1975-09-02 Chevron Res Hydrodesulfurization process for the production of low-sulfur hydrocarbon mixture
IN142203B (en) * 1973-04-30 1977-06-11 Uop Inc
US3960712A (en) * 1973-04-30 1976-06-01 Universal Oil Products Company Hydrodesulfurization of asphaltene-containing black oil with a gamma-alumina composite catalyst of specified particle density
US3846288A (en) * 1973-07-05 1974-11-05 Gulf Research Development Co Acid number reduction of hydrocarbon fractions using a solid catalyst and methanol
US3876523A (en) * 1973-08-29 1975-04-08 Mobil Oil Corp Catalyst for residua demetalation and desulfurization
US3931052A (en) * 1973-08-29 1976-01-06 Mobil Oil Corporation Alumina-supported catalyst for residua demetalation and desulfurization
US3891541A (en) * 1973-08-29 1975-06-24 Mobil Oil Corp Process for demetalizing and desulfurizing residual oil with hydrogen and alumina-supported catalyst
US3920538A (en) 1973-11-30 1975-11-18 Shell Oil Co Demetallation with nickel-vanadium on silica in a hydrocarbon conversion process
JPS51122105A (en) * 1975-04-18 1976-10-26 Toa Nenryo Kogyo Kk Process for hydrofining of hydrocarbon oil
US4062757A (en) * 1975-07-18 1977-12-13 Gulf Research & Development Company Residue thermal cracking process in a packed bed reactor
US4196102A (en) * 1975-12-09 1980-04-01 Chiyoda Chemical Engineering & Construction Co., Ltd. Catalysts for demetallization treatment of _hydrocarbons supported on sepiolite
US4048060A (en) * 1975-12-29 1977-09-13 Exxon Research And Engineering Company Two-stage hydrodesulfurization of oil utilizing a narrow pore size distribution catalyst
US4067799A (en) * 1976-07-02 1978-01-10 Exxon Research And Engineering Company Hydroconversion process
US4127470A (en) * 1977-08-01 1978-11-28 Exxon Research & Engineering Company Hydroconversion with group IA, IIA metal compounds
US4225421A (en) * 1979-03-13 1980-09-30 Standard Oil Company (Indiana) Process for hydrotreating heavy hydrocarbons
US4446244A (en) * 1979-09-26 1984-05-01 Chevron Research Company Hydrocarbons hydroprocessing with imogolite catalyst
US4358361A (en) * 1979-10-09 1982-11-09 Mobil Oil Corporation Demetalation and desulfurization of oil
JPS595011B2 (en) * 1979-11-27 1984-02-02 千代田化工建設株式会社 Catalyst for hydrotreating heavy hydrocarbon oil and its production method
US4301037A (en) * 1980-04-01 1981-11-17 W. R. Grace & Co. Extruded alumina catalyst support having controlled distribution of pore sizes
US4306964A (en) * 1980-09-16 1981-12-22 Mobil Oil Corporation Multi-stage process for demetalation and desulfurization of petroleum oils
US4411824A (en) * 1981-05-12 1983-10-25 Chevron Research Company Method of making a catalyst suitable for hydrometalation of hydrocarbonaceous feedstocks
US4456699A (en) * 1981-06-17 1984-06-26 Standard Oil Company (Indiana) Catalyst and support, and their methods of preparation
US4549957A (en) * 1981-06-17 1985-10-29 Amoco Corporation Hydrotreating catalyst and process
AU547464B2 (en) * 1981-06-17 1985-10-24 Amoco Corporation Catalyst for hydrotreating hydrocarbon feed
US4447314A (en) * 1982-05-05 1984-05-08 Mobil Oil Corporation Demetalation, desulfurization, and decarbonization of petroleum oils by hydrotreatment in a dual bed system prior to cracking
FR2528721B1 (en) * 1982-06-17 1986-02-28 Pro Catalyse Ste Fse Prod Cata SUPPORTED CATALYST HAVING INCREASED RESISTANCE TO POISONS AND ITS USE IN PARTICULAR FOR THE HYDROTREATMENT OF OIL FRACTIONS CONTAINING METALS
US4405441A (en) * 1982-09-30 1983-09-20 Shell Oil Company Process for the preparation of hydrocarbon oil distillates
JPS59150537A (en) * 1982-12-06 1984-08-28 アモコ　コーポレーション Hydrotreating catalyst and hydrotreating of hydrocarbon
US4886594A (en) 1982-12-06 1989-12-12 Amoco Corporation Hydrotreating catalyst and process
US4450068A (en) 1982-12-20 1984-05-22 Phillips Petroleum Company Demetallization of hydrocarbon containing feed streams
JPS59132945A (en) * 1983-01-21 1984-07-31 Shokubai Kasei Kogyo Kk Hydro-demetalation catalyst and use thereof
US4592827A (en) * 1983-01-28 1986-06-03 Intevep, S.A. Hydroconversion of heavy crudes with high metal and asphaltene content in the presence of soluble metallic compounds and water
US4525472A (en) * 1983-02-23 1985-06-25 Intevep, S.A. Process for catalyst preparation for the hydrodemetallization of heavy crudes and residues
JPS6065092A (en) * 1983-09-21 1985-04-13 Res Assoc Petroleum Alternat Dev<Rapad> Removal of metal from oil sand oil and residual oil
US4587012A (en) * 1983-10-31 1986-05-06 Chevron Research Company Process for upgrading hydrocarbonaceous feedstocks
US4520128A (en) * 1983-12-19 1985-05-28 Intevep, S.A. Catalyst having high metal retention capacity and good stability for use in the demetallization of heavy crudes and method of preparation of same
US4588709A (en) * 1983-12-19 1986-05-13 Intevep, S.A. Catalyst for removing sulfur and metal contaminants from heavy crudes and residues
US4572778A (en) * 1984-01-19 1986-02-25 Union Oil Company Of California Hydroprocessing with a large pore catalyst
US4844792A (en) * 1984-08-07 1989-07-04 Union Oil Company Of California Hydroprocessing with a specific pore sized catalyst containing non-hydrolyzable halogen
NL8402997A (en) * 1984-10-01 1986-05-01 Unilever Nv CATALYST MATERIAL.
GB2167430B (en) * 1984-11-22 1988-11-30 Intevep Sa Process for hydroconversion and upgrading of heavy crudes of high metal and asphaltene content
US4600503A (en) * 1984-12-28 1986-07-15 Mobil Oil Corporation Process for hydrotreating residual petroleum oil
US4729826A (en) * 1986-02-28 1988-03-08 Union Oil Company Of California Temperature controlled catalytic demetallization of hydrocarbons
US4738884A (en) * 1986-03-03 1988-04-19 Owens-Corning Fiberglas Corporation Asphalt adhesives superimposed on asphalt-based roofing sheet
US4670134A (en) * 1986-05-02 1987-06-02 Phillips Petroleum Company Catalytic hydrofining of oil
US4830736A (en) * 1986-07-28 1989-05-16 Chevron Research Company Graded catalyst system for removal of calcium and sodium from a hydrocarbon feedstock
JP2631712B2 (en) * 1988-08-18 1997-07-16 コスモ石油株式会社 Catalyst composition for hydrotreating heavy hydrocarbon oil and hydrotreating method using the same
US4992157A (en) * 1988-08-29 1991-02-12 Uop Process for improving the color and color stability of hydrocarbon fraction
JP2609301B2 (en) * 1988-08-31 1997-05-14 工業技術院長 Method for producing hydrotreating catalyst
EP0367021B1 (en) * 1988-10-19 1993-12-29 Research Association For Petroleum Alternatives Development Process for hydrogenation of heavy oil
US5124027A (en) * 1989-07-18 1992-06-23 Amoco Corporation Multi-stage process for deasphalting resid, removing catalyst fines from decanted oil and apparatus therefor
US4992163A (en) * 1989-12-13 1991-02-12 Exxon Research And Engineering Company Cat cracking feed preparation
US4988434A (en) 1989-12-13 1991-01-29 Exxon Research And Engineering Company Removal of metallic contaminants from a hydrocarbonaceous liquid
JPH03292395A (en) * 1989-12-28 1991-12-24 Chevron Res & Technol Co Removal of calcium from hydrocarbon supply material
US5053117A (en) * 1990-07-25 1991-10-01 Mobil Oil Corporation Catalytic dewaxing
US5851381A (en) 1990-12-07 1998-12-22 Idemitsu Kosan Co., Ltd. Method of refining crude oil
US5200060A (en) * 1991-04-26 1993-04-06 Amoco Corporation Hydrotreating process using carbides and nitrides of group VIB metals
US5215954A (en) 1991-07-30 1993-06-01 Cri International, Inc. Method of presulfurizing a hydrotreating, hydrocracking or tail gas treating catalyst
US5210061A (en) * 1991-09-24 1993-05-11 Union Oil Company Of California Resid hydroprocessing catalyst
US5215955A (en) * 1991-10-02 1993-06-01 Chevron Research And Technology Company Resid catalyst with high metals capacity
JP2966985B2 (en) * 1991-10-09 1999-10-25 出光興産株式会社 Catalytic hydrotreating method for heavy hydrocarbon oil
US5399259A (en) * 1992-04-20 1995-03-21 Texaco Inc. Hydroconversion process employing catalyst with specified pore size distribution
EP0569092A1 (en) * 1992-05-05 1993-11-10 Shell Internationale Researchmaatschappij B.V. Hydrotreating process
US5322617A (en) * 1992-08-07 1994-06-21 Her Majesty The Queen In Right Of Canada As Represented By The Minister Of Energy, Mines And Resources Upgrading oil emulsions with carbon monoxide or synthesis gas
JPH0753968A (en) * 1993-08-09 1995-02-28 Idemitsu Kosan Co Ltd Hydrotreatment of heavy hydrocarbon oil
US5928601A (en) * 1994-02-28 1999-07-27 Honda Giken Kogyo Kabushiki Kaisha Method for producing silicon nitride reaction sintered body
NO303837B1 (en) * 1994-08-29 1998-09-07 Norske Stats Oljeselskap Process for removing substantially naphthenic acids from a hydrocarbon oil
JP3504984B2 (en) * 1994-09-19 2004-03-08 日本ケッチェン株式会社 Hydrodesulfurization demetallization catalyst for heavy hydrocarbon oil
US5635056A (en) * 1995-05-02 1997-06-03 Exxon Research And Engineering Company Continuous in-situ process for upgrading heavy oil using aqueous base
US5807469A (en) * 1995-09-27 1998-09-15 Intel Corporation Flexible continuous cathode contact circuit for electrolytic plating of C4, tab microbumps, and ultra large scale interconnects
JP3315314B2 (en) 1996-05-30 2002-08-19 矢崎総業株式会社 Low insertion force connector
JPH1060456A (en) * 1996-08-15 1998-03-03 Catalysts & Chem Ind Co Ltd Hydrogenation treatment of heavy oil and device for hydrogenation treatment
FR2758278B1 (en) * 1997-01-15 1999-02-19 Inst Francais Du Petrole CATALYST COMPRISING A MIXED SULFIDE AND USE IN HYDRO-REFINING AND HYDROCONVERSION OF HYDROCARBONS
US5744025A (en) 1997-02-28 1998-04-28 Shell Oil Company Process for hydrotreating metal-contaminated hydrocarbonaceous feedstock
US6162350A (en) * 1997-07-15 2000-12-19 Exxon Research And Engineering Company Hydroprocessing using bulk Group VIII/Group VIB catalysts (HEN-9901)
US5910242A (en) * 1997-08-29 1999-06-08 Exxon Research And Engineering Company Process for reduction of total acid number in crude oil
US5871636A (en) 1997-08-29 1999-02-16 Exxon Research And Engineering Company Catalytic reduction of acidity of crude oils in the absence of hydrogen
US5897769A (en) * 1997-08-29 1999-04-27 Exxon Research And Engineering Co. Process for selectively removing lower molecular weight naphthenic acids from acidic crudes
BR9811387A (en) * 1997-08-29 2000-08-29 Exxon Research Engineering Co Process to reduce the amount of carboxylic acids in oil feeds
US5928502A (en) 1997-08-29 1999-07-27 Exxon Research And Engineering Co. Process for reducing total acid number of crude oil
US5914030A (en) 1997-08-29 1999-06-22 Exxon Research And Engineering. Co. Process for reducing total acid number of crude oil
US5928501A (en) * 1998-02-03 1999-07-27 Texaco Inc. Process for upgrading a hydrocarbon oil
JP2000005609A (en) * 1998-06-26 2000-01-11 Idemitsu Kosan Co Ltd Method for regeneration of hydrotreating catalyst
US6096192A (en) 1998-07-14 2000-08-01 Exxon Research And Engineering Co. Producing pipelinable bitumen
US6258258B1 (en) * 1998-10-06 2001-07-10 Exxon Research And Engineering Company Process for treatment of petroleum acids with ammonia
FR2787041B1 (en) * 1998-12-10 2001-01-19 Inst Francais Du Petrole HYDROCARBON CHARGE HYDROTREATMENT CATALYST IN A FIXED BED REACTOR
FR2787040B1 (en) 1998-12-10 2001-01-19 Inst Francais Du Petrole HYDROTREATMENT OF HYDROCARBON CHARGES IN A BOILING BED REACTOR
US6218333B1 (en) * 1999-02-15 2001-04-17 Shell Oil Company Preparation of a hydrotreating catalyst
US6554994B1 (en) * 1999-04-13 2003-04-29 Chevron U.S.A. Inc. Upflow reactor system with layered catalyst bed for hydrotreating heavy feedstocks
JP3824464B2 (en) * 1999-04-28 2006-09-20 財団法人石油産業活性化センター Method for hydrocracking heavy oils
FR2792851B1 (en) * 1999-04-29 2002-04-05 Inst Francais Du Petrole LOW-DISPERSE NOBLE METAL-BASED CATALYST AND USE THEREOF FOR THE CONVERSION OF HYDROCARBON CHARGES
JP2003171671A (en) * 2000-06-08 2003-06-20 Japan Energy Corp Method for hydrogenation refining of heavy oil
US20020056664A1 (en) * 2000-09-07 2002-05-16 Julie Chabot Extension of catalyst cycle length in residuum desulfurization processes
US6547957B1 (en) 2000-10-17 2003-04-15 Texaco, Inc. Process for upgrading a hydrocarbon oil
US7384537B2 (en) * 2000-10-24 2008-06-10 Jgc Corporation Refined oil and process for producing the same
US20020112987A1 (en) * 2000-12-15 2002-08-22 Zhiguo Hou Slurry hydroprocessing for heavy oil upgrading using supported slurry catalysts
US6759364B2 (en) 2001-12-17 2004-07-06 Shell Oil Company Arsenic removal catalyst and method for making same
GB0209222D0 (en) 2002-04-23 2002-06-05 Bp Oil Int Purification process
JP2003181292A (en) * 2002-12-25 2003-07-02 Chevron Research & Technology Co Highly active catalyst for treating residual oil
BRPI0405565A (en) * 2003-12-19 2005-08-30 Shell Int Research Methods of Producing a Transportable Fuel and Crude Oil Product, Heating Fuel, Lubricants or Chemicals, and Crude Oil Product
US10535462B2 (en) 2007-04-05 2020-01-14 Hans Wennerstrom Flat winding / equal coupling common mode inductor apparatus and method of use thereof

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CA2551096C (en) 2013-03-12
CA2549258A1 (en) 2005-07-21
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CA2549088A1 (en) 2005-07-14
NL1027755C2 (en) 2006-07-13
EP1704211A2 (en) 2006-09-27
JP2007514837A (en) 2007-06-07
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WO2005063926A3 (en) 2006-01-05
WO2005061670A2 (en) 2005-07-07
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JP2007521386A (en) 2007-08-02
MXPA06006794A (en) 2006-08-23
NL1027772C2 (en) 2006-08-29
CA2549251C (en) 2014-02-11
CA2549427C (en) 2013-09-24
JP2007514850A (en) 2007-06-07
AU2004303873A1 (en) 2005-07-07
NL1027752C2 (en) 2006-08-31
CA2562759A1 (en) 2005-07-21
TW200535225A (en) 2005-11-01
NL1027766A1 (en) 2005-06-22
CA2652088A1 (en) 2005-07-14
CA2549886C (en) 2015-03-17
NL1027764A1 (en) 2005-06-22
BRPI0405535B1 (en) 2014-09-16
MXPA06006795A (en) 2006-08-23
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