EP1836282A2 - Production de diesels ne contenant pratiquement pas d'aromatisants - Google Patents

Production de diesels ne contenant pratiquement pas d'aromatisants

Info

Publication number
EP1836282A2
EP1836282A2 EP05826703A EP05826703A EP1836282A2 EP 1836282 A2 EP1836282 A2 EP 1836282A2 EP 05826703 A EP05826703 A EP 05826703A EP 05826703 A EP05826703 A EP 05826703A EP 1836282 A2 EP1836282 A2 EP 1836282A2
Authority
EP
European Patent Office
Prior art keywords
diesel
synthetically derived
previous
derived diesel
catalyst
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
EP05826703A
Other languages
German (de)
English (en)
Inventor
Cyril David Knottenbelt
Carl Dunlop
Kholekile Zono
Maxwell Thomas
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Petroleum Oil and Gas Corp of South Africa Pty Ltd
Original Assignee
Petroleum Oil and Gas Corp of South Africa Pty Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Petroleum Oil and Gas Corp of South Africa Pty Ltd filed Critical Petroleum Oil and Gas Corp of South Africa Pty Ltd
Publication of EP1836282A2 publication Critical patent/EP1836282A2/fr
Ceased legal-status Critical Current

Links

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
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/12—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step
    • C10G69/126—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step polymerisation, e.g. oligomerisation

Definitions

  • This invention relates to a process for the production of synthetically derived near zero aromatic content diesel.
  • Crude derived diesels are not popular due to their high sulphur content.
  • a process for the production of synthetically derived diesel which process includes the steps of: catalytic conversion of Fisher-Tropsch derived light olefins to distillates
  • COD COD
  • zeolite type catalyst at pressures of more than 50barg; one step hydrotreating the COD product to simultaneously hydrogenate both olefins and aromatics; and collecting a hydrotreated fraction boiling between about 180 0 C to 360 ° C.
  • the Fisher-Tropsch derived olefins are converted to distillates over a shape selective zeolite type catalyst, a COD-9 or similar catalyst as defined by the International Zeolite Association (IZA). More specifically the Fisher- Tropsch derived light olefins comprising of carbon numbers 3 to 6 are oligomerised and isomerised to produce an intermediate highly branched olefinnic distillate.
  • IZA International Zeolite Association
  • the catalytic conversion reactor temperature may be maintained below 280 ° C.
  • the one step deep hydrotreating step may include hydrogenation over a Group 10 metal catalyst.
  • the Group 10 metal catalyst may include a high nickel content.
  • the Group 10 catalyst may include a noble metal catalyst such as supported platinum catalysts. These catalysts may also be bimetallic.
  • the support for the metal may be neutral.
  • the applicant is aware that an acidic support causes unwanted cracking during hydrogenation.
  • the catalyst may be Nickel supported on alumina or platinum supported on allumina. (Sud Chemie G134 or Axens LD 402).
  • the one step hydrotreating step may include hydrogenation over a high nickel content hydrotreating catalyst or hydrotreating with a noble metal catalyst.
  • Reactor pressures for such reactions would typically range from 5000 kPa to about 8000 kPa but not excluding higher pressures.
  • Reaction temperatures vary from about 200 0 C to 260 " C while the LHSV range from 0.3 to 2 depending on the feed.
  • the olefin content measured as Bromine Number determines the reactivity of a particular feed, highly reactive feeds may require a portion of the hydrogenated product to be recycled to quench the hydrogenation reaction.
  • the LHSV may also be altered to below 0.5 to control excessive exothermic reactions.
  • the catalyst may be loaded into the reactor bed in an increased graded approach to limit an excessive exothermic reaction developing at the top of the reactor.
  • the catalyst bed may have multiple zones with increased grades. Typically, a 4-zone graded catalyst bed.
  • the concentration of the active catalyst in each of the 4 zones may be diluted with an inert ceramic in the following typical ratios of catalyst to ceramics, 0.2; 0.5; 170.0 and 650.
  • the Fisher-Tropsch derived olefins are converted to distillates over a shape selective zeolite catalyst.
  • the conversion includes oligomerising and isomerising of the Fisher-Tropsch derived olefins to produce an intermediate olefinic COD product.
  • the process may include the step of blending the intermediate COD product or the hydrotreated fraction with crude derived diesels to enhance performance and/ or emission properties of crude derived diesels.
  • the process may include' the step of blending the intermediate COD product or the hydrotreated fraction with biodiesel derived from vegetable oils to improve the cold flow properties and motoring performance of the biodiesel.
  • the process may include the step of blending the intermediate COD product or the hydrotreated fraction with alcohols to reduce particulate matter emissions from fuels derived from intermediate COD product or the hydrotreated fraction.
  • the alcohols may range from 1 to 5 carbon alcohols, preferably 2 to 5 carbon alcohols.
  • a synthetically derived diesel produced by a catalytic conversion of Fisher- Tropsch derived olefins to distillates (COD) and deep hydrotreating thereof, the diesel boiling in the range of about 180 to 360 ° C, and including: less than 10% n-paraffins; more than 60% iso-paraffins; and less than 1 % aromatics.
  • the iso-paraffins may be predominantly methyl branched.
  • the methyl branched iso-paraffins may range between 50 and 80%, preferably between 60 and 70%, of the iso-paraffins.
  • the diesel may include about 20% naphtenes.
  • the naphtenes may be predominantly monocyclics.
  • the applicant has found that a relatively high cetane number can be maintained by replacing n-paraffins with predominantly methyl branched iso- paraffins and monocyclic naphtenes instead of more branched iso-paraffins and bicyclic naphtenes.
  • the boiling range may be between 180 and 360 0 C, however preferably between 210 and 345 ° C.
  • the flash point of the diesel as measured by ASTM D93 may be higher than 6O 0 C but preferably as high as 100 ° C significantly improving the safety of product during handling.
  • the diesel fuels kinematic viscosity at 40 ° C as measured by ASTM D445 may be below about 5.0 cSt but not lower than 2.0 cSt as measured at 40 ° C.
  • the kinematic viscosity plays a role in the diesel fuel pump ability as well as the fuel injectors ability to efficiently inject fuel. High viscosity fuels negatively influence the fuel atomisation process limiting the formation fine droplets that lead to poor air fuel mixing within the combustion chamber (cylinder) resulting in turn in incomplete combustion accompanied by loss of power and economy.
  • the cold flow properties are excellent due to the over 800 isoparaffinic hydrocarbon molecules that the diesel fuel comprises of.
  • Low temperature operability is measured by Cold Filter Plugging Point (CFPP) as tested by IP 85
  • the total sulphur content of the diesel may be below 2 ppm (m/m) as measured by ASTM 3120. Sulphur in diesels creates a distinctive odour and contributes to the emission of particulate matter during combustion. Fuels with such low sulphurs enable modern vehicle exhaust emission treatment technologies.
  • the olefins content may be respectively reflected by a Bromine
  • the diesel may include blends with crude derived diesels in 10 to 90%v/v, preferably 30 to 70%v/v ratios.
  • the diesel may include blends with biodiesel derived from vegetable oils.
  • the diesel may include blends with 1 to 5 carbon alcohols in 0.5 to
  • compositions of the fuels are such that once combusted they offer excellent environmental benefits over crude derived diesel fuels.
  • Exhaust emission qualities as tested on heavy-duty vehicles and compared against a standard US pump crude derived diesel fuel offered reductions in the following regulated emissions; particulate matter, oxides of nitrogen, carbon monoxide, carbon dioxide and hydrocarbons.
  • the catalysts (about 270 cc) were loaded into a pilot plant reactor in a graded bed format and diluted with inert ceramics in the ratios of catalyst to ceramics of, 0.2; 0.5; 170.0 and 650.
  • the reactor pressure was maintained at 58 bar, the WABT did not exceed 220 ° C 1 the LHSV was maintained at 0.9 and a third of the product was recycled back to the feed.
  • the one step hydrotreated distillate was fractioned by means of a true boiling point distillation apparatus to yield a diesel fraction in the boiling range 220 ° C to 340 ° C.
  • This fuel was found to contain less than 0.1 % v/v aromatics and no detectable polyaromatic hydrocarbons.
  • the fuel typical quality is depicted below:
  • the one step hydrotreated distillate was fractioned by means of a true boiling point distillation apparatus to yield a diesel fraction in the boiling range 220 ° C to 340 ° C. This fuel was found to contain less than 0.1 % v/v aromatics.
  • the fuel was dosed with a commercial lubricity additive (OLI 5000) as supplied by Ethyl at a dose rate of 150 ppm v/v. This was found to be an ideal additive for sulphur free synthetically derived fuels as produce by the above process.
  • OLI 5000 commercial lubricity additive
  • the fuel typical quality is depicted below:
  • the % branching of iso-paraffins methyl 60 to 70; ethyl 2 to 10; propyl 0.2 to 5; butyl 0.1 to 5; hexyl ⁇ .1 to 2.
  • the NMR branching index is 0.165, 0 indicating absence of branching and 1 indicating full branching.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un procédé permettant de produire un diesel dérivé synthétiquement ainsi que le diesel ainsi produit. Ledit procédé consiste notamment à convertir de manière catalytique des oléfines légères dérivées suivant le procédé Fisher-Tropsch en distillats (COD) sur un catalyseur du type zéolite à des pressions supérieures à 50 barg, à hydrotraiter le produit COD de façon à hydrogéner simultanément les oléfines et les aromatisants et à recueillir une fraction hydrotraitée bouillant à une température comprise entre environ 180 °C et environ 360 °C.
EP05826703A 2004-12-23 2005-12-20 Production de diesels ne contenant pratiquement pas d'aromatisants Ceased EP1836282A2 (fr)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
ZA200410360 2004-12-23
US65347105P 2005-02-16 2005-02-16
ZA200501372 2005-02-16
ZA200501373 2005-02-16
PCT/ZA2005/000185 WO2006069407A2 (fr) 2004-12-23 2005-12-20 Production de diesels ne contenant pratiquement pas d'aromatisants

Publications (1)

Publication Number Publication Date
EP1836282A2 true EP1836282A2 (fr) 2007-09-26

Family

ID=36085223

Family Applications (1)

Application Number Title Priority Date Filing Date
EP05826703A Ceased EP1836282A2 (fr) 2004-12-23 2005-12-20 Production de diesels ne contenant pratiquement pas d'aromatisants

Country Status (3)

Country Link
US (1) US20080250699A1 (fr)
EP (1) EP1836282A2 (fr)
WO (1) WO2006069407A2 (fr)

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20090125797A (ko) 2007-02-26 2009-12-07 더 페트롤리엄 오일 앤드 개스 코퍼레이션 오브 사우스 아프리카 (프로프라이어터리) 리미티드 바이오디젤 연료
CA2617614C (fr) 2007-08-10 2012-03-27 Indian Oil Corporation Limited Nouveau carburant synthetique et son procede de preparation
US7955495B2 (en) * 2008-07-31 2011-06-07 Chevron U.S.A. Inc. Composition of middle distillate
US20130109603A1 (en) * 2011-10-31 2013-05-02 Shell Oil Company Fuel and engine oil composition and its use
AP2014008121A0 (en) * 2012-05-11 2014-12-31 Pet Oil & Gas Corp S Africa Conversion of alcohols to distillates

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2362208A1 (fr) * 1976-08-17 1978-03-17 Inst Francais Du Petrole Procede de valorisation d'effluents obtenus dans des syntheses de type fischer-tropsch
US4544792A (en) * 1984-12-13 1985-10-01 Mobil Oil Corporation Upgrading Fischer-Tropsch olefins
FR2620724B1 (fr) * 1987-09-17 1994-04-15 Institut Francais Petrole Procede de production d'oligomeres d'olefines, utilisant un catalyseur a base de mordenite modifiee
EP1299506B1 (fr) * 2000-07-10 2016-03-16 Sasol Technology (Proprietary) Limited Procede et dispositif servant a produire des carburants diesel par oligomerisation de flux de charges olefiniques
US6605206B1 (en) * 2002-02-08 2003-08-12 Chevron U.S.A. Inc. Process for increasing the yield of lubricating base oil from a Fischer-Tropsch plant
US6822126B2 (en) * 2002-04-18 2004-11-23 Chevron U.S.A. Inc. Process for converting waste plastic into lubricating oils

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2006069407A2 *

Also Published As

Publication number Publication date
WO2006069407A3 (fr) 2006-08-31
US20080250699A1 (en) 2008-10-16
WO2006069407A2 (fr) 2006-06-29

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