EP0385538B1 - Verfahren zur Umwandlung von Kohlenwasserstoffen - Google Patents

Verfahren zur Umwandlung von Kohlenwasserstoffen Download PDF

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Publication number
EP0385538B1
EP0385538B1 EP90200415A EP90200415A EP0385538B1 EP 0385538 B1 EP0385538 B1 EP 0385538B1 EP 90200415 A EP90200415 A EP 90200415A EP 90200415 A EP90200415 A EP 90200415A EP 0385538 B1 EP0385538 B1 EP 0385538B1
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EP
European Patent Office
Prior art keywords
feedstock
process according
catalyst
zeolite
conversion
Prior art date
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Revoked
Application number
EP90200415A
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English (en)
French (fr)
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EP0385538A1 (de
Inventor
Jaydeep Biswas
Ian Ernest Maxwell
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.)
Shell Internationale Research Maatschappij BV
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Shell Internationale Research Maatschappij BV
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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
    • C10G35/00—Reforming naphtha
    • C10G35/04—Catalytic reforming
    • C10G35/10—Catalytic reforming with moving catalysts
    • 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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/16—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "moving bed" method

Definitions

  • the present invention relates to a process for the conversion of a hydrocarbonaceous feedstock.
  • US 4,514,285 discloses as illustration of a method for ballistic separation of conversion catalyst from hydrocarbonaceous products, conditions for conversion of a gas oil feed in a downflow reactor over an unspecified high activity, high alumina zeolite type cracking catalyst but makes no reference to degree of conversion or nature of products thereby obtained.
  • US 4,171,257 describes a process for upgrading a hydrocarbonaceous feedstock by contacting the feedstock with a ZSM-5 crystalline aluminosilicate catalyst at a pressure below 14 bar, a temperature of 260 to 427 °C and a space velocity of 0.1 to 15 l/l.h.
  • the feedstock exemplified as gas oil having a boiling point range of 230 to 437 °C, must contain less than 5 ppmw of nitrogen-containing compounds, calculated as nitrogen.
  • the upgraded product includes olefinic hydrocarbons, such as propene and butenes.
  • the present invention provides a process for the conversion of a straight-run hydrocarbonaceous feedstock containing hydrocarbons having such a boiling range that an amount thereof boils at a temperature of at least 330 °C, which process comprises contacting the feedstock with a moving bed of a zeolitic catalyst comprising a zeolite with a pore diameter of 0.3 to 0.7 nm, preferably 0.5 to 0.7 nm, at a temperature of greater than 480 °C during less than 10 seconds.
  • the feedstock is contacted with the zeolitic catalyst for less than 10 seconds.
  • the minimum contact time is 0.1 second. Very good results are obtainable with a process in which the feedstock is contacted with the zeolitic catalyst during 0.2 to 6 seconds.
  • the temperature during the reaction is relatively high. It is this combination of high temperature and short contact time which allows a high conversion to olefins.
  • a preferred temperature range is 500 to 900 °C, more preferably 550 to 850 °C.
  • the zeolitic catalyst may comprise one or more zeolites with a pore diameter of from 0.3 to 0.7 nm.
  • the catalyst suitably further comprises a refractory oxide that serves as binder material. Suitable refractory oxides include alumina, silica, silica-alumina, magnesia, titania, zirconia and mixtures thereof. Alumina is especially preferred.
  • the weight ratio of refractory oxide and zeolite suitably ranges from 10:90 to 90:10, preferably from 50:50 to 85:15.
  • the catalyst may comprise up to about 40% by weight of further zeolites with a pore diameter above 0.7 nm.
  • zeolites include the faujasite-type zeolites, zeolite beta, zeolite omega and in particular zeolite X and Y.
  • the zeolitic catalyst preferably comprises as zeolite substantially only zeolites with a pore diameter of from 0.3 to 0.7 nm.
  • zeolite in this specification is not to be regarded as comprising only crystalline aluminium silicates.
  • the term also includes crystalline silica (silicalite), silicoaluminophosphates (SAPO), chromosilicates, gallium silicates, iron silicates, aluminium phosphates (ALPO), titanium aluminosilicates (TASO), boron silicates, titanium aluminophosphates (TAPO) and iron aluminosilicates.
  • Examples of zeolites that may be used in the process of the invention and that have a pore diameter of 0.3 to 0.7 nm include SAPO-4 and SAPO-11, which are described in US-A-4,440,871, ALPO-11, described in US-A-4,310,440, TAPO-11, described in US-A-4,500,651, TASO-45, described in EP-A-229,295, boron silicates, described in e.g. US-A-4,254,297, aluminium silicates like erionite, ferrierite, theta and the ZSM-type zeolites such as ZSM-5, ZSM-11, ZSM-12, ZSM-35, ZSM-23, and ZSM-38.
  • SAPO-4 and SAPO-11 which are described in US-A-4,440,871, ALPO-11, described in US-A-4,310,440, TAPO-11, described in US-A-4,500,651, TASO-45, described in EP-A-229,29
  • the zeolite is selected from the group consisting of crystalline metal silicates having a ZSM-5 structure, ferrierite, erionite and mixtures thereof.
  • crystalline metal silicates with ZSM-5 structure are aluminium, gallium, iron, scandium, rhodium and/or scandium silicates as described in e.g. GB-B-2,110,559.
  • the zeolites usually a significant amount of alkali metal oxide is present in the prepared zeolite.
  • the amount of alkali metal is removed by methods known in the art, such as ion exchange, optionally followed by calcination, to yield the zeolite in its hydrogen form.
  • the zeolite used in the present process is substantially in its hydrogen form.
  • the pressure in the present process can be varied within wide ranges. It is, however, preferred that the pressure is such that at the prevailing temperature the feedstock is substantially in its gaseous phase or brought thereinto by contact with the catalyst. Then it is easier to achieve the short contact times envisaged. Hence, the pressure is preferably relatively low. This can be advantageous since no expensive compressors and high-pressure vessels and other equipment are necessary. A suitable pressure range is from 1 to 10 bar. Subatmospheric pressures are possible, but not preferred. It can be economically advantageous to operate at atmospheric pressure. Other gaseous materials may be present during the conversion such as steam and/or nitrogen.
  • the present process is carried out in a moving bed.
  • the bed of catalyst may move upwards or downwards.
  • When the bed moves upwards a process somewhat similar to a fluidized catalytic cracking process is obtained.
  • the catalyst is regenerated by subjecting it, after having been contacted with the feedstock, to a treatment with an oxidizing gas, such as air.
  • a continuous regeneration similar to the regeneration carried out in a fluidized catalytic cracking process, is especially preferred.
  • the residence time of the catalyst particles in a reaction zone is longer than the residence time of the feedstock in the reaction zone.
  • the contact time between feedstock and catalyst should be less than 10 seconds.
  • the contact time generally corresponds with the residence time of the feedstock.
  • the residence time of the catalyst is from 1 to 20 times the residence time of the feedstock.
  • the catalyst/feedstock weight ratio may vary widely, for example up to 150 kg of catalyst per kg of feedstock or even more. Preferably, the catalyst/feedstock weight ratio is from 20 to 100:1.
  • the feedstock which is to be converted in the present process comprises hydrocarbons which have a boiling point of at least 330 °C.
  • hydrocarbons which have a boiling point of at least 330 °C.
  • relatively light petroleum fractions such as naphtha and kerosine, have been excluded.
  • the feedstock has such a boiling range that at least 50% by weight thereof boils at a temperature of 330 °C.
  • Suitable feedstocks include vacuum distillates, long residues, deasphalted residual oils, paraffinic feedstocks and atmospheric distillates which fulfil the requirement as to boiling range, such as gas oils.
  • the feedstock is a gas oil or vacuum gas oil. When these feedstocks are subjected to the present process a gas oil with a very low pour point and an olefin-rich gaseous fraction are obtained.
  • a feedstock with a nitrogen content greater than 5 ppmw may be used with substantially no effect on the catalyst activity.
  • Suitable feedstocks may have a nitrogen content of more than 10 ppmw, calculated as nitrogen.
  • the feedstock may even have a nitrogen content of 1000 ppmw or more, calculated as nitrogen.
  • the feedstock in this example was a gas oil having the following properties: IBP, °C 213 20 %wt 331 50 %wt 379 90 %wt 421 FBP 448 pour point, °C 19.5 flash point, °C 147 carbon, %wt 86.6 hydrogen, %wt 13.1 sulphur, %wt 0.3 nitrogen, ppmw 330
  • the gas oil was treated in a down flow reactor in which co-currently a flow of feedstock and catalyst particles, having an average particle size of 74 micrometers, was passed downwards.
  • the catalyst used comprised ZSM-5, in hydrogen form, in an alumina matrix (weight ratio ZSM-5/alumina was 1:3). All experiments were carried out at atmospheric pressure. Further process conditions and the results of the experiments are indicated in the table below.

Claims (9)

  1. Ein Verfahren zur Umwandlung eines durch Destillation gewonnenen kohlenwasserstoffhaltigen Ausgangsmaterials mit einem Stickstoffgehalt von mehr als 5 TpM (Gew), welcher Kohlenwasserstoffe mit einem solchen Siedebereich aufweist, daß eine Anteilsmenge davon bei einer Temperatur von wenigstens 330°C siedet, welches Verfahren das in-Berührung-bringen des Ausgangsmaterials mit einem Fließbett aus einem Zeolith-Katalysator, umfassend einen Zeolith mit einem Porendurchmesser von 0,3 bis 0,7 nm, bei einer Temperatur von mehr als 480°C während weniger als 10 Sekunden, umfaßt.
  2. Ein Verfahren nach Anspruch 1, in dem das Ausgangsmaterial mit dem Zeolith-Katalysator während 0,2 bis 6 Sekunden in Berührung gebracht wird.
  3. Ein Verfahren nach Anspruch 1 oder 2, in dem die Temperatur 550 bis 850°C beträgt.
  4. Ein Verfahren nach irgendeinem der vorhergehenden Ansprüche, in dem der Zeolith einen Porendurchmesser von 0,5 bis 0,7 nm hat.
  5. Ein Verfahren nach irgendeinem der vorhergehenden Ansprüche, in dem der Zeolith aus kristallinen Metallsilikaten mit einer ZSM-5-Struktur, Ferrierit, Erionit und deren Gemischen ausgewählt ist.
  6. Ein Verfahren nach irgendeinem der vorhergehenden Ansprüche, in dem der Zeolith im wesentlichen in seiner Wasserstoff-Form vorhanden ist.
  7. Ein Verfahren nach irgendeinem der vorhergehenden Ansprüche, in dem der Druck von 1 bis 10 bar reicht.
  8. Ein Verfahren nach irgendeinem der vorhergehenden Ansprüche, in dem das Gewichtsverhältnis Katalysator/Ausgangsmaterial von 20 bis 100:1 reicht.
  9. Ein Verfahren nach irgendeinem der vorhergehenden Ansprüche, in dem die Zuspeisung ein Gasöl ist.
EP90200415A 1989-02-27 1990-02-21 Verfahren zur Umwandlung von Kohlenwasserstoffen Revoked EP0385538B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB8904408 1989-02-27
GB898904408A GB8904408D0 (en) 1989-02-27 1989-02-27 Process for the conversion of a hydrocarbonaceous feedstock

Publications (2)

Publication Number Publication Date
EP0385538A1 EP0385538A1 (de) 1990-09-05
EP0385538B1 true EP0385538B1 (de) 1994-06-01

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ID=10652368

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EP90200415A Revoked EP0385538B1 (de) 1989-02-27 1990-02-21 Verfahren zur Umwandlung von Kohlenwasserstoffen

Country Status (11)

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EP (1) EP0385538B1 (de)
JP (1) JPH02276888A (de)
KR (1) KR910015689A (de)
CN (1) CN1019981C (de)
AU (1) AU628929B2 (de)
BR (1) BR9000880A (de)
CA (1) CA2009986A1 (de)
DE (1) DE69009234T2 (de)
ES (1) ES2056362T3 (de)
GB (1) GB8904408D0 (de)
RU (1) RU2017791C1 (de)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6222087B1 (en) 1999-07-12 2001-04-24 Mobil Oil Corporation Catalytic production of light olefins rich in propylene
US6835863B2 (en) 1999-07-12 2004-12-28 Exxonmobil Oil Corporation Catalytic production of light olefins from naphtha feed

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB9026775D0 (en) * 1990-12-10 1991-01-30 Shell Int Research Process for the preparation of an olefins-containing mixture of hydrocarbons
GB9114390D0 (en) * 1991-07-03 1991-08-21 Shell Int Research Hydrocarbon conversion process and catalyst composition
EP1195424A1 (de) 2000-10-05 2002-04-10 ATOFINA Research Verfahren zur Krackung von olefinreichen Kohlenwasserstoffeinsätzen
DE102012006992A1 (de) * 2012-04-05 2013-10-10 Linde Aktiengesellschaft Verfahren zur Trennung von Olefinen bei milder Spaltung
WO2017109639A1 (en) 2015-12-21 2017-06-29 Sabic Global Technologies B.V. Methods and systems for producing olefins and aromatics from coker naphtha

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0349036A1 (de) * 1988-06-16 1990-01-03 Shell Internationale Researchmaatschappij B.V. Verfahren zur Umwandlung eines kohlenwasserstoffartigen Ausgangsmaterials

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3856659A (en) * 1972-12-19 1974-12-24 Mobil Oil Corp Multiple reactor fcc system relying upon a dual cracking catalyst composition
US4514285A (en) * 1983-03-23 1985-04-30 Texaco Inc. Catalytic cracking system
US4985136A (en) * 1987-11-05 1991-01-15 Bartholic David B Ultra-short contact time fluidized catalytic cracking process
ES2087073T3 (es) * 1988-06-16 1996-07-16 Shell Int Research Procedimiento para la conversion de un material de alimentacion hidrocarbonado.
NL8801653A (nl) * 1988-06-29 1990-01-16 Stork Kwant Bv Besturingsstelsel.
GB8828206D0 (en) * 1988-12-02 1989-01-05 Shell Int Research Process for conversion of hydrocarbonaceous feedstock

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0349036A1 (de) * 1988-06-16 1990-01-03 Shell Internationale Researchmaatschappij B.V. Verfahren zur Umwandlung eines kohlenwasserstoffartigen Ausgangsmaterials

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6222087B1 (en) 1999-07-12 2001-04-24 Mobil Oil Corporation Catalytic production of light olefins rich in propylene
US6835863B2 (en) 1999-07-12 2004-12-28 Exxonmobil Oil Corporation Catalytic production of light olefins from naphtha feed

Also Published As

Publication number Publication date
CN1045120A (zh) 1990-09-05
DE69009234D1 (de) 1994-07-07
AU5014990A (en) 1990-08-30
BR9000880A (pt) 1991-02-13
RU2017791C1 (ru) 1994-08-15
ES2056362T3 (es) 1994-10-01
KR910015689A (ko) 1991-09-30
GB8904408D0 (en) 1989-04-12
JPH02276888A (ja) 1990-11-13
DE69009234T2 (de) 1994-11-24
CA2009986A1 (en) 1990-08-27
CN1019981C (zh) 1993-03-03
AU628929B2 (en) 1992-09-24
EP0385538A1 (de) 1990-09-05

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