CA2056833A1 - Process for the preparation of an olefins-containing mixture of hydrocarbons - Google Patents
Process for the preparation of an olefins-containing mixture of hydrocarbonsInfo
- Publication number
- CA2056833A1 CA2056833A1 CA002056833A CA2056833A CA2056833A1 CA 2056833 A1 CA2056833 A1 CA 2056833A1 CA 002056833 A CA002056833 A CA 002056833A CA 2056833 A CA2056833 A CA 2056833A CA 2056833 A1 CA2056833 A1 CA 2056833A1
- Authority
- CA
- Canada
- Prior art keywords
- catalyst
- process according
- zeolite
- feedstock
- olefins
- 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.)
- Abandoned
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
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
- C10G11/04—Oxides
- C10G11/05—Crystalline alumino-silicates, e.g. molecular sieves
-
- 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
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
Abstract
A B S T R A C T
PROCESS FOR THE PREPARATION OF AN
OLEFINS-CONTAINING MIXTURE OF HYDROCARBONS
Process for the preparation of an olefins-containing mixture of hydrocarbons, which process comprises contacting a hydro-carbonaceous feedstock with a zeolitic catalyst at a temperature above 480 °C during less than 10 seconds, whereby the catalyst/-feedstock weight ratio is in the range from 5 to 150 and the zeolitic catalyst comprises a zeolite with a pore diameter of 0.3 to 0.7 nm and an average crystalline size of less than 2 micro-meter.
PROCESS FOR THE PREPARATION OF AN
OLEFINS-CONTAINING MIXTURE OF HYDROCARBONS
Process for the preparation of an olefins-containing mixture of hydrocarbons, which process comprises contacting a hydro-carbonaceous feedstock with a zeolitic catalyst at a temperature above 480 °C during less than 10 seconds, whereby the catalyst/-feedstock weight ratio is in the range from 5 to 150 and the zeolitic catalyst comprises a zeolite with a pore diameter of 0.3 to 0.7 nm and an average crystalline size of less than 2 micro-meter.
Description
2~6~3 PROCESS FOR THE PREPARATION OF AN
OLEFINS-CONTAINING MIXTURE OF ~YDROCARBONS
The present invention relates to a process for the preparation of an olefins-containing mixture of hydrocarbons.
There is considerable interest in the production of olefins, especially ethylene and propylene, as their reactivity renders them suitable for conversion to further products, in contrast to the low value lower paraffins.
It is known to convert hydrocarbonaceous feedstocks, such as light distillates, to products rich in lower olefins, especially ethylene and propylene, by high temperature steam cracking. The typical product slate obtained in such steam cracking processes is not entirely suited to the needs of the chemical industry in that it represents a relatively high methane production level and a high ratio of ethylene to propylene.
There have recently been developed alternative processes for the production of lower olefins, for example as described in EP
0347003, EP 0392590 and EP 0385538, from a wide range of hydro-carbonaceous feedstocks. Those processes have been found to give surprisingly high yiels of lower olefins, low amounts of methane and a low ratio of ethylene to propylene and C4 olefins when compared with conventional steam cracking.
Ethylene and propylene are valuable starting materials for chemical processes, while C4 olefins can find use as a starting material for alkylation and/or oligomerizat$on procedures in order to produce high octane gasoline and/or middle distillates.
Isobutene can be usefully converted to methyl t-butyl ether.
Surprisingly, it has now been found that even higher yields of lower olefins and lower ratios of ethylene to propylene can be obtained in comparison with the above-cited processes if use is made of a zeolitic catalyst comprising a zeolite having a specific average crystallite size.
2Q~6~3 Accordingly, the present invention relates to process for the preparation of an olefins-containing mixture of hydrocarbons, which process comprises contacting a hydrocarbonaceous feedstock with a zeolitic catalyst at a temperature above 480 C during less than lO
seconds, whereby the catalyst/feedstock weight ratio is in the range from 5 to 150 and the zeolitic catalyst comprises a zeolite with a pore diameter of 0.3 to 0.7 nm and an average crystallite size of less than 2 micrometer.
Preferably, the zeolitic catalyst to be applied in the process according to the present invention comprises a zeolite having an average crystallite size of less than l micrometer. More preferably, the zeolite has an average crystallite size in the range of 0.01 to 0.5 micrometer.
The term crystallite size in this specification is to be regarded as the size of the individual zeolite crystals. These individual crystals may agglomerate into clusters which each may comprise 3 to lO or more individual crystals. Preferably the zeolite comprises separate individual crystals.
The zeolitic catalyst to be used may comprise one or more zeolites with a pore diameter of from 0.3 to 0.7 nm, preferably from 0.5 to 0.7 nm.
The term zeolite in this specification is not to be regarded as comprising only crystalline aluminosilicates. The term also includes crystalline silica (silicalite), silicoaluminophosphates (SAP0), chromosilicates, gallium silicates, iron silicates, aluminium phosphates (ALP0), titanium aluminosilicates (TAS0), boron silicates, titanium aluminophos,phates (TAP0) and iron aluminosilicates.
Suitable examples include crystalline silica (silicalite), silicoaluminophosphates (SAP0), chromosilicates, gallium silicates, iron silicates, aluminium phosphates (ALP0), titanium alumino-silicates (TAS0), boron silicates, titanium aluminophosphates ~TAP0) and iron aluminosilicates. Examples of the zeolite include SAP0-4 and SAP0-11, which are described in US-A-4,440,871, ALP0-ll, described in US-A-4,310,440, TAP0-ll, desribed in US-A-4,500,651, 3 2 ~ 3 TAS0-45 described in US-A-4,254,297, aluminium silicates like erionite, ferrierite, theta and the ZSM-type zeolites such as ZSM-5, ZSM-ll, ZSM-12, ZSM-35, ZSM-23, and ZSM-3~. Preferably the zeolite with a pore diameter of from 0.3 to 0.7 nm is selected from the group consisting of crystalline (metallo)silicates having a ZSM-5 structure, ferrierite, erionite and mixtures thereof.
Preferably, the zeolite with a pore diameter of from 0.3 to 0.7 nm comprises a crystalline (metallo)silicate having a ZSM-5 structure.
Suitable examples of crystalline (metallo)silicates with ZSM-5 structure are aluminium, gallium, iron, scandium, rhodium and/or chromium silicates as described in e.g. GB-B-2,110,559.n After the preparation of the zeolites to be used in the present process usually a significant amount of alkali metal oxide is present in the readily prepared zeolites. Preferably, 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.
Preferably, the zeolite used in the process according to the present invention is substantially in its hydrogen form.
The catalyst suitably further comprises a matrix comprising a refractory oxide that serves as binder material. Suitable refractory oxides include alumina, silica, silica-alumina, magnesia, titania, zirconia and mixtures thereof. The matrix may further comprise natural or synthetic clays. The weight ratio of refractory oxide and zeolite suitably ranges from 10:90 to 99:1, preferably from 50:50 to 90:10. The zeolitic catalyst may comprise up to about 40~ by weight of further zeolites with a pore diameter above 0.7 nm. Suitable examples of such zeolites include the faujasite-type zeolites, zeolite beta, zeolite omega and in particular zeolite X and Y. The zeolitic catalyst comprises a zeolite with a pore diameter of from 0.3 to 0.7 nm. Suitably the zeolitic catalyst comprises ZSM-5 and zeolite Y.
The hydrocarbonaceous feedstock is contacted with the zeolitic catalyst for less than 10 seconds. Suitably, the minimum contact 2~6~33 time is ~.1 second. Very good results are obtained when the hydro-carbonaceous feedstock is contacted with the zeolitic catalyst during 0.2 to 6 seconds.
The process is carried out at a relatively high temperature.
A preferred temparature range is 480 to 900 C, ~ore preferably 500 to 750 C.
The pressure to be used in the process according to the presene invention can be varied within wide ranges. It is, however, preferred that the pressure is such that at prevailing temperature the mixture of hydrocarbons obtained is substantially in its gaseous phase or brought thereto by contact with the catalyst. 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 of the hydrocarbonaceous feedstock such as steam and/or nitrogen.
Olefin production is facilitated by the absence of hydrogen or a hydrogen donor. Hence, the present invention is advantageously carried out in the absence of added hydrogen. It is, of course, possible that during the reaction some small molecules, such as hydrogen molecules are formed. However, this amount is usually negligible and will be less than than 0.5 ~wt of the product.
The process according to the present invention may be carried out in a fixed bed. However, this would imply that extremely high space velocities be required to attain the short contact times envisaged. Therefore, the present invention is preferably 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.
In the process according to the present invention some coke forms on the catalyst. Therefore it is advantageous to regenerate the catalyst. Preferably, the catalyst is regenerated by subjecting 2 ~ 3 it to a treatment with an oxidizing gas, such as air. An continuous regeneration, similar to the regeneration carried out in a fluidized catalytic cracking process, is especially preferred.
The coke formation does not occur at a very high rate. Hence, it would be possible to arrange for a process in which the residence time of the catalyst particles in a reaction zone, e.g. a moving bed, is longer than the residence time of the feedstock in the reaction zone. Of course 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. Suitably the residence time of the catalyst is from l to 20 times the residence time of the feedstock.
The weight ratio of the catalyst used relative to the hydro-carbonaceous feedstock to be converted ~catalyst/oil ratio, g/g) may vary widely,viz. from 5 up to 150 kg catalyst per kg of the hydrocarbonaceous feedstock. Preferably, the weight ratio ofcatalyst relative to the hydrocarbonaceous feedstock is from 10 to 100, more preferably from 20 to 100. Apart from the substantial gain in lower olefins production it has been found that at (relatively) high catalyst/feedstock weight ratios far less coke is produced with small crystallite zeolites than with large crystallite zeolites.
It is especially the combination of high temperature, short contact time, use of the specific small crystallite catalyst and (relatively) high catalyst/feedstock weight ratio which allows an attractive high conversion to olefins and low coke make.
The hydrocarbonaceous feedstock which is to be contacted with the zeolitic catalyst in the process of the present invention can vary within a wide boiling range. Examples of suitable feedstocks are relatively light petroleum fractions such as feedstocks comprising C3 4 hydrocarbons (e.g. LPG), naphtha, gasoline fractions and kerosine fractions. Heavier feedstocks may comprise, for example, vacuum distillates, long residues, deasphalted residual oils and atmospheric distillates, for example gas oils and vacuum gas oils. Another attractive feedstock comprises a mixture 2 ~
of hydrocarbons obtained in a Fischer-Tro~sch hydrocarbon synthesis process.
The invention will now be illustrated by way of the following EXAMPLE
Experiment 1.
The hydrocarbonaceous feedstock in this experiment was a hydrowax having the following properties:
IBP, C 298 20 %wt 388 50 %wt 433 90 ~wt 495 density 70/4 0.8057 kg/l nitrogen 1.0 ppmw The feedstock was contacted in a downflow reactor by passing it downwards co-currently with a flow of catalyst particles. The catalyst comprised ZSM-5 in a silica-alumina matrix (weight ratio ZSN-5/silica-alumina 25:75). The ZSM-5 had an average crystallite size of 0.1 micrometer. The experiment was carried out at a pressure of 2 bar. Further process conditions and the results obtained are given in Table 1 as shown hereinbelow.
Experiment 2 was carried out for the purpose of co~parison in substantially the similar manner as experiment 1, eYrept that now a ZSM-5 was used having a conventional crystallite size ranging from 3 to 7 micrometer. The results obtained are given in Table 1 as shown herein below.
20~3~3 Experiment No. 1 2 Process conditions:
Reactor temperature, 5C 580 580 Catalyst/oil ratio, g/g 87 87 contact time, s 1.2 1.7 Product, ~wt on feed Cl 2.7 2.4 C2 1.4 1.5 c2~ 11.9 13.3 C3 1.4 2.6 C3 36.3 32.3 C4 0.6 0.8 C4 22.8 16.2 C5-220 C 7.1 9.3 221-425 C 9.8 5.6 425 C+ 0.7 8.2 Coke 4.6 7.8 Experiments 3 and 4 were carried out in substantially the same manner as Experiments 1 and 2 respectively. The results obtained are given in Table 2 as shown herein below.
2 ~ 3 Experiment No. 3 4 Process conditions:
Reactor temperature, C 587 583 Catalyst/oil ratio, g/g 29 24 contact time, s 1.05 1.65 Product, ~wt on feed hydrogen 0.7 0.6 Cl 3.4 2.8 C2 1.8 2.8 c2= 10.2 10.3 c3 0.8 6.5 C3 27.7 18.8 C4 3.8 C4= 18.1 11.0 C5-220 C 17.2 19.3 221-425 C 15.5 17.6 425 C+ 2.3 4.5 Coke 2.3 2.0 From the above it will be clear that the results obtained in the experiments according to the present invention are more attractive in terms of lower olefins yields and coke make than those obtained in the comparative experiment.
OLEFINS-CONTAINING MIXTURE OF ~YDROCARBONS
The present invention relates to a process for the preparation of an olefins-containing mixture of hydrocarbons.
There is considerable interest in the production of olefins, especially ethylene and propylene, as their reactivity renders them suitable for conversion to further products, in contrast to the low value lower paraffins.
It is known to convert hydrocarbonaceous feedstocks, such as light distillates, to products rich in lower olefins, especially ethylene and propylene, by high temperature steam cracking. The typical product slate obtained in such steam cracking processes is not entirely suited to the needs of the chemical industry in that it represents a relatively high methane production level and a high ratio of ethylene to propylene.
There have recently been developed alternative processes for the production of lower olefins, for example as described in EP
0347003, EP 0392590 and EP 0385538, from a wide range of hydro-carbonaceous feedstocks. Those processes have been found to give surprisingly high yiels of lower olefins, low amounts of methane and a low ratio of ethylene to propylene and C4 olefins when compared with conventional steam cracking.
Ethylene and propylene are valuable starting materials for chemical processes, while C4 olefins can find use as a starting material for alkylation and/or oligomerizat$on procedures in order to produce high octane gasoline and/or middle distillates.
Isobutene can be usefully converted to methyl t-butyl ether.
Surprisingly, it has now been found that even higher yields of lower olefins and lower ratios of ethylene to propylene can be obtained in comparison with the above-cited processes if use is made of a zeolitic catalyst comprising a zeolite having a specific average crystallite size.
2Q~6~3 Accordingly, the present invention relates to process for the preparation of an olefins-containing mixture of hydrocarbons, which process comprises contacting a hydrocarbonaceous feedstock with a zeolitic catalyst at a temperature above 480 C during less than lO
seconds, whereby the catalyst/feedstock weight ratio is in the range from 5 to 150 and the zeolitic catalyst comprises a zeolite with a pore diameter of 0.3 to 0.7 nm and an average crystallite size of less than 2 micrometer.
Preferably, the zeolitic catalyst to be applied in the process according to the present invention comprises a zeolite having an average crystallite size of less than l micrometer. More preferably, the zeolite has an average crystallite size in the range of 0.01 to 0.5 micrometer.
The term crystallite size in this specification is to be regarded as the size of the individual zeolite crystals. These individual crystals may agglomerate into clusters which each may comprise 3 to lO or more individual crystals. Preferably the zeolite comprises separate individual crystals.
The zeolitic catalyst to be used may comprise one or more zeolites with a pore diameter of from 0.3 to 0.7 nm, preferably from 0.5 to 0.7 nm.
The term zeolite in this specification is not to be regarded as comprising only crystalline aluminosilicates. The term also includes crystalline silica (silicalite), silicoaluminophosphates (SAP0), chromosilicates, gallium silicates, iron silicates, aluminium phosphates (ALP0), titanium aluminosilicates (TAS0), boron silicates, titanium aluminophos,phates (TAP0) and iron aluminosilicates.
Suitable examples include crystalline silica (silicalite), silicoaluminophosphates (SAP0), chromosilicates, gallium silicates, iron silicates, aluminium phosphates (ALP0), titanium alumino-silicates (TAS0), boron silicates, titanium aluminophosphates ~TAP0) and iron aluminosilicates. Examples of the zeolite include SAP0-4 and SAP0-11, which are described in US-A-4,440,871, ALP0-ll, described in US-A-4,310,440, TAP0-ll, desribed in US-A-4,500,651, 3 2 ~ 3 TAS0-45 described in US-A-4,254,297, aluminium silicates like erionite, ferrierite, theta and the ZSM-type zeolites such as ZSM-5, ZSM-ll, ZSM-12, ZSM-35, ZSM-23, and ZSM-3~. Preferably the zeolite with a pore diameter of from 0.3 to 0.7 nm is selected from the group consisting of crystalline (metallo)silicates having a ZSM-5 structure, ferrierite, erionite and mixtures thereof.
Preferably, the zeolite with a pore diameter of from 0.3 to 0.7 nm comprises a crystalline (metallo)silicate having a ZSM-5 structure.
Suitable examples of crystalline (metallo)silicates with ZSM-5 structure are aluminium, gallium, iron, scandium, rhodium and/or chromium silicates as described in e.g. GB-B-2,110,559.n After the preparation of the zeolites to be used in the present process usually a significant amount of alkali metal oxide is present in the readily prepared zeolites. Preferably, 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.
Preferably, the zeolite used in the process according to the present invention is substantially in its hydrogen form.
The catalyst suitably further comprises a matrix comprising a refractory oxide that serves as binder material. Suitable refractory oxides include alumina, silica, silica-alumina, magnesia, titania, zirconia and mixtures thereof. The matrix may further comprise natural or synthetic clays. The weight ratio of refractory oxide and zeolite suitably ranges from 10:90 to 99:1, preferably from 50:50 to 90:10. The zeolitic catalyst may comprise up to about 40~ by weight of further zeolites with a pore diameter above 0.7 nm. Suitable examples of such zeolites include the faujasite-type zeolites, zeolite beta, zeolite omega and in particular zeolite X and Y. The zeolitic catalyst comprises a zeolite with a pore diameter of from 0.3 to 0.7 nm. Suitably the zeolitic catalyst comprises ZSM-5 and zeolite Y.
The hydrocarbonaceous feedstock is contacted with the zeolitic catalyst for less than 10 seconds. Suitably, the minimum contact 2~6~33 time is ~.1 second. Very good results are obtained when the hydro-carbonaceous feedstock is contacted with the zeolitic catalyst during 0.2 to 6 seconds.
The process is carried out at a relatively high temperature.
A preferred temparature range is 480 to 900 C, ~ore preferably 500 to 750 C.
The pressure to be used in the process according to the presene invention can be varied within wide ranges. It is, however, preferred that the pressure is such that at prevailing temperature the mixture of hydrocarbons obtained is substantially in its gaseous phase or brought thereto by contact with the catalyst. 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 of the hydrocarbonaceous feedstock such as steam and/or nitrogen.
Olefin production is facilitated by the absence of hydrogen or a hydrogen donor. Hence, the present invention is advantageously carried out in the absence of added hydrogen. It is, of course, possible that during the reaction some small molecules, such as hydrogen molecules are formed. However, this amount is usually negligible and will be less than than 0.5 ~wt of the product.
The process according to the present invention may be carried out in a fixed bed. However, this would imply that extremely high space velocities be required to attain the short contact times envisaged. Therefore, the present invention is preferably 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.
In the process according to the present invention some coke forms on the catalyst. Therefore it is advantageous to regenerate the catalyst. Preferably, the catalyst is regenerated by subjecting 2 ~ 3 it to a treatment with an oxidizing gas, such as air. An continuous regeneration, similar to the regeneration carried out in a fluidized catalytic cracking process, is especially preferred.
The coke formation does not occur at a very high rate. Hence, it would be possible to arrange for a process in which the residence time of the catalyst particles in a reaction zone, e.g. a moving bed, is longer than the residence time of the feedstock in the reaction zone. Of course 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. Suitably the residence time of the catalyst is from l to 20 times the residence time of the feedstock.
The weight ratio of the catalyst used relative to the hydro-carbonaceous feedstock to be converted ~catalyst/oil ratio, g/g) may vary widely,viz. from 5 up to 150 kg catalyst per kg of the hydrocarbonaceous feedstock. Preferably, the weight ratio ofcatalyst relative to the hydrocarbonaceous feedstock is from 10 to 100, more preferably from 20 to 100. Apart from the substantial gain in lower olefins production it has been found that at (relatively) high catalyst/feedstock weight ratios far less coke is produced with small crystallite zeolites than with large crystallite zeolites.
It is especially the combination of high temperature, short contact time, use of the specific small crystallite catalyst and (relatively) high catalyst/feedstock weight ratio which allows an attractive high conversion to olefins and low coke make.
The hydrocarbonaceous feedstock which is to be contacted with the zeolitic catalyst in the process of the present invention can vary within a wide boiling range. Examples of suitable feedstocks are relatively light petroleum fractions such as feedstocks comprising C3 4 hydrocarbons (e.g. LPG), naphtha, gasoline fractions and kerosine fractions. Heavier feedstocks may comprise, for example, vacuum distillates, long residues, deasphalted residual oils and atmospheric distillates, for example gas oils and vacuum gas oils. Another attractive feedstock comprises a mixture 2 ~
of hydrocarbons obtained in a Fischer-Tro~sch hydrocarbon synthesis process.
The invention will now be illustrated by way of the following EXAMPLE
Experiment 1.
The hydrocarbonaceous feedstock in this experiment was a hydrowax having the following properties:
IBP, C 298 20 %wt 388 50 %wt 433 90 ~wt 495 density 70/4 0.8057 kg/l nitrogen 1.0 ppmw The feedstock was contacted in a downflow reactor by passing it downwards co-currently with a flow of catalyst particles. The catalyst comprised ZSM-5 in a silica-alumina matrix (weight ratio ZSN-5/silica-alumina 25:75). The ZSM-5 had an average crystallite size of 0.1 micrometer. The experiment was carried out at a pressure of 2 bar. Further process conditions and the results obtained are given in Table 1 as shown hereinbelow.
Experiment 2 was carried out for the purpose of co~parison in substantially the similar manner as experiment 1, eYrept that now a ZSM-5 was used having a conventional crystallite size ranging from 3 to 7 micrometer. The results obtained are given in Table 1 as shown herein below.
20~3~3 Experiment No. 1 2 Process conditions:
Reactor temperature, 5C 580 580 Catalyst/oil ratio, g/g 87 87 contact time, s 1.2 1.7 Product, ~wt on feed Cl 2.7 2.4 C2 1.4 1.5 c2~ 11.9 13.3 C3 1.4 2.6 C3 36.3 32.3 C4 0.6 0.8 C4 22.8 16.2 C5-220 C 7.1 9.3 221-425 C 9.8 5.6 425 C+ 0.7 8.2 Coke 4.6 7.8 Experiments 3 and 4 were carried out in substantially the same manner as Experiments 1 and 2 respectively. The results obtained are given in Table 2 as shown herein below.
2 ~ 3 Experiment No. 3 4 Process conditions:
Reactor temperature, C 587 583 Catalyst/oil ratio, g/g 29 24 contact time, s 1.05 1.65 Product, ~wt on feed hydrogen 0.7 0.6 Cl 3.4 2.8 C2 1.8 2.8 c2= 10.2 10.3 c3 0.8 6.5 C3 27.7 18.8 C4 3.8 C4= 18.1 11.0 C5-220 C 17.2 19.3 221-425 C 15.5 17.6 425 C+ 2.3 4.5 Coke 2.3 2.0 From the above it will be clear that the results obtained in the experiments according to the present invention are more attractive in terms of lower olefins yields and coke make than those obtained in the comparative experiment.
Claims (13)
1. Process for the preparation of an olefins-containing mixture of hydrocarbons, which process comprises contacting a hydro-carbonaceous feedstock with a zeolitic catalyst at a temperature above 480 °C during less than 10 seconds, whereby the catalyst/-feedstock weight ratio is in the range from 5 to 150 and the zeolitic catalyst comprises a zeolite with a pore diameter of 0.3 to 0.7 nm and an average crystallite size of less than 2 micro-meter.
2. Process according to claim 1, wherein the zeolite has an average crystallite size of less than 1 micrometer.
3. Process according to claim 2, wherein the zeolite has an average crystallite size in the range of 0.01 to 0.5 micrometer.
4. Process according to any one of claims 1-3, wherein the zeolite has a pore diameter of 0.5 to 0.7 nm.
5. Process according to any one of claims 1-4, wherein the zeolite is selected from crystalline (metallo)silicates having a ZSM-5 structure, ferrierite, erionite and mixtures thereof.
6. Process according to any one of claims 1-5, wherein the zeolite is substantially in its hydrogen form.
7. Process according to any one of claims 1-6, wherein the feedstock is contacted with the zeolitic catalyst during 0.2 to 6 seconds.
8. Process according to any one of claims 1-7, wherein the temperature is from 480 to 900 °C.
9. Process according to claim 8, wherein the temperature is from 500 to 750 °C.
10. Process according to any one of claims 1-9, wherein the pressure is from 1 to 10 bar.
11. Process according to any one of claims 1-10, wherein the catalyst/feedstock weight ratio is from 10 to 100.
12. Process according to any one of claims 1-11, which is carried out in a moving bed of catalyst.
13. A hydrocarbonaceous product, or a fraction thereof, when obtained by the process of any one of claims 1-12.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB909026775A GB9026775D0 (en) | 1990-12-10 | 1990-12-10 | Process for the preparation of an olefins-containing mixture of hydrocarbons |
| GB9026775.8 | 1990-12-10 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2056833A1 true CA2056833A1 (en) | 1992-06-11 |
Family
ID=10686747
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002056833A Abandoned CA2056833A1 (en) | 1990-12-10 | 1991-12-03 | Process for the preparation of an olefins-containing mixture of hydrocarbons |
Country Status (9)
| Country | Link |
|---|---|
| EP (1) | EP0490435B1 (en) |
| JP (1) | JPH04352731A (en) |
| KR (1) | KR920012398A (en) |
| CN (1) | CN1033317C (en) |
| AU (1) | AU645153B2 (en) |
| CA (1) | CA2056833A1 (en) |
| DE (1) | DE69103614T2 (en) |
| ES (1) | ES2059044T3 (en) |
| GB (1) | GB9026775D0 (en) |
Families Citing this family (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5628978A (en) * | 1994-12-23 | 1997-05-13 | Intevep, S.A. | MTW zeolite for cracking feedstock into olefins and isoparaffins |
| US5888378A (en) * | 1997-03-18 | 1999-03-30 | Mobile Oil Corporation | Catalytic cracking process |
| IT1290433B1 (en) * | 1997-03-24 | 1998-12-03 | Euron Spa | FLUID BED CATALYTIC CRACKING PROCESS CHARACTERIZED BY HIGH SELECTIVITY TO OLEFIN |
| 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 |
| ES2316514T3 (en) * | 2002-12-01 | 2009-04-16 | Sud-Chemie Ag | USE OF A CRYSTAL ALUMINOSILICATE BASED CATALYST. |
| KR20070056090A (en) | 2004-08-10 | 2007-05-31 | 쉘 인터내셔날 리써취 마트샤피지 비.브이. | Method and apparatus for making a middle distillate product and lower olefins from a hydrocarbon feedstock |
| US7582203B2 (en) | 2004-08-10 | 2009-09-01 | Shell Oil Company | Hydrocarbon cracking process for converting gas oil preferentially to middle distillate and lower olefins |
| FR2875234B1 (en) * | 2004-09-15 | 2006-11-03 | Inst Francais Du Petrole | PROCESS FOR PRODUCING PROPYLENE OPERATING IN A MOVING BED WITH RECYCLING OF A CATALYST FRACTION USING THE SAME |
| KR20100016499A (en) | 2007-04-13 | 2010-02-12 | 쉘 인터내셔날 리써취 마트샤피지 비.브이. | Systems and methods for making a middle distillate product and lower olefins from a hydrocarbon feedstock |
| KR100904297B1 (en) * | 2007-10-26 | 2009-06-25 | 한국화학연구원 | Process for Producing Light Olefins from Synthesis Gas Using Sequence Dual-bed Reactor |
| JP2012045505A (en) * | 2010-08-27 | 2012-03-08 | Idemitsu Kosan Co Ltd | Catalyst for producing light olefin, method for producing the catalyst, and method for producing light olefin by using the catalyst |
| CN108431180B (en) | 2015-12-21 | 2021-09-03 | 沙特基础工业全球技术公司 | Method and system for producing olefins and aromatics from coker naphtha |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3926782A (en) * | 1973-02-09 | 1975-12-16 | Mobil Oil Corp | Hydrocarbon conversion |
| GB8904408D0 (en) * | 1989-02-27 | 1989-04-12 | Shell Int Research | Process for the conversion of a hydrocarbonaceous feedstock |
-
1990
- 1990-12-10 GB GB909026775A patent/GB9026775D0/en active Pending
-
1991
- 1991-12-03 CA CA002056833A patent/CA2056833A1/en not_active Abandoned
- 1991-12-04 ES ES91203184T patent/ES2059044T3/en not_active Expired - Lifetime
- 1991-12-04 DE DE69103614T patent/DE69103614T2/en not_active Revoked
- 1991-12-04 EP EP91203184A patent/EP0490435B1/en not_active Revoked
- 1991-12-09 AU AU88959/91A patent/AU645153B2/en not_active Ceased
- 1991-12-09 KR KR1019910022639A patent/KR920012398A/en not_active Application Discontinuation
- 1991-12-10 JP JP3349815A patent/JPH04352731A/en active Pending
- 1991-12-10 CN CN91111560A patent/CN1033317C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| GB9026775D0 (en) | 1991-01-30 |
| CN1033317C (en) | 1996-11-20 |
| CN1062339A (en) | 1992-07-01 |
| KR920012398A (en) | 1992-07-27 |
| DE69103614T2 (en) | 1995-03-02 |
| AU8895991A (en) | 1992-06-11 |
| ES2059044T3 (en) | 1994-11-01 |
| DE69103614D1 (en) | 1994-09-29 |
| JPH04352731A (en) | 1992-12-07 |
| EP0490435A1 (en) | 1992-06-17 |
| AU645153B2 (en) | 1994-01-06 |
| EP0490435B1 (en) | 1994-08-24 |
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