ZA200900892B - Fcc catalyst for light olefin production - Google Patents
Fcc catalyst for light olefin production Download PDFInfo
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- ZA200900892B ZA200900892B ZA2009/00892A ZA200900892A ZA200900892B ZA 200900892 B ZA200900892 B ZA 200900892B ZA 2009/00892 A ZA2009/00892 A ZA 2009/00892A ZA 200900892 A ZA200900892 A ZA 200900892A ZA 200900892 B ZA200900892 B ZA 200900892B
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- catalyst
- blend
- molecular sieve
- weight
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- Prior art date
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- 239000003054 catalyst Substances 0.000 title claims description 103
- 238000004519 manufacturing process Methods 0.000 title claims description 18
- 150000001336 alkenes Chemical class 0.000 title description 7
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title description 3
- 239000000203 mixture Substances 0.000 claims description 41
- 229910052751 metal Inorganic materials 0.000 claims description 36
- 239000002184 metal Substances 0.000 claims description 36
- 239000002808 molecular sieve Substances 0.000 claims description 24
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 24
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 22
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 22
- 150000002739 metals Chemical class 0.000 claims description 17
- 239000011148 porous material Substances 0.000 claims description 17
- 239000010457 zeolite Substances 0.000 claims description 13
- 229910021536 Zeolite Inorganic materials 0.000 claims description 10
- GYHNNYVSQQEPJS-UHFFFAOYSA-N Gallium Chemical compound [Ga] GYHNNYVSQQEPJS-UHFFFAOYSA-N 0.000 claims description 9
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims description 9
- 229910052733 gallium Inorganic materials 0.000 claims description 9
- 229910052725 zinc Inorganic materials 0.000 claims description 9
- 239000011701 zinc Substances 0.000 claims description 9
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 8
- 229910052802 copper Inorganic materials 0.000 claims description 8
- 239000010949 copper Substances 0.000 claims description 8
- 238000004523 catalytic cracking Methods 0.000 claims description 7
- 229910052793 cadmium Inorganic materials 0.000 claims description 4
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 claims description 4
- 229910052738 indium Inorganic materials 0.000 claims description 4
- APFVFJFRJDLVQX-UHFFFAOYSA-N indium atom Chemical compound [In] APFVFJFRJDLVQX-UHFFFAOYSA-N 0.000 claims description 4
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 claims description 3
- 229910052732 germanium Inorganic materials 0.000 claims description 3
- GNPVGFCGXDBREM-UHFFFAOYSA-N germanium atom Chemical compound [Ge] GNPVGFCGXDBREM-UHFFFAOYSA-N 0.000 claims description 3
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 claims description 3
- 229910052753 mercury Inorganic materials 0.000 claims description 3
- 229910052716 thallium Inorganic materials 0.000 claims description 3
- BKVIYDNLLOSFOA-UHFFFAOYSA-N thallium Chemical compound [Tl] BKVIYDNLLOSFOA-UHFFFAOYSA-N 0.000 claims description 3
- 229910052718 tin Inorganic materials 0.000 claims description 3
- 229910052675 erionite Inorganic materials 0.000 claims description 2
- 229910052727 yttrium Inorganic materials 0.000 claims description 2
- 229930195733 hydrocarbon Natural products 0.000 description 23
- 150000002430 hydrocarbons Chemical class 0.000 description 23
- 238000000034 method Methods 0.000 description 23
- 239000004215 Carbon black (E152) Substances 0.000 description 22
- 238000004231 fluid catalytic cracking Methods 0.000 description 11
- 239000007789 gas Substances 0.000 description 11
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 8
- 239000000654 additive Substances 0.000 description 7
- 239000011230 binding agent Substances 0.000 description 7
- 239000000945 filler Substances 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 5
- 230000000996 additive effect Effects 0.000 description 4
- 238000005336 cracking Methods 0.000 description 4
- 230000001965 increasing effect Effects 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000009835 boiling Methods 0.000 description 3
- 238000000151 deposition Methods 0.000 description 3
- 239000003085 diluting agent Substances 0.000 description 3
- 230000002708 enhancing effect Effects 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 239000004033 plastic Substances 0.000 description 3
- 229920003023 plastic Polymers 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- -1 polyethylene Polymers 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical compound ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 238000010348 incorporation Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 229910052809 inorganic oxide Inorganic materials 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000011368 organic material Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000006069 physical mixture Substances 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Catalysts (AREA)
Description
" - ".2009/004g, oo | Il FIELD OF THE INVENTION
[0001] The present invention relates to a process for the production of light olefins from a hydrocarbon feed stream. This invention also relates to an improved catalyst used in the
Fluid Catalytic Cracking process for producing propylene.
[0002] Catalytic cracking is the process of breaking larger hydrocarbon molecules into smaller hydrocarbon molecules through contacting the larger hydrocarbon molecules witha catalyst at reaction conditions. The catalytic cracking process is one method used to produce ethylene and propylene from hydrocarbon feedstocks. The ethylene and propylene are important chemicals for the production of the respective plastics polyethylene and polypropylene, two important plastics having a wide variety of uses, such as a material for fabrication of products and as a material for packaging. Other uses of these chemicals include the production of vinyl chloride, ethylene oxide, ethylbenzene and alcohols. Hydrocarbons used as feedstock for light olefin production include natural gas, petroleum liquids, and carbonaceous materials including coal, recycled plastics or any organic material.
[0003] Currently, the majority of propylene production is from steam cracking, However, the demand for propylene is growing faster than the ability of steam crackers production to increase propylene. Fluid catalytic cracking (FCC) provides an alternative method of meeting the demand for the production of propylene. :
[0604] One process for enhancing propylene yield is disclosed in US 4,980,053, where a deep catalytic cracking process is disclosed. The process requires 5-10 seconds of contact ~ time, and uses a mixture of Y-type zeolite and a pentasil, shape-selective zeolite. However, - the process reports relatively high yields of dry gas. :
[0005] Other patents disclose short catalyst contact times, but do not recognize significant light olefin yields, such as in US 5,965,012 which discloses an FCC process, but a better example showing the importance of short contact times is found in US 6,538,169 showing short contact times during the cracking process in the riser reactor. Another FCC process is . _ i _ Bh :
disclosed in US 6,010,618 where there is a very short catalyst and feed contact time in the riser, and the cracked product is quickly removed below the outlet of the riser. Other patents, such as US 5,296,131 disclose very short FCC catalyst contact times, but these processes are operated to improve gasoline production rather than production of light olefins.
[0006] Other patents, US 4,787,967, US 4,871,446, and US 4,990,314, disclose the use of two component catalysts used in FCC processes. The two component catalyst systems use a large-pore catalyst for cracking large hydrocarbon molecules and a small-pore catalyst for cracking smaller hydrocarbon molecules.
[0007] To enhance propylene yields, shape selective additives are used in conjunction with conventional FCC catalysts containing Y-zeolites. The additives all have essentially the same selectivity characteristics. The problem with current catalysts is that selectivity is limited, and the amount of propylene produced is only a function of the amount of additive used in the catalyst mixture.
[0008] While much research has gone into trying new catalysts for enhancing propylene
I5 production, understanding the proper paradigm for selectivity as a function of shape selective catalyst content and additive can increase the propylene yield while operating at a lower temperature, and with a reduced dry gas production and reduced coking. An increased yield can increase the profitability of propylene production, and a small improvement in the catalyst can result in a large improvement in the yields of propylene from hydrocarbon feedstocks.
[0009] The invention provides a new catalyst blend for increasing propylene yields during a catalytic cracking process. The catalyst blend comprises a first catalyst having a large pore zeolite or molecular sieve blended with a second catalyst molecular sieve having a medium or. smaller pore size where the second catalyst has a metal deposited on the catalyst in an amount between 0.1% and 5% by weight. The catalyst blend comprises the first catalyst in an amount between 20% and 90% by weight, and the second catalyst in an amount between 10% and 80% by weight. The metal is at least one metal selected from the group consisting of gallium,
~ copper, zinc, germanium, cadmium, indium, tin, mercury, thallium and lead, where the total amount of the metal is between 0.1% and 5% by weight.
[0010] In another embodiment, the invention comprises contacting a hydrocarbon stream with the above catalyst blend.
[0011] Other objects, advantages and applications of the present invention will become apparent to those skilled in the art from the following detailed description.
[0012] It has been found that using a small but proper amount of metal and the proper choice of metal or metals on a shape selective small or medium pore size molecular sieve significantly improves the yield of propylene during the catalytic cracking process when blended with a large pore molecular sieve catalyst. oo
[0013] The present invention provides for a catalyst blend, for use in the catalytic cracking process. The catalyst blend comprises a first catalyst compris ing a large pore molecular sieve in an amount between 20% and 90% by weight, and a second catalyst comprising a medium or small pore size molecular sieve in an amount between 10% and 80% by weight, and where the second catalyst has a metal deposited on the catalyst in an amount from 0.1% to 5% by weight of the second catalyst.
[0014] Each of the catalysts comprise a molecular sieve with an inorganic oxide binder, a filler, or both to provide the desired level of mechanical strength and attrition resistance of the bound catalyst. The amount of binder and/or filler material contributes from 20% to 80% of the total catalyst weight. In addition to enhancing the catalyst strength properties, the binder and/or filler materials allow the molecular sieve to be bound into larger particle sizes suitable for commercial catalytic purposes. Binders and fillers are known in the art and not enumerated here. Examples of binders and fillers are described in US 6,649,802 which is incorporated by reference in its entirety. The term catalyst as used in this application refers to the molecular sieve with the binder and/or filler in a state useable for commercial catalytic purposes. The catalyst blend, when used herein, refers to a mixture of the first and second catalysts, and can be a physical mixture, or a blend that combines both catalysts into a single catalyst particle.
[0015] The metal, or metals, deposited on the second catalyst are deposited after the : catalyst is formed with the binder and/or filler, and can be dispersed within the molecular sieve, or deposited on the external surface of the catalyst particles, or some combination.
[0016] The catalyst is a shape selective zeolite or molecular sieve for use in cracking larger hydrocarbon molecules to propylene. Large pore molecular sieves are molecular sieves with pore opening diameters greater than 0.7 nm, and are typically defined by 12 membered or larger rings. A typical first catalyst 1s a Y-zeolite. Large pore Y-zeolites are known in the art and include H-Y, RE-Y, US-Y, NH4-Y, and LZ-210, which are described in
US 4,842,836, US 4,965,233, US 6,616,899, and US 6,869,521 and which are incorporated by reference in their entirety. Molecular sieves with medium and small pore sizes are characterized as having effective pore opening diameters of less than or equal to 0.7 nm, and with the pore ring sizes having 10 or fewer members. One such molecular sieve has an MFI type structure, and preferably is ZSM-5 or ST-5 molecular sieve. Other zeolites useable for the second catalyst in the present invention include, but are not limited to, ZSM-11, ZSM-22,
IS Beta, erionite, ZSM-34 and SAPO-11. In one embodiment, the metal is selected from gallium, copper, zinc and mixtures thereof, where the total metal content is between 0.1% and 5% by weight of the second catalyst, and preferably between 0.5% and 2% by weight of the second catalyst.
[0017] The preferred second catalyst is a zeolite and has an MFI type structure and the preparation is known in the art as exemplified by US 5,254,327 and is incorporated by reference in its entirety. However, the metal was deposited on the catalyst by the standard “incipient wetness” technique. The metals in the form of soluble metal salts, were dissolved in sufficient water to fill the pore volume of the catalyst. The metal solution was then added, dropwise, to the catalyst powder while stirring the catalyst in water. After depositing the metal in solution, the catalyst is dried at 93°C (200°F) and calcined at 540°C (1000°F). Other methods of depositing the metals on the catalyst include ion exchange methods, or even incorporation of the metals during the zeolite synthesis step.
[0018] In another embodiment, the second catalyst comprises a shape selective zeolite or molecular sieve having at least two metals deposited on the catalyst, where the total amount of the metals deposited is from 0.1% to 5% by weight. The metals deposited are selected from gallium, copper, zinc, germanium, cadmium, indium, tin, mercury, thallium, lead and mixtures thereof. Preferably, the metals are selected from gallium, copper and zinc, and the metals are each deposited in an amount between 0.1% and 2% by weight. For this embodiment, when selecting two metals and depositing the metals on the catalyst, it is preferred that the metals are deposited in substantially equal amounts by weight. | :
[0019] The process of the present invention is described in the context of an FCC process.
An FCC arrangement consists of a riser reactor that provides a pneumatic conveyance zone in which the reaction takes place, a separation unit in which the product gas leaving the riser reactor is separated from the catalyst blend, a regenerator that receives the catalyst blend and regenerates it (via coke combustion with air or suitable oxygen mixture) for reuse, and a blending vessel that mixes the catalyst blend with a fluidizing gas prior to feeding the catalyst : ~ blend and a hydrocarbon feedstream into the riser reactor. FCC technology is known, as shown in US 6,538,169, and is incorporated by reference in its entirety.
[0020] The catalyst blend, as described above, is mixed with a fluidizing gas, and fed with a hydrocarbon feedstream into the riser reactor, where the catalyst blend and 1S hydrocarbon gas react under reaction conditions to generate a'product gas that includes propylene. :
[0021] Hydrocarbon feedstocks suitable for processing in this invention include, but are not limited to, naphthas having a boiling range above 50°C (122°F), vacuum gas oil having a boiling range from 343°C to 552°C (650°F to 1025°F) and is prepared by vacuum fractionation of atmospheric residue, and heavy or residual feeds having boiling ranges above 499°C (930°F).
[0022] The riser typically operates with dilute phase conditions above the point of feed injection wherein the density is usually less than 320 kg/m’ (20 Ib/ft®) and, more typically, less than 160 kg/m (10 1b/ft>). The feedstream will ordinarily have been heated to a temperature in a range of from 150°C to 320°C (300°F to 600°F.), before contacting the catalyst. Additional amounts of feed may be added downstream of the initial feed point.
[0023] In an effort to minimize the contact time of the feed and the catalyst blend which may promote further conversion of desired products to undesirable other products, the catalyst blend is rapidly separated from the product gas. Contact times in the riser reactor are from
0.8 seconds to 3.5 seconds. A variety of separation means are known in the art and are not detailed here.
[0024] The catalyst blend to hydrocarbon feed ratio by weight is in the range from 5 to 50 and preferably from 5 to 30, and more preferably from 5 to 15.
[0025] Low hydrocarbon partial pressure operates to favor the production of light olefins.
Accordingly, the riser pressure is set at 140 to 420 kPa (20 to 60 psia) with a hydrocarbon partial pressure of 35 to 310 kPa (5 to 45 psia), with a preferred hydrocarbon partial pressure of 70 to 140 kPa (10 to 20 psia). This relatively low partial pressure for hydrocarbon is achieved by using steam as a diluent to the extent that the diluent is 2-40 wt-% of feed and preferably 10-20 wt-% of feed. Other diluents such as dry gas can be used to reach equivalent hydrocarbon partial pressures.
[0026] The temperature of the cracked stream at the riser outlet will be 510°C to 621°C (950°F to 1150°F). However, we have found that riser outlet temperatures above 566°C (1050°F) make more dry gas and little more olefins so the preferred temperature is from 510°C to 566°C (950°F to 1050°F). :
[0027] Testing was performed in an ACE testing microreactor unit. ACE units are available from Xytel Corp. in Elk Grove Village, IL. The hydrocarbon feedstream was a light naphtha and the reaction conditions included a temperature of 565°C (1050°F) and a catalyst to hydrocarbon ratio of 5 over the catalyst. :
[0028] The test results from the ACE unit are summarized in Table 1. The comparisons are with a commercial catalyst having a ST-5 molecular sieve in an amount of approximately 25% by weight and the molecular sieve with different amounts of activated ST-5s with metals deposited on the catalyst. ST-5 is an MFI type zeolite and is disclosed in US 5,254,327 which is incorporated by reference in its entirety.
Table 1
Selectivities | ST-5 1% Gaon |1%Znon |Zn-Cuon |1%Nion
BA rE
CL CE EL SC ELI
CE CEC Co
EC CC EE cn
EEC CN KEG Lr Kr a A
[0029] The results show that a small amount of additive to the ST-5 catalyst generated an increased amount of propylene produced from a naphtha feedstock, over the commercial ST-5 catalyst. Metals that showed an increase were gallium with a 21.7% increase, zinc with a 6.7% increase, and a 50-50 mixture of zinc and copper showed a 15% increase. On the other - hand, improper choice of additive can result in degradation of propylene production. Other possible combinations from the present results indicate a mixture of gallium and copper, and : a mixture of gallium and zinc.
[0030] By limiting the amounts of additives, and by selecting the proper metals to add to the catalysts, propylene production can be substantially increased.
[0031] While the invention has been described with what are presently considered the preferred embodiments, it is to be understood that the invention is not limited to the disclosed embodiments, but it is intended to cover various modifications and equivalent arrangements included within the scope of the appended claims. : .
Claims (10)
1. A catalyst blend for fluidized catalytic cracking to increase propylene production, comprising: : a first catalyst comprising a large pore molecular sieve in an amount from 20% to 90% of the catalyst in the catalyst blend by weight; a second catalyst comprising a medium or small pore molecular sieve in an amount from 10% to 80% of the catalyst blend by weight; wherein the second catalyst comprises a metal deposited on the second catalyst in an amount from 0.1% to 5% by weight of the second catalyst.
2. The catalyst blend of claim 1 wherein the metal is selected from the group consisting . of gallium, copper, zinc, indium, cadmium and mixtures thereof.
3. The catalyst blend of claim 1 wherein the metal is present in an amount from 0.5% to 2% of the catalyst by weight.
4, The catalyst blend of claim 1 wherein the metal comprises at least two metals selected from the group consisting of gallium, copper, zinc, germanium, cadmium, indium, tin, mercury, thallium and lead. Co
5. The catalyst blend of claim 4 wherein each metal comprises an amount between 0.1% and 2% of the second catalyst by weight. :
6. The catalyst blend of claim 1 wherein the second catalyst molecular sieve has an MFI . type structure.
7. The catalyst blend of claim 6 wherein the second catalyst molecular sieve is ZSM-5 or ST-5.
8. The catalyst blend of claim 1 wherein the second catalyst molecular sieve is selected from the group consisting of ZSM-5, ZSM-11, ZSM-22, beta, erionite, ZSM-34, SAPO-11, ST-5, and mixtures thereof. CL
9. The catalyst blend of claim 1 wherein the first catalyst is a Y-zeolite.
10. The catalyst blend of claim 9 wherein the first catalyst is selected from the group consisting of H-Y, NH4-Y, RE-Y, US-Y, LZ-210, and mixtures thereof. :
DATED THIS 6™ DAY OF FEBRUARY 2009 SPOOR & FISHER APPLICANT’S PATENT ATTORNEYS
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| ZA2009/00892A ZA200900892B (en) | 2009-02-06 | 2009-02-06 | Fcc catalyst for light olefin production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| ZA2009/00892A ZA200900892B (en) | 2009-02-06 | 2009-02-06 | Fcc catalyst for light olefin production |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| ZA200900892B true ZA200900892B (en) | 2010-02-24 |
Family
ID=58161213
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| ZA2009/00892A ZA200900892B (en) | 2009-02-06 | 2009-02-06 | Fcc catalyst for light olefin production |
Country Status (1)
| Country | Link |
|---|---|
| ZA (1) | ZA200900892B (en) |
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2009
- 2009-02-06 ZA ZA2009/00892A patent/ZA200900892B/en unknown
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