JPWO2022005544A5 - - Google Patents
Download PDFInfo
- Publication number
- JPWO2022005544A5 JPWO2022005544A5 JP2022580412A JP2022580412A JPWO2022005544A5 JP WO2022005544 A5 JPWO2022005544 A5 JP WO2022005544A5 JP 2022580412 A JP2022580412 A JP 2022580412A JP 2022580412 A JP2022580412 A JP 2022580412A JP WO2022005544 A5 JPWO2022005544 A5 JP WO2022005544A5
- Authority
- JP
- Japan
- Prior art keywords
- catalyst composition
- fcc catalyst
- zeolite
- fcc
- hydrocarbon feed
- 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.)
- Pending
Links
Description
実施の形態において、炭化水素供給物２１１を、この供給物の噴霧化のために蒸気または他の適切なガス（図示せず）と共に反応装置系２００のダウナー部分を通じて反応ゾーン２１２に導入することができる。再生ゾーン２２２からの有効量の加熱された新たなまたは再生されたＦＣＣ触媒組成物の粒子を反応ゾーン２１２の最上部に搬送することができる。再生ゾーン２２２からの加熱された新たなまたは再生されたＦＣＣ触媒組成物の粒子は、移送ラインまたは直立管と一般に称される、下方に向けられた導管２２３を通じて、反応ゾーン２１２の最上部にある取り出し(withdrawal)またはホッパー（図示せず）に搬送することができる。高温のＦＣＣ触媒組成物の粒子の流れは、典型的に、反応ゾーン２１２の混合ゾーンまたは供給物噴射部分に均一に向けるために、安定させることができる。炭化水素供給物２１１は、典型的に、再生されたＦＣＣ触媒組成物の粒子を反応ゾーン２１２に導入する地点に近接して位置する供給物噴射ノズルを通じて、混合ゾーンに噴射することができる。これらの多数の噴射ノズルにより、ＦＣＣ触媒組成物の粒子と炭化水素供給物２１１を完全かつ均一に混合することができる。炭化水素供給物２１１が高温のＦＣＣ触媒組成物の粒子と一旦接触したら、触媒反応が開始することができる。
In embodiments, hydrocarbon feed 211 may be introduced into reaction zone 212 through a downer portion of reactor system 200 along with steam or other suitable gas (not shown) for atomization of the feed. can. An effective amount of heated fresh or regenerated FCC catalyst composition particles from regeneration zone 222 may be conveyed to the top of reaction zone 212. Particles of heated fresh or regenerated FCC catalyst composition from the regeneration zone 222 are passed to the top of the reaction zone 212 through a downwardly directed conduit 223 , commonly referred to as a transfer line or standpipe. It can be withdrawn or conveyed to a hopper (not shown). The flow of hot FCC catalyst composition particles typically can be stabilized to uniformly direct it to the mixing zone or feed injection portion of reaction zone 212. Hydrocarbon feed 211 may be injected into the mixing zone typically through a feed injection nozzle located proximate to the point where particles of regenerated FCC catalyst composition are introduced into reaction zone 212. These multiple injection nozzles allow thorough and uniform mixing of the FCC catalyst composition particles and hydrocarbon feed 211. Once the hydrocarbon feed 211 contacts the hot FCC catalyst composition particles, the catalytic reaction can begin.
本記載および例は、炭化水素供給物としての全原油または脱塩原油の観点で与えられているが、本開示に記載されたシステムおよびプロセスは、以下に限られないが、原油、減圧残油、タールサンド、ビチューメン、常圧残油、真空軽油、または他の重油を含む多種多様の重油の変換に適用できるであろうことを理解すべきである。
Although this description and examples are given in terms of whole crude oil or desalted crude oil as the hydrocarbon feed , the systems and processes described in this disclosure may include, but are not limited to, crude oil, decompressed crude oil, It should be understood that it may be applied to converting a wide variety of heavy oils, including resid, tar sands, bitumen, atmospheric resid, vacuum gas oil, or other heavy oils.
本開示の主題を詳細に、かつ特定の実施の形態を参照して説明してきたが、本開示に記載された様々な詳細は、特定の要素が本記載に伴う図面の各々に図示されている場合であっても、これらの詳細が、本開示に記載された様々な実施の形態の必須構成要素である要素に関連することを暗示するものと解釈すべきではないことに留意されたい。むしろ、本明細書に添付された特許請求の範囲は、本開示の広さおよび本開示に記載された様々な実施の形態の対応する範囲を唯一表すものとみなされるべきである。さらに、添付の特許請求の範囲から逸脱せずに、改変および変更が可能であることが明らかであろう。
以下、本発明の好ましい実施形態を項分け記載する。
実施形態１
流動接触分解（ＦＣＣ）触媒組成物であって、
ＵＳＹゼオライトの骨格に置換された１つ以上の遷移金属を含む骨格置換ＵＳＹゼオライト、および
前記ＦＣＣ触媒組成物の総質量に基づいて、１質量パーセントから５０質量パーセントのＦＣＣゼオライト分解用添加物、
を含むＦＣＣ触媒組成物。
実施形態２
前記１つ以上の遷移金属が、ハフニウム、ジルコニウム、チタン、またはこれらの組合せを含む、実施形態１に記載のＦＣＣ触媒組成物。
実施形態３
前記骨格置換ＵＳＹゼオライトが、２．４３０ナノメートルから２．４５０ナノメートルの結晶格子定数および６００平方メートル毎グラムから９００平方メートル毎グラムの比表面積を有する、実施形態１または２に記載のＦＣＣ触媒組成物。
実施形態４
前記ＦＣＣ触媒組成物が、該ＦＣＣ触媒組成物の総質量に基づいて５質量パーセントから６０質量パーセントの前記骨格置換ＵＳＹゼオライトを含む、実施形態１から３いずれか１つに記載のＦＣＣ触媒組成物。
実施形態５
前記ＦＣＣゼオライト分解用添加物が、ＭＦＩ骨格ゼオライト、またはより好ましくはＺＳＭ－５ゼオライトを含む、実施形態１から４いずれか１つに記載のＦＣＣ触媒組成物。
実施形態６
炭化水素供給物をアップグレードする方法において、
前記炭化水素供給物の少なくとも一部をアップグレードするのに十分な反応条件で該炭化水素供給物をＦＣＣ触媒組成物と接触させる工程であって、
前記ＦＣＣ触媒組成物は、骨格置換ＵＳＹゼオライト、および該ＦＣＣ触媒組成物の総質量に基づいて１質量パーセントから５０質量パーセントのＦＣＣゼオライト分解用添加物を含み、該骨格置換ＵＳＹゼオライトは、該骨格置換ＵＳＹゼオライトの骨格に置換された、ハフニウム、ジルコニウム、チタン、またはこれらの組合せを含む、工程、
を有してなる方法。
実施形態７
前記炭化水素供給物が、４５０セ氏温度から７００セ氏温度の温度で、０．１秒から６０秒の滞留時間に亘り、１：２から１：３０の炭化水素供給物対ＦＣＣ触媒組成物の質量比で前記ＦＣＣ触媒組成物に接触させられる、実施形態６に記載の炭化水素供給物をアップグレードする方法。
実施形態８
前記骨格置換ＵＳＹゼオライトがジルコニウムまたはチタンを含む、実施形態６または７に記載の炭化水素供給物をアップグレードする方法。
実施形態９
前記ＦＣＣ触媒組成物が、該ＦＣＣ触媒組成物の総質量に基づいて５質量パーセントから６０質量パーセントの前記骨格置換ＵＳＹゼオライトを含む、実施形態６から８いずれか１つに記載の炭化水素供給物をアップグレードする方法。
実施形態１０
前記ＦＣＣ触媒組成物の総質量に基づいて１５質量パーセントから６０質量パーセントの無機充填剤をさらに含む、実施形態６から９いずれか１つに記載の炭化水素供給物をアップグレードする方法。
実施形態１１
前記ＦＣＣゼオライト分解用添加物が、ＭＦＩ骨格ゼオライト、またはより好ましくはＺＳＭ－５ゼオライトを含む、実施形態６から１０いずれか１つに記載の炭化水素供給物をアップグレードする方法。
実施形態１２
炭化水素供給物をアップグレードする方法において、
前記炭化水素供給物を流動接触分解ユニットに通過させる工程、
前記炭化水素供給物の少なくとも一部に分解反応を経験させるのに十分な反応条件下で、前記流動接触分解ユニット内で該炭化水素供給物をＦＣＣ触媒組成物と接触させて、使用済みＦＣＣ触媒組成物と、１種類以上のオレフィンを含む分解流出物とを含む分解反応混合物を生成する工程であって、
前記ＦＣＣ触媒組成物は、
骨格置換ＵＳＹゼオライトの骨格に置換されたハフニウム、ジルコニウム、チタン、またはこれらの組合せを含む該骨格置換ＵＳＹゼオライト、および
該ＦＣＣ触媒組成物の総質量に基づいて１質量パーセントから５０質量パーセントのＦＣＣゼオライト分解用添加物、
を含む工程、
前記分解反応混合物を前記使用済みＦＣＣ触媒組成物と前記分解流出物に分離する触媒分離装置に該分解反応混合物を通過させる工程、および
前記分解流出物を前記流動接触分解ユニットから流出させる工程、
を含む方法。
実施形態１３
前記炭化水素供給物が、１：２から１：３０の炭化水素供給物対ＦＣＣ触媒組成物の質量比で前記ＦＣＣ触媒組成物と接触させられる、実施形態１２に記載の炭化水素供給物をアップグレードする方法。
実施形態１４
前記ＦＣＣ触媒組成物が、該ＦＣＣ触媒組成物の質量に基づいて５質量パーセントから６０質量パーセントの前記骨格置換ＵＳＹゼオライトを含む、実施形態１２または１３に記載の炭化水素供給物をアップグレードする方法。
実施形態１５
前記ＦＣＣゼオライト分解用添加物がＭＦＩ骨格ゼオライトを含む、実施形態１２から１４いずれか１つに記載の炭化水素供給物をアップグレードする方法。
Although the subject matter of the present disclosure has been described in detail and with reference to particular embodiments, various details described in the disclosure may be illustrated in each of the drawings accompanying the description. Note that these details should not be construed to imply that these details relate to elements that are essential components of the various embodiments described in this disclosure. Rather, the claims appended hereto are to be considered solely representative of the breadth of this disclosure and the corresponding scope of the various embodiments described herein. Furthermore, it will be apparent that modifications and changes may be made without departing from the scope of the appended claims.
Preferred embodiments of the present invention will be described below.
Embodiment 1
A fluid catalytic cracking (FCC) catalyst composition comprising:
a framework-substituted USY zeolite comprising one or more transition metals substituted in the framework of the USY zeolite, and
1 weight percent to 50 weight percent FCC zeolite cracking additive, based on the total weight of the FCC catalyst composition;
An FCC catalyst composition comprising:
Embodiment 2
FCC catalyst composition according to embodiment 1, wherein the one or more transition metals include hafnium, zirconium, titanium, or a combination thereof.
Embodiment 3
The FCC catalyst composition of embodiment 1 or 2, wherein the framework-substituted USY zeolite has a crystal lattice constant of 2.430 nanometers to 2.450 nanometers and a specific surface area of 600 square meters per gram to 900 square meters per gram. .
Embodiment 4
The FCC catalyst composition of any one of embodiments 1-3, wherein the FCC catalyst composition comprises from 5 weight percent to 60 weight percent of the framework-substituted USY zeolite, based on the total weight of the FCC catalyst composition. .
Embodiment 5
The FCC catalyst composition according to any one of embodiments 1 to 4, wherein the FCC zeolite cracking additive comprises an MFI framework zeolite, or more preferably a ZSM-5 zeolite.
Embodiment 6
In a method of upgrading hydrocarbon feeds,
contacting the hydrocarbon feed with an FCC catalyst composition at reaction conditions sufficient to upgrade at least a portion of the hydrocarbon feed;
The FCC catalyst composition includes a framework-substituted USY zeolite and an additive for cracking FCC zeolite from 1 percent by weight to 50 percent by weight based on the total weight of the FCC catalyst composition, wherein the framework-substituted USY zeolite comprises a a process comprising hafnium, zirconium, titanium, or a combination thereof substituted in the backbone of a substituted USY zeolite;
How to have.
Embodiment 7
The hydrocarbon feed is 1:2 to 1:30 mass of hydrocarbon feed to FCC catalyst composition at a temperature of 450 degrees Celsius to 700 degrees Celsius, for a residence time of 0.1 seconds to 60 seconds. 7. The method of upgrading a hydrocarbon feed according to embodiment 6, wherein the FCC catalyst composition is contacted with the FCC catalyst composition at
Embodiment 8
8. The method of upgrading a hydrocarbon feed according to embodiment 6 or 7, wherein the backbone substituted USY zeolite comprises zirconium or titanium.
Embodiment 9
The hydrocarbon feed of any one of embodiments 6-8, wherein the FCC catalyst composition comprises from 5 weight percent to 60 weight percent of the framework-substituted USY zeolite, based on the total weight of the FCC catalyst composition. How to upgrade.
Embodiment 10
10. The method of upgrading a hydrocarbon feed as in any one of embodiments 6-9, further comprising 15 weight percent to 60 weight percent inorganic filler based on the total weight of the FCC catalyst composition.
Embodiment 11
A method of upgrading a hydrocarbon feed according to any one of embodiments 6 to 10, wherein the FCC zeolite cracking additive comprises an MFI framework zeolite, or more preferably a ZSM-5 zeolite.
Embodiment 12
In a method of upgrading hydrocarbon feeds,
passing the hydrocarbon feed through a fluid catalytic cracking unit;
Contacting the hydrocarbon feed with an FCC catalyst composition in the fluid catalytic cracking unit under reaction conditions sufficient to cause at least a portion of the hydrocarbon feed to undergo a cracking reaction to produce a spent FCC catalyst. producing a cracking reaction mixture comprising a composition and a cracking effluent comprising one or more olefins, the process comprising:
The FCC catalyst composition includes:
a framework-substituted USY zeolite comprising hafnium, zirconium, titanium, or a combination thereof substituted in the framework of the framework-substituted USY zeolite, and
1 weight percent to 50 weight percent FCC zeolite cracking additive, based on the total weight of the FCC catalyst composition;
A process including;
passing the cracking reaction mixture through a catalyst separation device that separates the cracking reaction mixture into the spent FCC catalyst composition and the cracking effluent; and
draining the cracked effluent from the fluid catalytic cracking unit;
method including.
Embodiment 13
Upgrading the hydrocarbon feed of embodiment 12, wherein the hydrocarbon feed is contacted with the FCC catalyst composition at a hydrocarbon feed to FCC catalyst composition mass ratio of 1:2 to 1:30. how to.
Embodiment 14
14. The method of upgrading a hydrocarbon feed according to embodiment 12 or 13, wherein the FCC catalyst composition comprises from 5 weight percent to 60 weight percent of the framework-substituted USY zeolite based on the weight of the FCC catalyst composition.
Embodiment 15
15. The method of upgrading a hydrocarbon feed as in any one of embodiments 12-14, wherein the FCC zeolite cracking additive comprises an MFI framework zeolite.
Claims (15)
ＵＳＹゼオライトの骨格に置換された１つ以上の遷移金属を含む骨格置換ＵＳＹゼオライト、
前記ＦＣＣ触媒組成物の総質量に基づいて、１質量パーセントから５０質量パーセントのＦＣＣゼオライト分解用添加物、および
前記ＦＣＣ触媒組成物の総質量に基づいて、３５質量パーセントから６０質量パーセントの無機充填剤であって、シリカゾル、塩基性塩化アルミニウム、重リン酸アルミニウム、アルミナゾル、活性アルミナ、多孔質シリカ、金属捕捉剤、またはこれらの組合せの１つ以上を含む無機充填剤、
を含むＦＣＣ触媒組成物。 A fluid catalytic cracking (FCC) catalyst composition comprising:
a backbone-substituted USY zeolite comprising one or more transition metals substituted in the backbone of the USY zeolite ;
1 weight percent to 50 weight percent FCC zeolite cracking additive, based on the total weight of the FCC catalyst composition; and
Based on the total weight of the FCC catalyst composition, from 35 weight percent to 60 weight percent inorganic fillers, including silica sol, basic aluminum chloride, aluminum biphosphate, alumina sol, activated alumina, porous silica, metal scavenger. an inorganic filler containing one or more of these agents, or a combination thereof;
An FCC catalyst composition comprising:
前記炭化水素供給物の少なくとも一部をアップグレードするのに十分な反応条件で該炭化水素供給物をＦＣＣ触媒組成物と接触させる工程であって、
前記ＦＣＣ触媒組成物は、
骨格置換ＵＳＹゼオライトであって、該骨格置換ＵＳＹゼオライトの骨格に置換された、ハフニウム、ジルコニウム、チタン、またはこれらの組合せを含む骨格置換ＵＳＹゼオライト、
前記ＦＣＣ触媒組成物の総質量に基づいて、１質量パーセントから５０質量パーセントのＦＣＣゼオライト分解用添加物、および
前記ＦＣＣ触媒組成物の総質量に基づいて、３５質量パーセントから６０質量パーセントの無機充填剤であって、シリカゾル、塩基性塩化アルミニウム、重リン酸アルミニウム、アルミナゾル、活性アルミナ、多孔質シリカ、金属捕捉剤、またはこれらの組合せの１つ以上を含む無機充填剤、
を含む、工程、
を有してなる方法。 In a method of upgrading hydrocarbon feeds,
contacting the hydrocarbon feed with an FCC catalyst composition at reaction conditions sufficient to upgrade at least a portion of the hydrocarbon feed;
The FCC catalyst composition includes:
a backbone -substituted USY zeolite, the backbone-substituted USY zeolite comprising hafnium, zirconium, titanium, or a combination thereof substituted in the backbone of the backbone-substituted USY zeolite;
1 weight percent to 50 weight percent FCC zeolite cracking additive, based on the total weight of the FCC catalyst composition; and
Based on the total weight of the FCC catalyst composition, from 35 weight percent to 60 weight percent inorganic fillers, including silica sol, basic aluminum chloride, aluminum biphosphate, alumina sol, activated alumina, porous silica, metal scavenger. an inorganic filler containing one or more of these agents, or a combination thereof;
process, including
How to have.
前記炭化水素供給物を流動接触分解ユニットに通過させる工程、
前記炭化水素供給物の少なくとも一部に分解反応を経験させるのに十分な反応条件下で、前記流動接触分解ユニット内で該炭化水素供給物をＦＣＣ触媒組成物と接触させて、使用済みＦＣＣ触媒組成物と、１種類以上のオレフィンを含む分解流出物とを含む分解反応混合物を生成する工程であって、
前記ＦＣＣ触媒組成物は、
骨格置換ＵＳＹゼオライトの骨格に置換されたハフニウム、ジルコニウム、チタン、またはこれらの組合せを含む該骨格置換ＵＳＹゼオライト、および
該ＦＣＣ触媒組成物の総質量に基づいて１質量パーセントから５０質量パーセントのＦＣＣゼオライト分解用添加物であって、ＭＥＬ骨格ゼオライト、ベータ骨格ゼオライト、モルデナイト骨格ゼオライトまたはこれらの組合せであるＦＣＣゼオライト分解用添加物、
を含む工程、
前記分解反応混合物を前記使用済みＦＣＣ触媒組成物と前記分解流出物に分離する触媒分離装置に該分解反応混合物を通過させる工程、および
前記分解流出物を前記流動接触分解ユニットから流出させる工程、
を含む方法。 In a method of upgrading hydrocarbon feeds,
passing the hydrocarbon feed through a fluid catalytic cracking unit;
Contacting the hydrocarbon feed with an FCC catalyst composition in the fluid catalytic cracking unit under reaction conditions sufficient to cause at least a portion of the hydrocarbon feed to undergo a cracking reaction to produce a spent FCC catalyst. producing a cracking reaction mixture comprising a composition and a cracking effluent comprising one or more olefins, the process comprising:
The FCC catalyst composition includes:
a framework-substituted USY zeolite comprising hafnium, zirconium, titanium, or a combination thereof substituted in the framework of the framework-substituted USY zeolite, and from 1 percent by weight to 50 percent by weight of an FCC zeolite based on the total weight of the FCC catalyst composition. a decomposition additive for FCC zeolite, which is a MEL framework zeolite, a beta framework zeolite, a mordenite framework zeolite, or a combination thereof;
A process including;
passing the cracking reaction mixture through a catalyst separation device that separates the cracking reaction mixture into the spent FCC catalyst composition and the cracking effluent; and draining the cracking effluent from the fluid catalytic cracking unit.
method including.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US16/919,336 | 2020-07-02 | ||
| US16/919,336 US11446645B2 (en) | 2020-07-02 | 2020-07-02 | FCC catalyst compositions for fluid catalytic cracking and methods of using the FCC catalyst compositions |
| PCT/US2021/024620 WO2022005544A1 (en) | 2020-07-02 | 2021-03-29 | Fcc catalyst compositions for fluid catalytic cracking and methods of using the fcc catalyst compositions |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2023532295A JP2023532295A (en) | 2023-07-27 |
| JPWO2022005544A5 true JPWO2022005544A5 (en) | 2023-11-10 |
Family
ID=75870701
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2022580412A Pending JP2023532295A (en) | 2020-07-02 | 2021-03-29 | FCC catalyst composition and method of using FCC catalyst composition for fluid catalytic cracking |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US11446645B2 (en) |
| EP (1) | EP4149674A1 (en) |
| JP (1) | JP2023532295A (en) |
| KR (1) | KR20230065233A (en) |
| CN (1) | CN116096496A (en) |
| WO (1) | WO2022005544A1 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11566185B1 (en) | 2022-05-26 | 2023-01-31 | Saudi Arabian Oil Company | Methods and catalysts for cracking hydrocarbon oil |
| US11725149B1 (en) | 2022-06-13 | 2023-08-15 | Saudi Arabian Oil Company | Fluidized catalytic cracking processes and additives for improving gasoline yield and quality |
| WO2024069636A1 (en) | 2022-09-27 | 2024-04-04 | Hindustan Petroleum Corporation Limited | A catalyst composition for catalytic cracking of paraffin rich feed into light olefins |
| US11857955B1 (en) | 2022-10-12 | 2024-01-02 | Saudi Arabian Oil Company | Processes of producing catalysts |
Family Cites Families (30)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4210560A (en) | 1978-11-08 | 1980-07-01 | Gulf Research And Development Company | Catalytic supports with controlled pore properties |
| US4255288A (en) | 1979-08-13 | 1981-03-10 | Exxon Research & Engineering Co. | Zirconia-containing catalysts |
| US4855036A (en) | 1984-10-03 | 1989-08-08 | Uop | Catalytic cracking process |
| US4826586A (en) | 1986-09-03 | 1989-05-02 | Mobil Coil Corporation | Single riser fluidized catalytic cracking process utilizing a C3-4 paraffin-rich co-feed and mixed catalyst system |
| EP0987220A1 (en) | 1998-09-17 | 2000-03-22 | Technische Universiteit Delft | Mesoporous amorphous silicate materials and process for the preparation thereof |
| US5308813A (en) | 1993-02-01 | 1994-05-03 | Exxon Research & Engineering Company | Selective demetallation of zeolites and related materials |
| US5411724A (en) | 1993-06-02 | 1995-05-02 | W. R. Grace & Co.-Conn. | Method for substitution of alumina in the framework of zeolites by silicon |
| JP3383071B2 (en) | 1994-05-18 | 2003-03-04 | 出光興産株式会社 | New zeolite catalyst and method for producing the same |
| US6482313B1 (en) | 1994-10-03 | 2002-11-19 | Exxonmobil Research And Engineering Company | FCC process incorporating crystalline microporous oxide catalysts having increased Lewis acidity |
| US6267873B1 (en) * | 1997-04-11 | 2001-07-31 | Indian Oil Corporation, Ltd. | Fluidized catalytic cracking process |
| US6069012A (en) | 1997-05-23 | 2000-05-30 | Kayser Technology, Inc. | Versatile fluidized bed reactor |
| JP3772285B2 (en) | 1998-04-15 | 2006-05-10 | 新日本石油株式会社 | Hydrocracking catalyst for hydrocarbon oil and hydrocracking method |
| US7084087B2 (en) | 1999-09-07 | 2006-08-01 | Abb Lummus Global Inc. | Zeolite composite, method for making and catalytic application thereof |
| US6762143B2 (en) | 1999-09-07 | 2004-07-13 | Abb Lummus Global Inc. | Catalyst containing microporous zeolite in mesoporous support |
| US6346224B1 (en) | 1999-10-22 | 2002-02-12 | Intevep, S.A. | Metaloalluminosilicate composition, preparation and use |
| US6726834B2 (en) | 1999-10-22 | 2004-04-27 | Intevep, S.A. | Process for catalytic cracking of a hydrocarbon feed with a MFI aluminisilcate composition |
| US6656346B2 (en) | 2001-06-07 | 2003-12-02 | King Fahd University Of Petroleum And Minerals | Fluid catalytic cracking process for heavy oil |
| JP5033640B2 (en) | 2004-12-23 | 2012-09-26 | アンスティテュ フランセ デュ ペトロール | Improved process for producing zeolite catalysts and hydrocarbon feedstocks with controlled doping element content |
| US20090283443A1 (en) | 2005-09-12 | 2009-11-19 | Catalysts & Chemicals Industries Co., Ltd. | Catalytic composition for hydrotreating of hydrocarbons and method for hydrotreating |
| CN101134576B (en) | 2006-09-01 | 2010-09-08 | 中国石油大学(北京) | Method for improving Y-shaped molecular sieve water heat stability by employing cage heteroatom |
| CN101898144B (en) | 2009-05-27 | 2013-02-13 | 中国石油天然气股份有限公司 | Catalytic cracking catalyst of Y-type molecular sieve containing skeleton heteroatom and preparation method thereof |
| JP5640142B2 (en) | 2010-03-18 | 2014-12-10 | ダブリュー・アール・グレイス・アンド・カンパニー−コネチカット | FCC catalyst composition for high light olefins |
| CA2806118C (en) | 2010-08-02 | 2018-09-11 | Saudi Arabian Oil Company | Hydrocracking catalyst for hydrocarbon oil, method for producing hydrocracking catalyst, and method for hydrocracking hydrocarbon oil with hydrocracking catalyst |
| CA2851988C (en) | 2011-10-21 | 2019-05-21 | Igtl Technology Ltd | Methods of preparation and forming supported active metal catalysts and precursors |
| US20160017238A1 (en) | 2012-02-17 | 2016-01-21 | Kior, Inc. | Mesoporous Zeolite-Containing Catalysts For The Thermoconversion Of Biomass And For Upgrading Bio-Oils |
| GB2521515B (en) | 2013-10-22 | 2021-04-28 | China Petroleum & Chem Corp | A metal modified Y zeolite, its preparation and use |
| US9943836B2 (en) | 2013-10-22 | 2018-04-17 | China Petroleum & Chemical Corporation | Metal modified Y zeolite, its preparation and use |
| CN106660034A (en) * | 2014-05-22 | 2017-05-10 | 沙特阿拉伯石油公司 | Framework substituted zeolite catalyst for fluidized catalytic cracking and method for fluidized catalytic cracking |
| US10889768B2 (en) | 2018-01-25 | 2021-01-12 | Saudi Arabian Oil Company | High severity fluidized catalytic cracking systems and processes for producing olefins from petroleum feeds |
| US11220640B2 (en) | 2019-10-30 | 2022-01-11 | Saudi Arabian Oil Company | System and process for steam cracking and PFO treatment integrating selective hydrogenation, FCC and naphtha reforming |
-
2020
- 2020-07-02 US US16/919,336 patent/US11446645B2/en active Active
-
2021
- 2021-03-29 WO PCT/US2021/024620 patent/WO2022005544A1/en active Application Filing
- 2021-03-29 JP JP2022580412A patent/JP2023532295A/en active Pending
- 2021-03-29 CN CN202180046654.6A patent/CN116096496A/en active Pending
- 2021-03-29 EP EP21724400.3A patent/EP4149674A1/en active Pending
- 2021-03-29 KR KR1020237004000A patent/KR20230065233A/en unknown
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US10870802B2 (en) | High-severity fluidized catalytic cracking systems and processes having partial catalyst recycle | |
| EP0127285B1 (en) | Secondary injection of zsm-5 type zeolite in catalytic cracking | |
| KR101798970B1 (en) | Catalystic cracking apparatus and process thereof | |
| AU766848B2 (en) | Fluid cat cracking with high olefins production | |
| US7611622B2 (en) | FCC process for converting C3/C4 feeds to olefins and aromatics | |
| JP5424879B2 (en) | Ancillary disassembly of paraffinic naphtha using FCC unit operation | |
| TWI404794B (en) | An integrated fluid catalytic cracking process | |
| JP6158807B2 (en) | Fluid catalytic cracking of paraffinic naphtha in a downflow reactor | |
| JP2020517793A (en) | Improving Light Olefin Yield by Steam Catalytic Downer Pyrolysis of Hydrocarbon Feedstocks | |
| US20130001130A1 (en) | Dual riser catalytic cracking process for making middle distillate and lower olefins | |
| US20030196933A1 (en) | Process and apparatus for upgrading FCC product with additional reactor with catalyst recycle | |
| US9816037B2 (en) | Methods and systems for increasing production of middle distillate hydrocarbons from heavy hydrocarbon feed during fluid catalytic cracking | |
| JPS6384632A (en) | Fluid catalytic cracking method | |
| US5637207A (en) | Fluid catalytic cracking process | |
| WO2001004237A2 (en) | Catalytic production of light olefins rich in propylene | |
| JP2003504500A (en) | Catalytic production of light olefins from naphtha feed | |
| CN108350367B (en) | Method and system for fluid catalytic cracking | |
| US4802971A (en) | Single riser fluidized catalytic cracking process utilizing hydrogen and carbon-hydrogen contributing fragments | |
| EP1049754A1 (en) | Catalytic cracking for olefin production | |
| JP5988875B2 (en) | Catalytic conversion method to increase cetane barrel of diesel fuel | |
| US4888103A (en) | Process of stripping in a catalytic cracking operation employing a catalyst mixture which includes a shape selective medium pore silicate zeolite component | |
| JP2023537258A (en) | Fluid Catalytic Cracking Using a Catalyst System Containing a Modified Beta Zeolite Additive | |
| JPWO2022005544A5 (en) | ||
| EP3555236A1 (en) | Process integration for cracking light paraffinic hydrocarbons | |
| WO2006067104A1 (en) | Gasoline cracking |