ENHANCED OLEFIN RECOVERY PROCESS

A demethanizer employing C3, C4 and C4+ hydrocarbons as absorbents can be employed in a methanol to olefin process to reduce both operating and capital costs in comparison to a convention process which employs only cryogenic distillation to remove methane and other low boilers from a light olefin process stream. By reducing the use of propane, the size and operating costs of the C3 splitter can be reduced thereby providing an economic advantage over conventional applications.

ENHANCED OLEFIN RECOVERY PROCESS

A demethanizer employing C3, C4 and C4+ hydrocarbons as absorbents can be employed in a methanol to olefin process to reduce both operating and capital costs in comparison to a convention process which employs only cryogenic distillation to remove methane and other low boilers from a light olefin process stream. By reducing the use of propane, the size and operating costs of the C3 splitter can be reduced thereby providing an economic advantage over conventional applications. 1. A method for producing olefins from methanol , the method comprising employing a demethanizer to remove methane from a light olefin containing process stream wherein the demethanizer uses an absorbent selected from the group consisting of C3 , C4 , and C4+ hydrocarbons , and combinations thereof , wherein when the absorbent is a C3 hydrocarbon it is not exclusively propane.2. The method of claim 1 , wherein propane makes up less than ten percent of the total amount of the selected absorbent.3. The method of claim 1 , wherein propane makes up less than one percent of the total amount of the selected absorbent.4. The method of claim 1 , wherein an effluent of the demethanizer is sent to a deethanizer.5. The method of claim 4 , wherein a first portion of an effluent from the deethanizer is returned to the demethanizer.6. The method of claim 5 , wherein a second portion of the effluent from the deethanizer is sent to a debutanizer.7. The method of claim 6 , wherein a portion of an effluent of the debutanizer is sent to the demethanizer.8. The method of claim 5 , wherein a third portion of the effluent from the deethanizer is sent to a C3 splitter.9. The method of claim 8 , wherein a portion of an effluent of the C3 splitter is sent to the demethanizer.10. A system for producing olefins from methanol claim 8 , comprising:demethanizer configured to remove methane from a light olefin containing process stream wherein the demethanizer uses an absorbent selected from the group consisting of C3, C4, ...

SYSTEM AND METHOD FOR CATALYST REMOVAL FROM MTO EFFLUENT

According to the invention a system and method for catalyst removal from MTO effluent is provided. The method includes removing catalyst from methanol to olefin effluent including contacting the methanol to olefin effluent with a wash oil separate the catalyst fines from the effluent into the wash oil and cool the effluent, separating the catalyst fines from the cooled effluent in a separator or a column to obtain an essentially catalyst free effluent, directing the catalyst free effluent out from the separator or the column, slurrying the separated catalyst fines to obtain a slurry and directing the slurry to one or more filters to filter out the catalyst. 1. A method for recovering catalyst from a methanol to olefin effluent , the method comprising:a) contacting methanol to olefin effluent with wash oil to separate catalyst fines from the effluent;b) withdrawing slurry comprising catalyst fines and wash oil from the cooled effluent in a separator or column to obtain an essentially catalyst free effluent;c) filtering the slurry by at least one filter through slurry circulating pump;d) returning the filtered wash oil from filter to quench fitting as a recirculated wash oil;e) back flushing the filter by gaseous medium to flush the catalyst fines; andf) collecting the catalyst fines from a accumulator.2. The method of further comprising recirculated wash oil is routed to contact with methanol to olefin effluent.3. The method of where circulating the oil-catalyst slurry through a filter comprises continuously passing the oil-catalyst slurry through at least one first filter in a filtration mode to separate the catalyst therefrom giving filtrate while at least one second filter in parallel with the first filter is in a backwashing mode thereby removing the separated catalyst therefrom.4. The method of further comprising returning filtrate from the filter to the oil quench.5. The method of where the backwashing of the at least one filter further comprises periodically ...

Processes for catalytic paraffin dehydrogenation and catalyst recovery

A paraffin having 2-8 carbon atoms may be dehydrogenated by contacting the paraffin with metal oxide catalyst(s) to produce light olefins, such as propylene, under certain reaction conditions in a riser, fluidized bed, or fixed-bed swing reactor. The resulting metal oxide catalyst fines contained in the reactor effluent stream formed by the dehydrogenation reaction may be recovered by contacting the reactor effluent stream with a wash fluid to form a catalyst effluent stream that is subsequently slurried and filtered to capture the catalyst fines for potential reuse.

Integrated catalytic cracking and steam pyrolysis process for olefins

Integration of gas oil and light olefin catalytic cracking zones with a pyrolytic cracking zone to maximize efficient production of petrochemicals is disclosed. Integration of the units in parallel allows production of an overall product stream with maximum ethylene and/or propylene by routing various feedstreams and recycle streams to the appropriate cracking zone(s), e.g. ethane/propane to the steam pyrolysis zone and C 4 C 6 olefins to the light olefin cracking zone. This integration enhances the value of the material balances produced by the integrated units.

Integrated catalytic cracking and steam pyrolysis process for olefins

Integration of gas oil and light olefin catalytic cracking zones with a pyrolytic cracking zone to maximize efficient production of petrochemical feedstocks is disclosed Integration of the units in parallel allows production of an overall product stream with maximum ethylene and/or propylene by routing various feedstreams and recycle streams to the appropriate cracking zone(s), eg. Ethane /propane to the steam pyrolysis zone and C[err] - C[err] olefins to the light olefin cracking zone. This integration enhances the value of the material balances produced by the integrated units even while using the lowest value feedstreams.

Integrated light olefin separation/cracking process

Systems and methods for producing a hydrocarbon are provided. The method can include separating a hydrocarbon comprising olefins and paraffins to produce an olefin-rich hydrocarbon comprising about 70 wt % or more olefins and a paraffin-rich hydrocarbon comprising about 70 wt % or more paraffins. The method can also include cracking at least a portion of the olefin-rich hydrocarbon in the presence of one or more catalysts at conditions sufficient to produce a cracked product comprising about 20 wt % or more C 2 -C 3 olefins.

オレフィンのための統合された接触分解および水蒸気熱分解法

【課題】接触分解装置と熱分解的／熱的分解装置とを統合して石油化学用供給原料の効率的製造を最大限に増加させる方法を提供する。 【解決手段】軽油および軽質オレフィン接触分解ゾーンと熱分解的分解ゾーンとを、色々な供給材料流れおよび再循環流れを適切な分解ゾーン（１つまたは複数）へと、例えばエタン／プロパンを水蒸気熱分解ゾーンへと、そしてＣ ４ −Ｃ ６ オレフィンを軽質オレフィン分解ゾーンへとそのルートを定めるように平行統合する。この統合によって最大のエチレンおよび／またはプロピレンを有する総合生成物流れの製造を可能にする。この統合は、最低の価値の供給材料流れを用いながらでも統合された装置によってもたらされる物質バランスの価値を高め、かくして石油化学供給原料の効率的な製造を最大限に増加させる。 【選択図】図３

Integrated light olefin separation/cracking process

Systems and methods for producing a hydrocarbon are provided. The method can include separating a hydrocarbon comprising olefins and paraffins to produce an olefin-rich hydrocarbon comprising about 70 wt% or more olefins and a paraffin-rich hydrocarbon comprising about 70 wt% or more paraffins. The method can also include cracking at least a portion of the olefin-rich hydrocarbon in the presence of one or more catalysts at conditions sufficient to produce a cracked product comprising about 20 wt% or more C 2 -C 3 olefins.

Processes for catalytic paraffin dehydrogenation and catalyst recovery

A paraffin having 2-8 carbon atoms may be dehydrogenated by contacting the paraffin with metal oxide catalyst(s) to produce light olefins, such as propylene, under certain reaction conditions in a riser, fluidized bed, or fixed-bed swing reactor. The resulting metal oxide catalyst fines contained in the reactor effluent stream formed by the dehydrogenation reaction may be recovered by contacting the reactor effluent stream with a wash fluid to form a catalyst effluent stream that is subsequently slurried and filtered to capture the catalyst fines for potential reuse.

Integrated carbon capture and olefins production process

Carbon capture of carbon dioxide (CO2) gives an extracted CO2 stream that is reacted with hydrogen to produce methanol (MeOH), which can in turn be fed to catalytic production of olefins such as ethylene and propylene to give an integrated process.

Integrated carbon capture and olefins production process

Carbon capture of carbon dioxide (CO 2 ) gives an extracted CO 2 stream that is reacted with hydrogen to produce methanol (MeOH), which can in turn be fed to catalytic production of olefins such as ethylene and propylene to give an integrated process.

Processes for catalytic paraffin dehydrogenation and catalyst recovery

Integrated carbon capture and olefins production process

Carbon capture of carbon dioxide (CO 2 ) gives an extracted CO 2 stream that is reacted with hydrogen to produce methanol (MeOH), which can in turn be fed to catalytic production of olefins such as ethylene and propylene to give an integrated process.

Integrated carbon capture and olefins production process

Carbon capture of carbon dioxide (CO2) gives an extracted CO2 stream that is reacted with hydrogen to produce methanol (MeOH), which can in turn be fed to catalytic production of olefins such as ethylene and propylene to give an integrated process.

Processes for catalytic paraffin dehydrogenation and catalyst recovery

A paraffin having 2-8 carbon atoms may be dehydrogenated by contacting the paraffin with metal oxide cataiyst(s) to produce light olefins, such as propylene, under certain reaction conditions in a riser, fluidized bed, or fixed-bed swing reactor. The resulting metal oxide catalyst fines contained in the reactor effluent stream formed by the dehydrogenation reaction may be recovered by contacting the reactor effluent stream with a wash fluid to form a catalyst effluent stream that is subsequently slurried and filtered to capture the catalyst fines for potential reuse.

Processes for catalytic paraffin dehydrogenation and catalyst recovery

A paraffin having 2-8 carbon atoms may be dehydrogenated by contacting the paraffin with metal oxide catalyst(s) to produce light olefins, such as propylene, under certain reaction conditions in a riser, fluidized bed, or fixed-bed swing reactor. The resulting metal oxide catalyst fines contained in the reactor effluent stream formed by the dehydrogenation reaction may be recovered by contacting the reactor effluent stream with a wash fluid to form a catalyst effluent stream that is subsequently slurried and filtered to capture the catalyst fines for potential reuse.

Electrification of heat supply to fluidized regeneration system

A system for reactivating a catalyst having a predetermined heat content includes a reactor, a regenerator, and an electrically energized heater. The reactor is configured to generate a spent catalyst. The regenerator is configured to receive the spent catalyst from the reactor. The electrically energized heater has a plurality of energy emitting members at least partially immersed in the spent catalyst. The heater is configured to provide a supplemental heat content to obtain the predetermined heat content.

Electrification of heat supply to fluidized regeneration system

A system for reactivating a catalyst having a predetermined heat content includes a reactor, a regenerator, and an electrically energized heater. The reactor is configured to generate a spent catalyst. The regenerator is configured to receive the spent catalyst from the reactor. The electrically energized heater has a plurality of energy emitting members at least partially immersed in the spent catalyst. The heater is configured to provide a supplemental heat content to obtain the predetermined heat content.