Abstract: A uniflow cyclone that has multiple inlets, normally achieved via a vane, a barrel length, then a solids collection channel of larger diameter but concentric with the barrel and a tangential solids outlet to either a plenum or a dust hopper. The gas flows past the enlarged channel and continues through additional barrel length to an outlet zone. The cyclone would normally have a concentric center pipe the extends from the vane to the gas outlet of the cyclone.

Abstract: A uniflow cyclone that has multiple inlets, normally achieved via a vane, a barrel length, then a solids collection channel of larger diameter but concentric with the barrel and a tangential solids outlet to either a plenum or a dust hopper. The gas flows past the enlarged channel and continues through additional barrel length to an outlet zone. The cyclone would normally have a concentric center pipe the extends from the vane to the gas outlet of the cyclone.

Abstract: A counter-current catalyst regenerator with at least two stages of counter-current contact is proposed. Each stage may comprise a permeable barrier that allows upward passage of oxygen-containing gas and downward passage of coked catalyst into each stage, but inhibits upward movement of catalyst to mitigate back mixing and approximate true counter-current contact and efficient combustion of coke from catalyst.

Abstract: A compact dual stage cyclone separation assembly, an efficient dual stage cyclone separator, and a method for utilizing the same, comprising a lower pressure drop across the dual stage separators due to fewer particle-contaminated gas flow directional changes in the particle contaminated gas stream, and method for using same. The dual stage cyclone separator comprises a primary stage cyclone barrel and a second stage cyclone barrel, wherein the second stage cyclone barrel is coaxial with and concentric within the first cyclone separator, a solids extraction port, wherein said sidewall of said main body defines a solids extraction port opening located between said upper end and said lower end for discharging large particles from said cyclone body, and a small particle discharge opening, wherein the small particle discharge opening is located inside the lower end of the main body.

Abstract: A counter-current catalyst regenerator with at least two stages of counter-current contact is proposed. Each stage may comprise a permeable barrier that allows upward passage of oxygen-containing gas and downward passage of coked catalyst into each stage, but inhibits upward movement of catalyst to mitigate back mixing and approximate true counter-current contact and efficient combustion of coke from catalyst.

Abstract: One exemplary embodiment can be a fluid catalytic cracking process. The process can include a reaction zone operating at conditions to facilitate olefin production and including at least one riser. The at least one riser can receive a first feed having a boiling point of about 180° to about 800° C., and a second feed having more than about 70%, by weight, of one or more C4+ olefins.

Abstract: One exemplary embodiment can be a process for fluid catalytic cracking. The process can include withdrawing a catalyst from a reaction vessel to replace a catalyst inventory over a period of about 10- about 35 days for maximizing propylene yield.

Abstract: A process for improving the yield of ethylene and propylene from a light naphtha feedstock includes obtaining light naphtha feedstock from a primary cracking zone having a cracking catalyst. The light naphtha feedstock is contacted with an olefin catalyst in an olefin producing zone to produce an ethylene- and propylene-rich stream. After reacting with the olefin catalyst, the ethylene- and propylene-rich stream is separated from the olefin catalyst from in a separator zone. At least a portion of the olefin catalyst is regenerated by combusting coke deposited on a surface of the olefin catalyst in an oxygen-containing environment, and at least a portion of the olefin catalyst is heated. These portions could be the same one or they could be different. In some embodiments, at least a portion of the olefin catalyst could be neither regenerated nor heated. The olefin catalyst is returned to the olefin producing zone.

Abstract: A process and apparatus for improving flow properties of crude may include processing a first crude stream, which may in turn include cracking the first crude stream with catalyst to form a cracked stream and spent catalyst, hydrotreating a portion of the cracked stream and then mixing the hydrotreated stream with an unprocessed second crude stream.

Abstract: A process for improving flow properties of crude may include processing a first crude stream, which may in turn include cracking the first crude stream with fresh catalyst to form a cracked stream and spent catalyst, and then mixed with an unprocessed second stream. The spent catalyst may be regenerated to form fresh catalyst, which may then be recycled. At least part of the cracked stream may be mixed with a second crude stream. A ratio of the second crude stream to the first crude stream may be between about 0.5:1 and about 9:1. A ratio of part of the cracked stream to add to the second crude stream may be selected to achieve a API gravity of at least about 18. The first crude stream may be heated and stripped before being cracked.

Abstract: One exemplary embodiment can be a process for stripping. The process can include passing catalyst to a stripping vessel containing a riser, providing a plurality of baffles having a first baffle and a second baffle, and providing one or more packing layers. The stripping vessel and riser may define an annular zone including annular area for stripping of the catalyst, and the first and second baffles collectively overlap in no more than about 50% of the annular area. Often, the first baffle is coupled to an outer circumference of the riser and extends outward, and the second baffle is coupled to an inner circumference of the stripping vessel and extends inward. Typically, the one or more packing layers are within the annular zone.

Abstract: Embodiments of a gas-solids separation unit and embodiments of a method for manufacturing a separation unit are provided. In one embodiment, the separation unit includes a cyclonic separator and a vessel having a flue gas chamber, a clean gas chamber, and an entrained solids chamber between the flue gas chamber and the clean gas chamber. The cyclonic separator includes, in turn, a cyclone barrel extending from the flue gas chamber toward the clean gas chamber, a swirl vane positioned across the cyclone barrel, a gas outlet tube fluidly coupling the cyclone barrel to the clean gas chamber, and a first check valve opening formed through the barrel sidewall upstream of the gas outlet tube. The check valve opening fluidly couples the cyclone barrel to the entrained solids chamber to permit the centrifugal separation of the particulate matter from the gas stream during operation of the gas-solids separation unit.

Abstract: Process for increasing mixing in a fluidized bed. A slide, which may be in the form of a tube or trough, transports particles from an upper zone downward to a lower zone at a different horizontal position, thereby changing the horizontal position of the particle and creating lateral mixing in the fluidized bed. Increased mixing may improve efficiency for an apparatus using a fluidized bed. For example, increased lateral mixing in a regenerator may increase temperature and oxygen mixing and reduce stagnation to improve efficiency. A slide may be relatively unobtrusive, inexpensive, and simple for a retrofit or design modification and may improve combustion efficiency at high rates by enhancing the lateral blending of spent and regenerated catalyst.

Abstract: Cyclone separators and separator devices for separating gas and entrained particles from a particle-contaminated gas stream are provided. The cyclone separator comprises a cyclone body having a first end and a second end with a sidewall extending therebetween. The cyclone body defines a cyclone gas inlet for receiving the particle-contaminated gas stream. A cyclone gas outlet is for discharging the clean gas stream. A centripetal accelerator is proximate the cyclone gas inlet to induce centripetal acceleration of the particle-contaminated gas stream. The sidewall defines a discharge opening between the first end and the second end for discharging separated particles from the cyclone body. The discharge opening has a leading edge and a top edge in relation to a flow path of entrained particles within the particle-contaminated gas stream. The top edge extends at an acute angle relative to the leading edge.

Abstract: Cyclone separators and separator devices for separating gas and entrained particles from a particle-contaminated gas stream are provided. The cyclone separator comprises a cyclone body having a first end and a second end with a sidewall extending therebetween. The cyclone body defines a cyclone gas inlet for receiving the particle-contaminated gas stream. A cyclone gas outlet is for discharging the clean gas stream. A centripetal accelerator is proximate the cyclone gas inlet to induce centripetal acceleration of the particle-contaminated gas stream. The sidewall defines a discharge opening between the first end and the second end for discharging separated particles from the cyclone body. The discharge opening has a leading edge and a top edge in relation to a flow path of entrained particles within the particle-contaminated gas stream. The top edge extends at an acute angle relative to the leading edge.

Abstract: Embodiments of a gas-solids separation unit and embodiments of a method for manufacturing a separation unit are provided. In one embodiment, the separation unit includes a cyclonic separator and a vessel having a flue gas chamber, a clean gas chamber, and an entrained solids chamber between the flue gas chamber and the clean gas chamber. The cyclonic separator includes, in turn, a cyclone barrel extending from the flue gas chamber toward the clean gas chamber, a swirl vane positioned across the cyclone barrel, a gas outlet tube fluidly coupling the cyclone barrel to the clean gas chamber, and a first check valve opening formed through the barrel sidewall upstream of the gas outlet tube. The check valve opening fluidly couples the cyclone barrel to the entrained solids chamber to permit the centrifugal separation of the particulate matter from the gas stream during operation of the gas-solids separation unit.

Abstract: A process for improving the yield of ethylene and propylene from a light naphtha feedstock includes obtaining light naphtha feedstock from a primary cracking zone having a cracking catalyst. The light naphtha feedstock is contacted with an olefin catalyst in an olefin producing zone to produce an ethylene- and propylene-rich stream. After reacting with the olefin catalyst, the ethylene- and propylene-rich stream is separated from the olefin catalyst from in a separator zone. At least a portion of the olefin catalyst is regenerated by combusting coke deposited on a surface of the olefin catalyst in an oxygen-containing environment, and at least a portion of the olefin catalyst is heated. These portions could be the same one or they could be different. In some embodiments, at least a portion of the olefin catalyst could be neither regenerated nor heated. The olefin catalyst is returned to the olefin producing zone.

Abstract: One exemplary embodiment can be a fluid catalytic cracking process. The process can include a reaction zone operating at conditions to facilitate olefin production and including at least one riser. The at least one riser can receive a first feed having a boiling point of about 180° to about 800° C., and a second feed having more than about 70%, by weight, of one or more C4+ olefins.

Abstract: A process and apparatus for improving flow properties of crude may include processing a first crude stream, which may in turn include cracking the first crude stream with catalyst to form a cracked stream and spent catalyst, hydrotreating a portion of the cracked stream and then mixing the hydrotreated stream with an unprocessed second crude stream.

Abstract: One exemplary embodiment can be a fluid catalytic cracking system. The system can include a reaction zone operating at conditions to facilitate olefin production and including at least one riser. The at least one riser can receive a first feed having a boiling point of about 180-about 800° C., and a second feed having more than about 70%, by weight, of one or more C4+ olefins.