A process and apparatus for fluidized catalytic cracking of heavy oils is disclosed using a modified high efficiency catalyst regenerator. A fast fluidized bed coke combustor, which is essentially free of gas/catalyst separation means, partially regenerates catalyst and discharges a steam laden flue gas and catalyst into a dilute phase transport riser. Closed cyclones separate catalyst from steam laden flue gas exiting the transport riser outlet. This flue gas is isolated from a second fluidized bed of catalyst maintained in a vessel containing the transport riser and closed cyclones. Coke combustion in the drier region of the second fluidized bed is possible. Catalyst deactivates less in the second fluidized bed because it is drier.

Heavy oil catalytic cracking process and apparatus

Acetylene (C2 H2 ) capture is a step in a number of industrial processes, but it comes with a high-energy footprint. Although physisorbents have the potential to reduce this energy footprint, they are handicapped by generally poor selectivity versus other relevant gases, such as CO2 and C2 H4 . In the case of CO2 , the respective physicochemical properties are so similar that traditional physisorbents, such as zeolites, silica, and activated carbons cannot differentiate well between CO2 and C2 H2 . Herein, we report that a family of three isostructural, ultramicroporous (<7 A) diamondoid metal-organic frameworks, [Cu(TMBP)X] (TMBP=3,3',5,5'-tetramethyl-4,4'-bipyrazole), TCuX (X=Cl, Br, I), offer new benchmark C2 H2 /CO2 separation selectivity at ambient temperature and pressure. We attribute this performance to a new type of strong binding site for C2 H2 . Specifically, halogen⋅⋅⋅HC interactions coupled with other noncovalent in a tight binding site is C2 H2 specific versus CO2 . The binding site is distinct from those found in previous benchmark sorbents, which are based on open metal sites or electrostatic interactions enabled by inorganic fluoro or oxo anions.

Halogen–C2H2 Binding in Ultramicroporous Metal–Organic Frameworks (MOFs) for Benchmark C2H2/CO2 Separation Selectivity

Process and apparatus for rapidly cracking a hydrocarbon feed followed by rapid separation of the cracked gases from the particulate solids including a cracking reactor having offset orifices and at least two opposed inlet nozzles in the same plane, an entrained bed heater having an array of fuel inlet nozzles in a plane at the bottom of the heater and axially directed air inlet nozzles, and a separator assembly for separating particulate solids from the gaseous products thus produced.

Particulate solids cracking apparatus and process

A method and system for recovering fines from a light FCC-type effluent gas. Cracked gases from the reactor are cooled by direct contact with circulating oil in an oil quench tower. The circulating oil also washes out the catalyst fines carried with the reactor effluent gas. A flow of the oil from the quench tower bottoms is sent through one of a pair of filters to remove fines and recycled to the tower. The other filter is in backwash operation using a compressed gas to remove the fines therefrom and into a surge drum. Fuel oil or quench oil is added to the drum to form a slurry, which carries the catalyst fines to the regenerator where the oil is combusted to supply the FCC system heat requirements. Since a minimum amount of fuel oil is generated in the FCC, fuel oil is imported to inventory the quench tower.

Catalyst recovery from light olefin fcc effluent

Effective quenching is provided in a catalytic cracking process to increase product yield and decrease thermal cracking. To this end, the quench is injected at special locations and a special quench is used. In the illustrated embodiment, the quench is injected into the oil product immediately downstream of an external gross cut separator before the product enters a disengaging vessel and the quench comprises cycle oil.

Quenching downstream of an external vapor catalyst separator

Acetylene is obtained by thermal cracking of liquid hydrocarbons in the presence of insufficient oxygen for complete combustion by reacting part of the liquid product containing carbon black with oxygen by burning in a free space and introducing into the combustion products lateral, penetrating jets first of hydrocarbon to be cracked in an amount of 1-3 kg. per cubic metre (S.T.P.) of oxygen and then, as quenching fluid, liquid product containing carbon black in an amount to reduce the temperature below 500 DEG C. The flame direction is preferably upward and the reactor walls may be washed with liquid cracked product. The amount of liquid product, boiling above 85 DEG C., recycled to the burner may be 30-150% of the hydrocarbons to be cracked. The process may be effected at 1-20 atmospheres, the combustion products being at 1200-2800 DEG C. before mixing with the hydrocarbon feed and 800-1600 DEG C. after. Diluent gases, e.g. steam or carbon dioxide, may be introduced at any point as desired. In an example, crude petroleum oil is cracked.

Production of acetylene by thermal cracking of liquid hydrocarbons

In the production of gaseous olefins by cracking hydrocarbons such as crude oil or a crude oil distillate at 680 DEG -850 DEG C. in the presence of fluidized, hot, inert, heat carrier particles which circulate between the reactor and a regenerator where the heat necessary for the cracking is supplied by burning carbon deposits on the particles and by combustion of part of the oil residues boiling above 200 DEG C. from the product which have been used to quench the vapour leaving the reactor to below 400 DEG C., the particles used have a grain size between 0,05 and 4 mm., at least 10% having a size above 1 mm. The feedstock, having a final boiling point of 200 DEG -400 DEG C., is injected into reactor 1 by line 9 where it is contacted with a fluidized bed of hot inert solids, e.g. aluminium silicate containing more than 50% by weight of alumina, corundum, sillimanite or mullite. The cyclone 11 is adjusted so that the vapours leaving it still contain 5-50 grams of solid per normal cubic meter which prevent carbon deposits in the exit pipe. The vapours are quenched in vessel 13 with residual oil from line 15; this also removes the solids from the vapours. From receiver 17 the vapours are introduced into fractionating column 19 where gases and gasoline are recovered overhead, fuel oil by line 28, a rinsing oil for pump 26 by line 25 and quenching oil by line 24. Solids leave reactor 1 by standpipe 3 which is at an angle to the vertical of not more than 20 degrees and passed to regenerator 2 by riser 4 using air, flue gas or nitrogen introduced by line 30; the amount of solid leaving the reactor is regulated by a gas stream 29. In the regenerator carbon deposits and oil from line 32 are burned with sufficient excess oxygen to ensure an oxygen content of 0,3-3% by volume in the flue gas. This gas may be used as a conveying gas. Solids are returned to the reactor by pipes 5 and 6, steam being used as the conveying gas. Steam is also preferably used as the fluidizing gas.

Sinn Richard

Papers

Production of acetylene by thermal cracking of liquid hydrocarbons

Cracking of hydrocarbons to gaseous olefines

Procédé pour le mélange de substances solides

Verfahren zur Herstellung von Acetylen durch thermische Spaltung von fluessigen Kohlenwasserstoffen

Verfahren zur Spaltung von Kohlenwasserstoffen zu gasfoermigen Olefinen