Catalytic reactor engineering ⇒ information-driven design of packed (operando), fluidized, multi-functional, and -phase reactors

Problem statement

At lab-scale, the ultimate goal of a catalytic reactor is to provide (1) reliable kinetic information, neglecting or controlling other phenomena (heat-mass transfer and hydrodynamics); (2) high-throughput data to amplify the results, accelerate model and catalyst discoveries; and (3) results with the minimum requirements of reactants and wastes generated. The pillars of these reactors are quality, quantity, and safety.

We design, build and test different laboratory-scale reactors. Our strategy involves creating and testing reactor prototypes while modeling these using our workflow. We have high-speed cameras, probes, and other measuring instruments to understand the reactor behavior. We focus on packed-, fluidized-bed, and multiphase reactors:

In packed bed reactors, we focus on forced dynamic and operando reactors. These are the quintessence of information-driven reactors where the dynamics can involve flow changes, temperature, pressure, partial pressure, presence of activity modifiers (poissons, H2O…). In operando reactors, we follow a spectro-kinetic-deactivation-hydrodynamic approach to resolve the individual steps involved. In fluidized bed reactors, we focus on downers and multifunctional reactors (circulating, multizone or two-zone, Berty reactors) We focus on trickle-bed, slurry, and bio-electrochemical reactors in multiphase bed reactors.

Al pilot-plant scale, we aim to reach the maximum productivity levels while solving the growing pains: the scale-up. Based on a robust kinetic model obtained in the intrinsic kinetic reactor (lab-scale) and using computational fluid dynamics, we design, build, and operate pilot plants. At this stage, we seek partnerships with investment or industrial enterprises to make these pilot plants.

Goals

  • Multifunctional fluidized bed reactors ⇒ multizone, circulating...
  • Packed bed membrane reactors
  • Forced dynamic reactors ⇒ pulsing, SSITKA...
  • Forced dynamic operando reactors ⇒ DRIFTS, TPSR...
  • Operando reactors
  • Spray fluidized bed reactors
  • Downer reactor I ⇒ micro downer
  • Downer reactor II ⇒ counter-current and scale-up
  • Batch Berty reactor ⇒ short contact time
  • Multiphase reactors ⇒ trickle bed and slurry
  • High throughput experimentation (HTE) reactors
  • Photo-thermal and bioreactors
  • Reactor visualization and prototyping lab
  • Spatio-temporal hydrodynamic characterization and validation

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Related Publications

Polyethylene Cracking on a Spent FCC Catalyst in a Conical Spouted Bed

by Elordi, Olazar, Castaño, Artetxe, Bilbao
Ind. Eng. Chem. Res. Year: 2012

Abstract

The catalytic cracking of HDPE (high density polyethylene) at 500 °C using a spent FCC catalyst agglomerated with bentonite (50 wt %) has been studied in a conical spouted bed reactor. The reaction is carried out in continuous regime (1 g min–1 of HDPE is fed) with no bed defluidization problems. The results obtained, namely, total conversion, and high yields of gasoline (C5–C11 fraction) (50 wt %) and C2–C4 olefins (28 wt %), are explained by favorable reactor conditions and good catalyst properties. These results are compared with those for a catalyst prepared in the laboratory by agglomerating a commercial HY zeolite (SiO2/Al2O3 = 5.2). The conical spouted bed is a suitable reactor for enhancing the physical steps of melting the polymer and coating the catalyst with the melted polymer. Furthermore, high heat and mass transfer rates promote devolatilization, and short residence times minimize secondary reactions from olefins by enhancing primary cracking products. The meso- and macroporous structure of the spent FCC catalyst matrix enhances the diffusion of long polymer chains, whereas the zeolite crystals have micropores that give a proper shape selectivity to form the lumps of gasoline and light olefins. Because of long use in reaction–regeneration cycles, the moderate acidity of the spent FCC catalyst minimizes the secondary reactions of hydrogen transfer, and so restricts the formation of aromatics and paraffins, as well as the reactions of overcracking and condensation and, therefore, the coke formation. The spent FCC catalyst exhibits a low deactivation rate and is regenerable by coke combustion with air at 550 °C. Consequently, the use of a catalyst with the sole cost of a simple agglomeration and the production of value added product streams make the process of polyolefin catalytic cracking a promising option for refinery integration.

Keywords

FCC W2C CRE