Abstract: Process for the preparation of olefins comprising reacting an oxygenate and/or olefinic feed in a reactor in the presence of a molecular sieve catalyst to form a mixture which comprises olefins and at least partially coked catalyst; passing at least partially coked catalyst to a regenerator; introducing into the regenerator an oxygen-containing gas to regenerate the at least partially coked catalyst, thereby producing a gaseous mixture and at least partially regenerated catalyst; separating at least partially regenerated catalyst and at least part of the gaseous mixture; analysing the composition of the gaseous mixture to control the burning rate of the coke present on the at least partially coked catalyst in the regenerator by adjusting the mass flow rate of the oxygen-containing gas on the basis of the analysis of the gaseous mixture; and passing at least part of the at least partially regenerated catalyst back to the reactor.

Abstract: Process for the regeneration of an at least partially coked molecular sieve catalyst comprising introducing the at least partially coked catalyst into a regenerator; introducing into the regenerator an oxygen-containing gas to regenerate at least part of the at least partially coked catalyst, thereby producing a gaseous mixture and at least partially regenerated catalyst; recovering part of the at least partially regenerated catalyst; analysing the at least partially regenerated catalyst to control the burning rate of the coke present on the at least partially coked catalyst in the regenerator by adjusting one or more conditions of the regeneration of the at least partially coked catalyst on the basis of the analysis of the at least partially regenerated catalyst; and separating at least partially regenerated catalyst and at least part of the gaseous mixture as obtained in step (b).

Abstract: Process for the regeneration of an at least partially coked molecular sieve catalyst comprising introducing the at least partially coked catalyst into a regenerator; introducing into the regenerator an oxygen-containing gas to regenerate at least part of the at least partially coked catalyst, thereby producing a gaseous mixture and at least partially regenerated catalyst; separating at least partially regenerated catalyst and at least part of the gaseous mixture; and analyzing the composition of the gaseous mixture to control the burning rate of the coke present on the at least partially coked catalyst in the regenerator by adjusting the mass flow rate of the oxygen-containing gas on the basis of the analysis of the gaseous mixture.

Abstract: A composition capable of radiation activated catalysis is provided. The composition comprises a metal compound, a mercapto compound and an olefinic compound. Radiation curable urethane compositions comprising the disclosed composition are also provided. The radiation curable urethane compositions comprise the disclosed composition, a hydroxyl compound and an isocyanate compound. Activation of the composition by radiation in a urethane formulation provides for an efficient method of curing the urethane composition. Coating and adhesive compositions comprising the radiation curable urethane compositions are also provided. In addition, methods for coating and bonding substrates are disclosed.

Abstract: A method of producing a regenerated hydrotreating catalyst, including a first step of preparing a hydrotreating catalyst that has been used for hydrotreatment of a petroleum fraction and has a metal element selected from Group 6 elements of the periodic table; a second step of performing regeneration treatment for part of the catalyst prepared in the first step, then performing X-ray absorption fine structure analysis for the catalyst after the regeneration treatment, and obtaining regeneration treatment conditions in which a ratio IS/IO of a peak intensity IS of a peak attributed to a bond between the metal element and a sulfur atom to a peak intensity IO of a peak attributed to a bond between the metal element and an oxygen atom is in the range of 0.1 to 0.3 in a radial distribution curve obtained from an extended X-ray absorption fine structure spectrum.

Abstract: Process for the regeneration of an at least partially coked molecular sieve catalyst comprising introducing the at least partially coked catalyst into a regenerator; introducing into the regenerator an oxygen-containing gas to regenerate at least part of the at least partially coked catalyst, thereby producing a gaseous mixture and at least partially regenerated catalyst; separating at least partially regenerated catalyst and at least part of the gaseous mixture; and analysing the composition of the gaseous mixture to control the burning rate of the coke present on the at least partially coked catalyst in the regenerator by adjusting the mass flow rate of the oxygen-containing gas on the basis of the analysis of the gaseous mixture.

Abstract: Process for the regeneration of an at least partially coked molecular sieve catalyst comprising introducing the at least partially coked catalyst into a regenerator; introducing into the regenerator an oxygen-containing gas to regenerate at least part of the at least partially coked catalyst, thereby producing a gaseous mixture and at least partially regenerated catalyst; recovering part of the at least partially regenerated catalyst; analysing the at least partially regenerated catalyst to control the burning rate of the coke present on the at least partially coked catalyst in the regenerator by adjusting one or more conditions of the regeneration of the at least partially coked catalyst on the basis of the analysis of the at least partially regenerated catalyst; and separating at least partially regenerated catalyst and at least part of the gaseous mixture as obtained in step (b).

Abstract: A desulfurization method of a nitrogen oxide absorption catalyst when diesel is used may include determining how many times a regeneration of a diesel particulate filter (DPF) is completed, ending a DPF regeneration, if the number of times of the DPF regeneration reaches a predetermined value and entering into a desulfurization mode to desulfurize the DPF, ending the desulfurization mode after the desulfurization mode is performed for a predetermined time, and calculating a particulate matters (PM) amount that is trapped in the DPF after the desulfurization, compensating the trapped PM amount, and determining a time of the DPF regeneration. A desulfurization timing is determined based on the number of times that the DPF is regenerated to be able to simplify the desulfurization logic and also reduce the memory of ECU, when the LNT catalyst is poisoned by a small amount of sulfur included in exhaust gas.

Abstract: Process for providing a flow of particulate matter to a reactor, by intermittently adding the particulate matter and a diluent to a mixing tank, and continuously withdrawing a slurry of particulate matter in diluent from the mixing tank for introduction into the reactor. Prior to each addition of particulate matter and diluent to the mixing tank, the concentration of particulate matter in the diluent already in the mixing tank is measured or calculated, and the amount of particulate matter and diluent subsequently added is measured so as to achieve the same concentration at the end of the addition as that measured or calculated prior to the addition.

Abstract: A system and method for desulfurizing an oxidation catalyst enhances fuel economy and reduces noxious exhaust gas emission as a consequence of increasing desulfurization period of the oxidation catalyst or shortening desulfurization time by reflecting desulfurization history consisting of natural desulfurization occurrence. The method may include detecting an inlet temperature of the oxidation catalyst, estimating natural desulfurization according to the inlet temperature of the oxidation catalyst, and resetting desulfurization time or desulfurization period by reflecting the estimated natural desulfurization.

Abstract: In an embodiment, a method is disclosed to increase the activity of an ionic liquid catalyst comprising emulsifying the ionic liquid catalyst with one or more liquid components. In an embodiment, a method is disclosed comprising introducing into a reaction zone a monomer feed and a reduced amount of ionic liquid catalyst and controlling an amount of shear present in the reaction zone to maintain a desired conversion reaction of the monomer. In an embodiment, a catalyzed reaction system is disclosed comprising a reactor configured to receive one or more liquid components and ionic liquid catalyst; a device coupled to the reactor for adding high shear to the liquid components and ionic liquid catalyst; and a controller coupled to the device for adding high shear and configured to control the amount of shear added to a catalyzed reaction zone to maintain a conversion reaction.

Abstract: A process is disclosed for providing a flow of particulate matter such as a catalyst to a reactor, comprising intermittently adding said particulate matter and a diluent to a mixing tank, and continuously withdrawing a slurry of particulate matter in diluent from the mixing tank for introduction into the reactor, wherein prior to each addition of particulate matter and diluent to the mixing tank, the concentration of particulate matter in the diluent already in the mixing tank is measured or calculated, and the amount of particulate matter and diluent subsequently added is measured so as to achieve the same concentration at the end of the addition as that measured or calculated prior to the addition. Preferably measurement of the amount of particulate mailer and diluent added to the mixing tank is carried out before any diluent is added to the particulate matter.

Abstract: The catalytic efficiency of supported catalysts containing metal nanoparticles is strongly related to the chemical softness at the surfaces of such nanoparticles. The chemical softness of a nanoparticle is obtained using results from Density Functional Theory modeling, an extended version of Embedded Atom Method modeling, and continuum modeling based on size and shape of the nanoparticle. A metal nanoparticle of a certain size and shape is first modeled using the extended EAM and EAM parameters that have been validated with results from DFT modeling, to obtain atomic energy densities at each atom location. The chemical softness value at each atom location is then calculated from the atomic energy densities and various parameters that are derived based on results from DFT modeling. The surface chemical softness value is derived from the local chemical softness values based on the geometry and atomistic structure of the metal nanoparticle.

Abstract: A catalyst development engine for providing a rapid approach to the rational development of scalable heterogeneous catalysts and of high-performance solid materials. The catalyst development engine includes three main components: the high-throughput data generation cycle, the knowledge generation cycle, and the knowledge repository or database. The high-throughput data generation cycle rapidly generates high quality data in a high-throughput mode for the virtual and experimental evaluation of new catalytic materials and also generates data on well-characterized systems for use in the knowledge generation cycle. The knowledge generation cycle generates working hypotheses, relating performance to key catalyst properties, which guide the search for better catalysts, and generates fundamental structure-property relationships required in order to select catalysts for further experimental evaluation in the high-throughput cycle.

Abstract: A process and apparatus for cooling FCC catalyst that provides two modes of operation for a remote heat exchanger type cooler. In the first mode the exchanger is operated in a backmix fashion where catalyst is circulated between the cooler and a disengagement zone. Regenerated catalyst is withdrawn from an outlet located close to the heat exchanger inlet so that essentially all of the heat removed by the cooler serves to reduce the temperature of catalyst entering the reaction zone. This mode of operation is particularly useful in obtaining a benefit from the cooler when processing light to moderate FCC feeds. In the second mode, the exchanger is operated in a flow through mode where hot catalyst is withdrawn from the disengaging zone cooled in the exchanger and passed into the combustion zone. The second mode of operation is used to withdraw heat from the overall regeneration process in the case of heavy FCC feedstock conversion.

Abstract: A method and apparatus for passivating the adverse catalytic effects of metal contaminated hydrocarbon feedstocks is described. The method is directed at the use of control means to regulate the residence time of the catalyst in the passivation zone and to regulate the reducing gas flow rate to the passivation zone.

Abstract: In a process for the reactivation of a catalyst, which is used for the removal of NO.sub.x, oxides of nitrogen, from exhaust gases, the catalyst should be capable of easy reactivation. For this purpose, when the catalyst starts to lose its activity, it is exposed in a reducing atmosphere to a carbon monoxide current. In an apparatus for the execution of the process, the catalyst is placed in two separate chambers. The carbon monoxide stream is directed alternately to both chambers.

Abstract: A process and apparatus for the cooling of hot fluidized solid particles such as catalyst of an FCC petroleum refining process. The particles flow downward from a first dense phase fluidized bed into a cooling chamber and contact the shell side of a vertically oriented shell and tube heat exchanger where cooling occurs via indirect heat exchange with a cooling medium circulating in the tubes. The extent of cooling is controlled by the varying of the heat transfer coefficient between the tubes and particles in the heat exchanger. The coefficient is varied by changing the quantity of fluidizing gas fed to the fluidized bed in the heat exchanger. The heat exchanger is located within a lower portion of the cooling chamber totally below the particle inlet and outlet conduits. The heat exchanger can therefore be removed from service and protected by being buried under unfluidized relatively cool catalyst. The fluidizing gas supports combustion within a lower combustion zone.

Abstract: A process vessel which contains a control system for maintaining average pressure drop across gas discharge nozzles above a minimum valve to prevent the occurrence of inactive nozzles, said nozzles comprising part of a distributor which is used to distribute gas across the lower portion of the processing vessel, wherein the control system comprises:(a) means for establishing a flow signal representative of the rate of flow of gas in said pipeline supplying the gas to said distributor;(b) means for establishing a temperature signal representative of the temperature of the gas flowing in said distributor;(c) means for establishing a pressure signal representative of the pressure of the gas flowing in said distributor;(d) computing means for calculating the average pressure drop across said nozzles using said flow, pressure, and temperature signals and appropriate constant parameters and equations;(e) means for comparing said average pressure drop across said nozzles with a minimum value, generating a correction

Abstract: Where gas flows through distribution nozzles and then up through a liquid or a bed of particles contained in a processing vessel, the method and apparatus of this invention can be used to maintain a minimum average pressure drop across the nozzles, thus preventing the occurrence of inactive nozzles and the consequences thereof.

Abstract: A process and associated apparatus for the cooling of hot fluidized solid particles. The particles flow from a first dense phase fluidized bed into the shell side of a vertically oriented shell and tube heat exchanger where cooling occurs via indirect heat exchange with a cooling medium circulating in the tubes. The extent of cooling is controlled by the varying of the heat transfer coefficient between the tubes and particles in the heat exchanger which are maintained as a second dense phase fluidized bed. The coefficient is varied by varying the quantity of fluidizing gas to the fluidized bed in the heat exchanger. The particles flow freely to and from the first and second dense phase fluidized beds through which the particles recirculate and are backmixed. The process has particular applicability to a combustive regeneration process and most particular applicability to the FCC process.