A method for executing multiple chemical experiments in parallel may be provided. The method comprises receiving a list of actions to be performed for synthesizing a chemical product. Thereby, the actions correspond to at least two chemical partial reactions and the list comprises a delimiter symbol separating two chemical partial reactions, determining identical chemical partial reactions, and building a reaction commonality tree (RCT) of the chemical reactions. Furthermore, the method comprises executing a plurality of the identical chemical partial reactions independent of a sequence of chemical partial reactions of the reaction commonality tree only once. Each of the identical chemical partial reactions is executed in a different chemical reactor and each resulting intermediate product has a quantity of the sum of the related identical chemical partial reactions. The method also comprises, storing the intermediate chemical products in a separate container, and executing remaining chemical partial reactions according to the RCT.

Various embodiments of the present disclosure relate to proactive dosing optimization chemical feed units producing an output solution (such as an oxidizing biocide) therefrom. Online sensors generate signals corresponding to directly measured variables for respective process components. Information is selectively retrieved from models relating combinations of input variables to respective industrial process states, wherein various current process states may be indirectly determined based on directly measured variables for respective system components. An output feedback signal is automatically generated corresponding to a detected intervention event based on the indirectly determined process state. A controller may receive the signal and implement, e.g., regulation of oxidizing biocide feed for optimization of end products and/or performance metrics.

Processes for dehydrogenation of a hydrocarbon feedstock are described. The process can be run at lower H.sub.2/HC ratios and lower RITs while maintaining coke production at the same level as operation at higher H.sub.2/HC ratios and higher RITs without decreasing the yield per pass. Acceptable levels of coke were achieved when operating the process at low hydrogen to hydrocarbon molar ratio in the range of 0.01 to 0.40 and reactor inlet temperatures in the range of 500-645 C.

Disclosed are methods and apparatuses for processing a powder alloy to improve its microstructure. The methods for processing the powder alloy can include introducing the powder alloy into a powder vessel having an inert atmosphere, uniformly heat treating the powder alloy inside the powder vessel at its solutionizing temperature, and cooling the heat treated powder alloy at a rate of at least 5 C./s to form treated particles. The treated particles obtained from the methods and apparatuses disclosed herein can be used in any suitable manufacturing process, such as in cold gas dynamic spray.

Methods for determining the concentration of transition metal compounds in a solution containing more than one transition metal compound are described. Polymerization reactor systems providing real-time monitoring and control of the concentrations of the transition metal components of a multicomponent catalyst system are disclosed, as well as methods for operating such polymerization reactor systems and for improving methods of preparing the multicomponent catalyst system.

Processes for dehydrogenation of a hydrocarbon feedstock are described. The process can be run at lower H.sub.2/HC ratios and lower RITs while maintaining coke production at the same level as operation at higher H.sub.2/HC ratios and higher RITs without decreasing the yield per pass. Acceptable levels of coke were achieved when operating the process at low hydrogen to hydrocarbon molar ratio in the range of 0.01 to 0.40 and reactor inlet temperatures in the range of 500-645 C. The process uses a low coke catalyst.

Large pill dehydrogenation catalysts and large screens slot width are combined in dehydrogenation units to reduce the pressure drop across the catalyst bed and reactor screens compared to conventional screen and catalyst size combinations. The catalyst has an average pill diameter in the range of 1.6 mm to 3.0 mm, and the slot width of the screen is in the range of about 30% to about 60% of the pill diameter.

A process includes periodically or continuously introducing an olefin monomer and periodically or continuously introducing a catalyst system or catalyst system components into a reaction mixture within a reaction system, oligomerizing the olefin monomer within the reaction mixture to form an oligomer product, and periodically or continuously discharging a reaction system effluent comprising the oligomer product from the reaction system. The reaction system includes a total reaction mixture volume and a heat exchanged portion of the reaction system comprising a heat exchanged reaction mixture volume and a total heat exchanged surface area providing indirect contact between the reaction mixture and a heat exchange medium. A ratio of the total heat exchanged surface area to the total reaction mixture volume within the reaction system is in a range from 0.75 in.sup.1 to 5 in.sup.1, and an oligomer product discharge rate from the reaction system is between 1.0 (lb)(hr.sup.1)(gal.sup.1) to 6.0 (lb)(hr.sup.1)(gal.sup.1).

A test system comprising a reactor having a fluid circuit and a test zone for an item under test. A plurality of control zones are included in the fluid circuit for controlling parameters of the fluid in accordance with control information. A control system receives input data specifying test values for the fluid parameters, predicts the behaviour of the fluid using the input data and a mathematical model of the reactor, calculates control information based on the predicted fluid behaviour, and communicates the control information to the control zones. The system can simulate transient test conditions by selective use of fluid evacuation and dilution, and by use of temperature and flow bypass circuits.

Systems for producing performic acid and methods for producing performic acid. The systems may include two or more reactor units, two or more servient programmable logic controllers, a control panel, and a master programmable logic controller. The system may modify the production of performic acid in at least one of the two or more reactor units upon and/or after the occurrence of a disruptive event in order to maintain a desired level of performic acid production and/or a desired level of disinfection.