A reactor layout for a process of methanol production from low quality synthesis gas, in which relatively smaller adiabatic reactors can be operated more efficiently, some of the inherent disadvantages of adiabatic reactors for methanol production are avoided. This is done by controlling the outlet temperature in the pre-converter by rapid adjustment of the recycle gas, i.e. by manipulating the gas hourly space velocity in the pre-converter.

This invention relates to the preparation of N-(phosphonomethyl)glycine (“glyphosate”) from N-(phosphonomethyl)iminodiacetic acid (“PMIDA”), and more particularly to methods for control of the conversion of PMIDA, for the identification of reaction end points relating to PMIDA conversion and the preparation of glyphosate products having controlled PMIDA content. One such method involves obtaining a series of Fourier transform infrared (“FTIR”) analyses of the PMIDA content of the aqueous reaction medium or a sample thereof during the course of the reaction. From a plurality of FTIR analyses, a projection is made of the batch reaction time or continuous oxidation residence time within the oxidation reaction zone at which a target conversion or end point may be anticipated to be attained or is attained.

A polyester with ultra-high flowability and good stability over time is provided. The polyester can be polybutylene terephthalate (PBT) or another aliphatic polyester, whose intrinsic viscosity (IV) is less than 0.6 dL/g and a carboxylic end group (CEG) content is 15 meq/kg or less, and characterized by having a melt volume rate (MVR) of greater than 400 cm.sup.3/10 min at 250° C. A resin composition of this polyester is provided, which can be meltblown into microfibers of a uniform diameter and a concentrated diameter distribution, forming a fabric with a uniform small pore size.

In the hydroconversion processes of heavy hydrocarbon oils, in which the hydrogen is introduced at the reactor base by bubbling, the low diffusion rate of hydrogen, from the gas phase to the reaction liquid, limits the degree of conversion. The process circumvents the obstacle of the limited amount of reactant hydrogen by using a slurry bubble column reactor which reduces the formation of light hydrocarbon products, and therefore the hydrogen required for the hydroconversion, allowing to operate at full conversion.

A process and system for maintaining optimum polymerization production in a loop polymerization reactor by continuously and periodically obtaining polymerization results, such as melt index (MI), production rate and ash content of the polymer produced, determining whether each of the results is within desired ranges, storing and averaging recently obtained results in a database within a reaction rate controller program, and when one of the results is out of the desired range modifying at least one reaction parameter set-point such as monomer concentration, catalyst feed rate and reactor temperature to drive any out-of-range polymerization result(s) toward the desired range for that result.

A chemical plant or a petrochemical plant or a refinery may include one or more pieces of equipment that process one or more input chemicals to create one or more products. For example, catalytic dehydrogenation can be used to convert paraffins to the corresponding olefin. A delta temperature controller may determine and control differential temperature across the reactor, and use a delta temperature to control a set point for a heater temperature controller. By doing so, the plant may ramp up a catalytic dehydrogenation unit faster and ensure it does not coke up the catalyst and/or foul a screens too quickly. Catalyst activity may be taken into account and allow the plant to have better control over production and run length of the unit.

A method for process monitoring and control of a chemical reactor in which a chemical reaction utilizing a halogenated selectivity modifier is performed includes: measuring a level of halogenated components in an inlet stream of a reactor inlet; measuring a level of halogenated components in an outlet stream of a reactor outlet; based on the level of halogenated components at the inlet stream and the outlet stream, determining a process performance indicator associated with a halogenated component; and adjusting an amount of halogenated selectivity modifier added to the reactor based on the process performance indicator.

A biomass torrefaction system includes a reactor vessel for biomass particles, a burner for combusting one or more fuels to produce a heated gas, a fan for supplying a flow of the heated gas through the reactor vessel to heat the biomass particles, and a controller configured to calculate a torrefaction index according to one or more sensed parameters of the system. The sensed parameter(s) include at least one of a reactor vessel retention time, a reactor vessel temperature difference and a higher heating value (HHV) of a syngas output by the reactor vessel. The controller is also configured to automatically adjust one or more operation values of the system according to the calculated torrefaction index. The operation value(s) include at least one of the reactor vessel retention time, a heating rate of the system, and a mixture of the one or more fuels combusted by the burner.

Techniques regarding the synthesis of one or more polymers of a target polymer class are provided. For example, one or more embodiments described herein can comprise a system, which can comprise a memory that can store computer executable components. The system can also comprise a processor, operably coupled to the memory, and that can execute the computer executable components stored in the memory. The computer executable components can comprise a recommendation component that can generate a recommended chemical reactor control setting for inverse synthesis of a polymer based on a target polymer characteristic and reactor training data.

An elastomer rheology process can include: receiving material formation data associated with an elastomer; conveying the elastomer towards one or more rollers that compress and stretch the elastomer according to a predetermined rolling profile comprising roller gap and speed settings; sensing a first dimension of a first portion of the elastomer before the first portion of the elastomer is passed through the sheeter; sensing a second dimension of a second portion of the elastomer after the second portion of the elastomer is passed through the sheeter; and calculating an elastomer property of the elastomer based on the controlled roller gap width, a measured roller force, the first dimension, and the second dimension.