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 on-board Flex-Fuel H.sub.2 reforming apparatus provides devices and the methods of operating these devices to produce a combustible reformate containing H.sub.2 and CO from hydrocarbons and bio-fuels. For this generator, one or more parallel autothermal reformers are used to convert the fuels into the reformate over Pt group metal catalysts, and the produced reformate is then cooled, compressed and stored in vessels at a pressure between 1 to 100 atmospheres. The reformate from the storage vessels is used either as the sole fuel or is mixed with other fuels as the fuel mixture for a lean burn engine/gas turbine. For this system, the pressure of the storage vessels and the flow control curves are used directly to control the amount of the reformers' reformate flow output.

The present invention provides an improved process for removing heat from an exothermic reaction. In particular, the present invention provides a process wherein heat can be removed from multiple reaction trains using a common coolant system.

Houdry lumps can be reduced by controlling the reactors in a fixed bed dehydrogenation process for producing olefins according to defined rules. A programmable logic controller can apply the rules to the operation of the dehydrogenation unit and control the operation of individual reactors according to the rules. By doing so, the performance of dehydrogenation units can be improved without adding any heat generating inerts, such as CuO- alumina For example, the dehydrogenation units can be operated according to combinatorics in the programmable logic controller such that the farthest two reactors in the dehydrogenation unit never operate in parallel in the dehydrogenation or air regeneration steps.

The invention relates to a process for treating a lignocellulosic biomass comprising a solids content of not more than 80% by weight, said process comprising the use of at least one reactor (9,14) for treating said biomass, in which the or at least one of said reactors is fed with biomass via a feed means (6,11) creating a pressure increase between the biomass inlet and the biomass outlet of said feed means, in which said feed means is washed by circulation of a washing fluid between a washing inlet (7,12) and a washing outlet (8,13). According to the process, at least a portion of the washing fluid (8,13) exiting the fluid outlet of the at least one feed means (6,11) is reintroduced into the washing inlet of the same feed means or of another of said feed means.

Provided is a graphene production method using Joule heating, including: a catalytic metal placement step in which a catalytic metal is disposed on a pair of electrodes disposed inside a chamber; a gas supply step in which a carbon-containing reaction gas and a carrier gas for transporting the reaction gas are supplied into the chamber; a heating step in which the catalytic metal is rapidly heated to a temperature required for synthesis of graphene; a temperature maintenance step in which the temperature of the catalytic metal is maintained to form the graphene on the catalytic metal; and a cooling step in which the catalytic metal is cooled to prevent local occurrence of hotspots on the graphene formed on the catalytic metal, wherein the heating step, the temperature maintenance step, and the cooling step constitute one cycle of temperature control and the cycle is repeated for a predetermined process time.

Disclosed herein are various examples of systems, methods and devices for an oxygen reduction system with a universally compatible, adaptive front end that can be coupled with various different gas sources, wherein the oxygen reduction system determines its operations separate and independent from any signal lines from any upstream components or systems. In one example, the oxygen reduction system determines its functions, operations, and operational states from parameters that it measures from the input gas stream and other internal measurements. In this manner, installation of an oxygen reduction system is simplified, time-efficient and universal, and embodiments of the present disclosure provide for oxygen reduction systems that can be installed in a variety of different environments, applications, and with new or existing natural gas productions sites.

Systems and methods are provided for improving the operation of groups of reverse flow reactors by operating reactors in a regeneration portion of the reaction cycle to have improved flue gas management. The flue gas from reactor(s) at a later portion of the regeneration step can be selectively used for recycle back to the reactors as a diluent/heat transport fluid. The flue gas from a reactor earlier in a regeneration step can be preferentially used as the gas vented from the system to maintain the desired volume of gas within the system. This results in preferential use of higher temperature flue gas for recycle and lower temperature flue gas for venting from the system. This improved use of flue gas within a reaction system including reverse flow reactors can allow for improved reaction performance while reducing or minimizing heat losses during the regeneration portion of the reaction cycle.

Producing C5 olefins from steam cracker C5 reeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a traction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system. Other aspects of the C5 olefin systems and processes, including catalyst configurations and control schemes, are also described.

Producing C5 olefins from steam cracker C5 feeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a fraction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system. Other aspects of the C5 olefin systems and processes, including catalyst configurations and control schemes, are also described.