Abstract: Disclosed herein are adjuvanted protein vaccines comprising: a non-phospholipid liposome and one or more proteins, wherein the protein is encapsulated within the non-phospholipid liposome, and wherein the protein is selected from: (i) a modified full-length spike protein that generates IgG antibody responses for 120 days after two injections of the adjuvanted protein vaccine, by subcutaneous or intramuscular routes; (ii) a modified spike protein sequence of a coronavirus; (iii) a protein sequence from a coronavirus; and (iv) a protein from an infectious agent that generates IgG antibody responses to proteins after one or two subcutaneous or intramuscular injections. Also disclose herein are modified spike protein sequence containing a modified full-length SARS-COV-2 spike protein sequence. Methods of use of the vaccines and sequences are also disclosed herein.

Abstract: Disclosed herein are adjuvanted protein vaccines comprising: a non-phospholipid liposome and one or more proteins, wherein the protein is encapsulated within the non-phospholipid liposome, and wherein the protein is selected from: (i) a modified full-length spike protein that generates IgG antibody responses for 120 days after two injections of the adjuvanted protein vaccine, by subcutaneous or intramuscular routes; (ii) a modified spike protein sequence of a coronavirus; (iii) a protein sequence from a coronavirus; and (iv) a protein from an infectious agent that generates IgG antibody responses to proteins after one or two subcutaneous or intramuscular injections. Also disclose herein are modified spike protein sequence containing a modified full-length SARS-COV-2 spike protein sequence. Methods of use of the vaccines and sequences are also disclosed herein.

Abstract: The present disclosure is directed to examples of a light emitting diode (LED) device. In one embodiment, the LED device includes a printed circuit board (PCB), at least one LED chip electrically coupled to the PCB, a LED package to encapsulate the at least one LED chip, and at least one volatile organic compound (VOC) barrier layer coating the LED package.

Abstract: Disclosed herein are subcutaneously administered, immunogenic compositions (e.g., vaccines) and methods of using and preparing the same. In some embodiments, the immunogenic compositions generate IgG antibodies to the spike proteins of the Wuhan-Hu-1, Delta B.1.617.2, and Omicron BA.1 variants of SARS-CoV-2 and may be suitable for use in preventing an infectious disease, such as SARS-CoV-2.

Abstract: Disclosed herein are adjuvanted protein vaccines comprising: a SARS-CoV-2 variant C.1.2 modified S1 Spike protein sequence and a non-phospholipid liposome, wherein the protein is encapsulated within the non-phospholipid liposome. The adjuvanted protein vaccines are suitable for subcutaneous administration. Also disclosed herein are modified spike protein sequences containing SARS-CoV-2 variant C.1.2 modified S1 Spike proteins and methods of use of the vaccines and sequences.

Abstract: Disclosed herein are immunogenic compositions (e.g., vaccines) and methods of using and preparing the same. In some embodiments, the immunogenic compositions are suitable for use in treating or preventing an infectious disease, such as SARS-CoV-2 or HIV.

Abstract: A compact catalytic reactor (20) comprises a channel for a rapid reaction having an inlet (26) for a gas mixture to undergo the reaction. The channel is provided with two different catalyst structures (32, 34), a first catalyst structure (32) in the vicinity of the inlet (26) and a second catalyst structure (34) further from the inlet, such that a gas mixture supplied to the inlet flows past them both. The first catalyst structure (32) has little catalytic activity for the rapid reaction, whereas the second catalyst structure (34) has catalytic activity for the rapid reaction. This is applicable to combustion of gas mixtures containing hydrogen, for which the first catalyst structure (32) may comprise uncoated oxidised aluminium-containing ferritic steel, while the second catalyst structure (34) may incorporate Pt and/or Pd in an alumina support. Exhaust gases may also be recycled to the inlet (26) to inhibit combustion.

Abstract: A metal substrate is coated with a layer of ceramic, by spraying droplets of a slurry of a ceramic precursor onto the substrate, the substrate being at a temperature between 500° C. and 750° C. The ceramic comprises alumina, and is made macroporous by spraying a mixture of alumina sol and alumina particles with no more than 35% by weight of dispersible alumina. Spraying onto a red-hot surface in this fashion leads to a very marked improvement in adhesion of the resulting ceramic to the metal substrate. A catalytically active material may then be incorporated in the ceramic layer, so as to form a catalyst structure (16).

Abstract: Biological waste materials are mixed with water and subjected to intense ultrasonic irradiation (14), before being supplied to an anaerobic digester (16), so that a biogas is generated which contains methane. The biogas is supplied to a catalytic reformer unit (20) to form a synthesis gas; steam may also be supplied, and the proportion of steam to methane is adjustable so that the synthesis gas may be rich in hydrogen or alternatively rich in carbon monoxide. Adjusting the proportion of steam to biogas enables the output of the process to be adjusted according to market conditions. If the synthesis gas is rich in hydrogen, it may be supplied to a fuel cell (26) to generate electricity, while if it is rich in carbon monoxide, it may be used to generate liquid hydrocarbons in a Fischer-Tropsch synthesis reactor (32).

Abstract: Natural gas is reacted with steam, to generate carbon monoxide and hydrogen in a first catalytic reactor; the resulting gas mixture is used to perform Fischer-Tropsch synthesis in a second catalytic reactor. After performing Fischer-Tropsch synthesis, the remaining hydrogen is separated from a hydrocarbon-rich stream using a hydrogen-permeable membrane, and the hydrocarbon-rich stream is returned to be subjected to steam reforming. Preferably the hydrogen-rich stream is supplied to a combustion channel to provide heat for the endothermic steam-reforming reaction. The overall process converts natural gas to longer-chain hydrocarbons and can provide a carbon conversion of more than 80%.

Abstract: Natural gas is reacted with steam, to generate carbon monoxide and hydrogen in a first catalytic reactor (16); the resulting gas mixture is used to perform Fischer-Tropsch synthesis in a second catalytic reactor (26). After cooling the resulting gas stream in a heat exchanger (29), the remaining gas stream (30) is cooled a second time by decreasing its pressure (32), and the resulting condensed liquid is separated (33) from the remaining gas phase. This increases the production of condensate. The second cooling step may utilise a turbine (32), or a vortex tube (40), or a throttle valve.

Abstract: A valve assembly (10) comprises a valve stem (14) with a bore (15) and radial apertures (17), and a sleeve (18) closed atone end and slidable over the valve stem (14) to obstruct the apertures (17). At the end of the valve stem opposite the outlet end, the valve stem (14) defines a fluidic vortex chamber (22) with both tangential inlets (28) and non-tangential peripheral inlets (26), and with an axial outlet (24) communicating with the bore (15). The sleeve (18) defines at least one radial port (32) near its closed end. The valve assembly operates in a conventional fashion except when approaching closure. Once the last of the apertures (17) in the valve stem has been closed, the only flow path is through the fluidic vortex chamber (22). Further movement of the sleeve (18) alters the distribution of the flow between the non-tangential inlets (26) and the tangential inlets (28), so adjusting the strength of the fluidic vortex and the resistance to fluid flow.

Abstract: A catalytic reactor (40) comprises a plurality of sheets (42) defining flow channels (44) between them. Within each flow channel (44) is a foil (46) of corrugated material whose surfaces are coated with catalytic material apart from where they contact the sheets (44). At each end of the reactor (40) are headers to supply gas mixtures to the flow channels (44), the headers communicating with adjacent channels being separate. The reactor (40) enables different gas mixtures to be supplied to adjacent channels (44), which may be at different pressures, and the corresponding chemical reactions are also different. Where one of the reactions is endothermic while the other reaction is exothermic, heat is transferred through the sheets (42) separating the adjacent channels (44), from the exothermic reaction to the endothermic reaction.

Abstract: A composition and method for forming a composite material comprising a mixture of component A and component B, component A comprising gypsum and an inhibitor; and component B comprising an accelerator, wherein at least one of component A and component B further comprises a polymer binder having a Tg of below ?23° C. or wherein the Shore D hardness of the composite material when cured is less than 70; the method comprising providing a first slurry mixture of component A and a second slurry mixture of component B and blending the first slurry mixture and the second slurry mixture to form a soft composite using a weight ratio of from 10:1 to 1:2.

Abstract: Fischer-Tropsch synthesis is performed using a compact catalytic reactor unit (10) defining channels in which is a gas-permeable catalyst structure (16), the channels extending between headers (18). The synthesis occurs in at least two stages, as the reactor unit provides at least two successive channels (14, 14a) for the Fischer-Tropsch synthesis connected by a header, the gas flow velocity through the first channel being sufficiently high that no more than 65% of the carbon monoxide undergoes conversion. The gases are cooled (25) in the header between the two stages, so as to condense water vapour, and then pass through the second channel at a sufficiently high gas flow velocity that no more than 65% of the remaining carbon monoxide undergoes conversion. This lowers the partial pressure of water vapour and so suppresses oxidation of the catalyst.

Abstract: Fischer-Tropsch synthesis is performed on a CO/H*2 feed gas using a plurality of compact catalytic reactor modules (12) each defining catalytic reaction channels and coolant channels, in two successive stages, with the same number of reactor modules for each stage. The gas flow velocity in the first stage is sufficiently high that no more than 75% of the CO undergoes conversion. The gases are cooled (16) between successive stages so as to remove water vapour, and the pressure is reduced (20) before they are subjected to the second stage. In addition the reaction temperature for the second stage is lower than for the first stage, such that no more than 75% of the remaining carbon monoxide undergoes conversion during the second stage too. The deleterious effect of water vapour on the catalyst is hence suppressed, while the overall capacity of the plant (10) can be adjusted by closing off modules in each stage while keeping the numbers equal.

Abstract: A compact catalytic reactor comprises a stack of plates (72, 74, 75) to define a multiplicity of first and second flow channels arranged alternately in the stack; each flow channel in which a chemical reaction is to take place is defined by straight-through channels across at least one plate, each such straight-through channel containing a removable gas-permeable catalyst structure (80) incorporating a metal substrate. The first flow channels (76) are oriented in a direction that is perpendicular to that of the second flow channels (77), and between successive second flow channels in the stack the reactor defines at least three side-by-side first flow channels (76); and the reactor incorporates flow diversion means (80; 88) such that the first fluid must flow through at least three such first flow channels (76) in succession, in flowing from an inlet to an outlet. The overall flow paths can therefore be approximately co-current or counter-current.

Abstract: Natural gas is processed to generate longer-chain hydrocarbons, the process comprising subjecting the gas to steam reforming to generate a mixture of carbon monoxide and hydrogen, and then subjecting this mixture to Fischer-Tropsch synthesis. The Fischer-Tropsch synthesis is performed at an elevated temperature above 230° C. and with a gas hourly space velocity greater than 10 000 hr?1 so as to achieve a selectivity to the production of C5+ hydrocarbons that is less than 65%. The resulting liquid product can be used as a vehicle fuel, while the tail gases may be used to generate electricity.

Abstract: Natural gas is processed to generate longer-chain hydrocarbons, the process comprising subjecting the gas to steam reforming to generate a mixture of carbon monoxide and hydrogen, and then subjecting this mixture to Fischer-Tropsch synthesis. The reforming reaction (20) is performed at 0.4-0.5 MPa and the Fischer-Tropsch synthesis (50) at 1.8-2.1 MPa, and two compressors (36, 44) are used to raise the pressure, the gas mixture being cooled (26, 32, 40) before and after the first compressor (36). This reduces both the operating cost and capital cost of the plant.

Abstract: A valve system (10) controls the fluid flow between an inlet (12) and an outlet (14). The system (10) splits the flow into two parallel flow ducts (15, 16) and recombines the flows through opposed tangential inlets (18) and (19) of a fluidic vortex valve (20) which has an axial outlet (22). An adjustable valve (24) controls the flow through one of the parallel flow ducts (15), controlling the strength of the vortex generated within the vortex valve (20). Hence a small valve (24) can control and adjust the flows in both ducts (15 and 16).