HYDROTHERMAL LIQUEFACTION SYSTEM (iEdison No. 0685901-19-0011)
Using a two stage heat exchanger with two independent heat exchanger designs to heat up HTL feedstock will drastically reduce the capital investment for a HTL plant. The first stage HTL heat exchanger will be rated for lower pressure, and maximize the heat exchanger area by reducing the tube size within the pressure drop limits of the system. The second heat exchanger will involve large tubes to produce a turbulent stream, thereby changing the heat transfer regime and drastically increasing the heat transfer. The second heat exchanger will be rated for high pressure.
Methods and Compositions for Degradation of Lignocellulosic Material
The present invention provides methods and compositions for the conversion of plant biomass to fermentable sugars that can be converted to useful products. The methods include methods for degrading lignocellulosic material using enzyme mixtures to liberate sugars. The compositions of the invention include enzyme combinations that break down lignocellulose. The invention includes methods to identify the optimum ratios and compositions of enzymes with which to degrade each lignocellulosic material. These methods entail tests to identify the optimum enzyme composition and ratios for efficient conversion of any lignocellulosic substrate to its constituent sugars. While the multi-enzyme product may contain many types of enzymes, mixtures comprising enzymes that increase or enhance sugar release from biomass are preferred, including hemicellulases. The enzymes of the multi-enzyme product can be provided by a variety of sources. In one embodiment, the enzymes can be produced by a growing microorganism, especially a fungus, which produce the enzymes naturally or by virtue of being genetically modified to express the enzyme or enzymes.
Liquefaction Processes and Systems and Liquefaction Process Intermediate Compositions
IDR Improved HTL Bio-oil Separation by Gas Exsolvation (April 8, 2014) Prepared by: AJ Schmidt HTL Background and Importance of Bio-oil Separation Hydrothermal liquefaction is a conceptually simple process in which bio-oil is generated by heating biomass slurry to temperatures in the range of 300 to360 degrees C while the pressure is maintained above the vapor pressure of water (2000 to 3000 psig) to facilitate a condensed phase reaction medium. Compressed hot water has enhanced solvent properties that facilitate the formation of liquid oil products from biomass. HTL reactions involve fragmentation and condensation coupled with dehydration, decarbonylation, and decarboxylation. The major products are bio-oil, water with dissolved organics, gas (predominantly CO2), and solids (minerals and unconverted biomass). Challenges to the commercialization of HTL exist in the areas of pumping biomass slurries to high pressures, process heat integration, efficient separation of the bio-oil from the aqueous phase, and undesirable physico-chemical properties of the bio-oils such as high viscosity. To allow pumping to pressures of 3000 psig, the solids concentration of biomass slurries to the HTL process typically ranges from about 10 to 30 wt% (with the balance being water). Mass yields to bio-oil range from about 25 to 40 wt% (dry ash-free biomass basis). As an example, a 20 wt% slurry with a mass yield of 35% will produce an HTL product stream that is 7 wt% bio-oil with the balance consisting of an aqueous phase. For an economical HTL process, efficient separation of the bio-oil from the aqueous phase is critical. Current HTL Bio-oil/Water Separations Over the past 5 years, continuous bench-scale HTL testing has been conducted at PNNL with biomass slurries from agricultural residues (e.g. corn stover), forest residuals (e.g. pine), industrial/municipal sludges, and aquatic biomass sources (e.g. algae, kelp). While the bench-scale testing has been performed using continuous flow, product collection and bio-oil/water separations have been done batch-wise. For the test system, downstream of the HTL reactor, solids are removed; the product is collected in one of two alternating separators/collection vessels. The collection vessels facilitate degassing of the product, liquid/gas separation, and product collection at system pressure. When one collection vessel is full, it is valved offline and the product is diverted to the second collection vessel. The product in the valved-out collector is depressurized from 3000 psig to ambient pressure, and then removed. The removed product is settled under quiescent conditions, and the less polar bio-oil coalesces and separates from the aqueous phase. The bio-oil can then be recovered by decanting the aqueous phase (higher density bio-oil). When the bio-oil has a lower density then the aqueous phase, a separatory funnel is used. The gravity separation is a relatively slow process (10 to 60 minutes), and not efficient if oil emulsions form. While generally effective in a research setting, batch-wise gravity separation will present scale up challenges to pilot and commercial HTL applications. Invention Figure 1 provides an overview of the HTL configuration and shows the product collection vessels, which are bypassed in the subject invention. A more detailed sketch and an image of the invention in operation are shown in Figure 2. A continuous HTL bio-oil water separations process has been conceived and demonstrated in a proof of principle test with an algae feedstock (tetraselmis). For the invention, a biomass slurry feed is processed in an HTL reactor. The HTL product slurry is filtered (to remove solids/particulate) at HTL temperature and pressure (300 to 350 degrees C, at 2000 to 3000 psig). Next, the product is cooled to between 20 - 110 degrees C via heat exchange (40 degrees C in the test performed) and then flashed to atmospheric pressure. During the flashing, dissolved CO2 (which is more soluble in the bio-oil vs. the aqueous phase) exsolves and a bio-oil froth or foam is formed on top of the aqueous phase (see example, Figure 3). Nearly all of the produced bio-oil is present in the froth. With the proper use of float traps and expansion vessels, and effective separation of bio-oil is achieved. Figure 1. Continuous HTL System Configuration. Red dashed line show flow routing for invention (bypass of Jacketed Liquid Collections and Rapid Pressure letdown. Figure 2 Detailed schematic on rapid pressure letdown and bio-oil/water separation Figure 3Example of bio-oil foam formation during convention collection of product. The use of Bio-oil Separation via Gas Exsolvation Enhancement has advantages over other HTL bio-oil separations approach including the following: Increases HTL scalability: This invention eliminates labor intensive batch-wise, poorly scalable separation process. Eliminates batch-wise product collection and the need for high pressure nitrogen. In the current product collection approach, after emptying the product accumulator, it must be backfilled with nitrogen gas at 3000 psig to allow smooth transition when it is brought back on line (else, system pressure will drop and boiling will occur throughout the HTL reactor). Improves process safety. The liquid collection vessels represent the largest pressure vessels in the HTL system. Elimination of the need for these vessels significantly reduces the system volume at pressure. Increase quantity of oil recovered (speculative at this time) This invention takes advantage of the much higher solubility of CO2 in bio-oil vs. the aqueous phase. In a separation much like dissolved air flotation; the aqueous phase is essentially scrubbed of bio-oil constituents, which in turn are separated in a quasi-stable bio-oil foam. The foam is stable for a short time (15 sec to 2 minutes) and can be readily collapsed to a liquid. Keys Parameters for Implementation Effective/Efficient Solids Removal Before Flashing. Fine particulate will erode the pressure let down system (e.g., back pressure regulator), will promote emulsion formation, and will stabilize the bio-oil foam. Appropriate Geometry for Foam Routing and Foam Breaking. During flashing, the volume of bio-oil will expand by a factor of 10 to 50 (foaming). A route for this foam to separate from the liquid aqueous phase followed by a means to collapse the foam (e.g., condenser, demister pad) is essential for implementation of this approach (e.g. Figure 2). Potential enhancement: Flashing of product stream above 100C to enhance oil/organic recovery via steam stripping mechanism. Recycle of the gas stream (that exits the second float trap in Figure 2) back through the aqueous phase in the collector to promote additional oil separation/recovery. Attachments: Video 1: Video of separate bio-oil and aqueous collection (method demonstration). Video 2: Video of bio-oil foam during convention collection (while draining of bio-oil colllecter (Figure 1) at moderate pressure.
PROCESSES AND SYSTEMS FOR THE PRODUCTION OF PROPYLENE GLYCOL FROM GLYCEROL
Processes and systems for converting glycerol to propylene glycol are disclosed. The glycerol feed is diluted with propylene glycol as the primary solvent, rather than water which is typically used. The diluted glycerol feed is sent to a reactor where the glycerol is converted to propylene glycol (as well as other byproducts) in the presence of a catalyst. The propylene glycol-containing product from the reactor is recycled as a solvent for the glycerol feed.
CATALYTIC HYDROTHERMAL LIQUEFACTION FOR BIO-OIL PRODUCTION
Embodiments of a method for producing bio-oil include hydrothermal liquefaction of a biomass (e.g., a lignocellulosic biomass) feedstock to provide a process stream comprising crude oil and an aqueous fraction. The process stream is catalytically upgraded by contact with a sulfided-ruthenium catalyst, in the absence of added hydrogen, at a temperature and pressure effective to reduce an oxygen content of the crude oil, reduce a nitrogen content of the crude oil, reduce a total acid number of the crude oil, increase a H:C mole ratio of the crude oil, reduce a density of the crude oil, reduce a moisture content of the crude oil, reduce viscosity of the crude oil, or any combination thereof, thereby producing an upgraded oil and an upgraded aqueous fraction, which are subsequently separated. The catalytic upgrading process may be a plug-flow process and/or may be performed at or near liquefaction conditions.
METHODS AND SYSTEMS FOR FUEL PRODUCTION IN ELECTROCHEMICAL CELLS AND REACTORS
Methods and systems for fuel, chemical, and/or electricity production from electrochemical cells are disclosed. A voltage is applied between an anode and a cathode of an electrochemical cell. The anode includes a metal or metal oxide electrocatalyst. Oxygen is supplied to the cathode, producing oxygen ions. The anode electrocatalyst is at least partially oxidized by the oxygen ions transported through an electrolyte from the cathode to the anode. A feed gas stream is supplied to the anode electrocatalyst, which is converted to a liquid fuel. The anode electrocatalyst is re-oxidized to higher valency oxides, or a mixture of oxide phases, by supplying the oxygen ions to the anode. The re-oxidation by the ions is controlled or regulated by the amount of voltage applied.
WASTE MATERIAL ENCAPSULATION USING POLYMERIC MATERIALS (iEdison No. 0685901-22-0165)
A low-temperature encapsulation of iodine-loaded sorbents (getters) into polymer matrix was developed to address a need for an easily employed, reliable, and on-site production of durable waste forms. This invention is for the process and composition variation for a suit of low-temperature polymer matrices that have a high potential to encapsulate getters into durable waste forms. The method is based on mixing getters with polymer powder which is then followed by a low temperature encapsulation via uniaxial pressing or pressureless sintering at temperatures below 350?. Lab-scale conversion with a hot press produced fully densified products for 'Polymer matrix/Iodine-loaded Ag0-aerogel, 75/25 vol% fraction" with total iodine loadings of 16 mass% in the final waste form.
Device, Method and System for Improving Electrical Power factor and Harmonic Power Quality Through Active Control of Power Quality Improving Electrical Appliances
This patent teaches “power quality-improving appliances” (hereafter referred to as “PQI appliances™”), which are appliances that will counteract the aggregate power factor and harmonic pollution currents within a building to greatly reduce a building’s relative aggregate reactive power and harmonic pollution currents. The PQI appliances simultaneously serve their primary functions as water heaters, space heaters, thermoelectric heating or cooling, range top and oven cooking, for examples. The PQI appliance is therefore a novel application for mundane existing appliance types to improve distribution power system quality.
Decision Support Systems and Methods for Complex Networks
This invention is a method of advanced contingency analysis visualization for power grid operations. It converts the large volume of contingency analysis results to a visual space and presents the results as user-friendly color-contoured maps. This novel visualization method unloads overwhelmed power grid operators from examining raw data and enables them to focus on critical portions of the grid and respond to adverse situations in a timely manner. The major point of novelty of this invention is the visual representation of the analysis results of multiple contingencies, which has not been done in the area of power grid operations. Geographical information is readily included in the visualization techniques. Another point of novelty is the quantitative assessment of risks. Comprehensive analysis of the contingency analysis results is performed and risk indices are derived. This quantitative risk assessment is not available in today’s tool. The developed visualization and analysis reveals the vulnerability of the power grid which otherwise would be buried in the pages and pages of tabular entries.