# US 8,771,387 B2 · Systems and methods for solar-thermal gasification of biomass

> Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt

- Number: US 8,771,387 B2
- Document ID: US8771387B2
- Status: Granted
- Kind: B2
- Application number: 12/796,045
- Filed: 2010-06-08
- Published: 2010-09-23
- Granted: 2014-07-08
- Earliest claimed: 2009-06-09
- Assignees: Sundrop Fuels, Inc.
- Applicants: Wayne Simmons; Christopher Perkins; Zoran Jovanovic
- Inventors: Wayne Simmons; Christopher Perkins; Zoran Jovanovic
- Web page: https://patentgrep.com/patent/US8771387B2

## CPC

- C01B 3/384: with external heating of the catalyst
- B01J 19/0013: {Controlling the temperature of the process}
- B01J 19/0033: {Optimalisation processes, i.e. processes with adaptive control systems (adaptive control systems per se G05B13/00)}
- B01J 19/2445: {placed in parallel}
- B01J 19/245: {placed in series}
- C01B 3/22: by decomposition of gaseous or liquid organic compounds
- C01B 3/34: by reaction of hydrocarbons with gasifying agents
- C07C 29/15: by reduction of oxides of carbon exclusively
- C07C 29/1518: {one step being the formation of initial mixture of carbon oxides and hydrogen for synthesis}
- C10G 2/30: {from carbon monoxide with hydrogen}
- C10G 2/32: {with the use of catalysts}
- C10G 3/00: Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids (production from non-melting solid oxygen-containing carbonaceous materials C10G1/00)
- C10J 3/00: Production of combustible gases containing carbon monoxide from solid carbonaceous fuels (destructive distillation processes C10B)
- C10J 3/466: {Entrained flow processes}
- C10J 3/482: {Gasifiers with stationary fluidised bed}
- C10J 3/485: {Entrained flow gasifiers}
- C10J 3/506: {for entrained flow gasifiers}
- C10J 3/54: Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J 3/56: Apparatus; Plants
- C10J 3/58: combined with pre-distillation of the fuel
- C10J 3/60: Processes
- C10J 3/62: with separate withdrawal of the distillation products
- C10J 3/721: {Multistage gasification, e.g. plural parallel or serial gasification stages}
- C10J 3/723: {Controlling or regulating the gasification process}
- C10J 3/82: Gas withdrawal means
- C10J 3/84: with means for removing dust or tar from the gas
- C10K 1/024: {by filtration}
- C10L 1/04: essentially based on blends of hydrocarbons
- F24S 20/20: Solar heat collectors for receiving concentrated solar energy, e.g. receivers for solar power plants
- B01J 2219/00117: with two or more reactions in heat exchange with each other, such as an endothermic reaction in heat exchange with an exothermic reaction
- B01J 2219/00186: controlling the composition of the reactive mixture
- C01B 2203/0216: containing a non-catalytic steam reforming step
- C01B 2203/0233: the reforming step being a steam reforming step
- C01B 2203/061: Methanol production
- C01B 2203/0811: by combustion of fuel
- C01B 2203/1241: Natural gas or methane
- C01B 2203/1685: Control based on demand of downstream process
- C01B 2203/84: Energy production
- C10G 2300/1014: of vegetal origin
- C10G 2300/1025: Natural gas
- C10G 2300/807: Steam
- C10J 2200/09: Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
- C10J 2200/15: Details of feeding means
- C10J 2200/158: Screws
- C10J 2300/0906: Physical processes, e.g. shredding, comminuting, chopping, sorting
- C10J 2300/0909: Drying
- C10J 2300/0916: Biomass
- C10J 2300/094: Char
- C10J 2300/0973: Water
- C10J 2300/0976: as steam
- C10J 2300/0989: Hydrocarbons as additives to gasifying agents to improve caloric properties
- C10J 2300/0993: Inert particles, e.g. as heat exchange medium in a fluidized or moving bed, heat carriers, sand
- C10J 2300/1223: by burners
- C10J 2300/123: by electromagnetic waves, e.g. microwaves
- C10J 2300/1284: by renewable energy, e.g. solar energy, photovoltaic cells, wind
- C10J 2300/1292: mSolar energy
- C10J 2300/1621: Compression of synthesis gas
- C10J 2300/1659: to liquid hydrocarbons
- C10J 2300/1665: to alcohols, e.g. methanol or ethanol
- C10J 2300/1693: with storage facilities for intermediate, feed and/or product
- C10J 2300/1853: Steam reforming, i.e. injection of steam only
- C10J 2300/1861: Heat exchange between at least two process streams
- C10L 2200/0492: Fischer-Tropsch products
- C10L 2290/02: Combustion or pyrolysis
- C10L 2290/04: Gasification
- C10L 2290/06: Heat exchange, direct or indirect
- C10L 2290/08: Drying or removing water
- C10L 2290/28: Cutting, disintegrating, shredding or grinding
- C10L 2290/42: Fischer-Tropsch steps
- C10L 2290/50: Screws or pistons for moving along solids
- C10L 2290/52: Hoppers
- C10L 2290/547: Filtration for separating fractions, components or impurities during preparation or upgrading of a fuel
- Y02B 40/18: using renewables, e.g. solar cooking stoves, furnaces or solar heating
- Y02E 10/40: Solar thermal energy, e.g. solar towers
- Y02E 50/10: Biofuels, e.g. bio-diesel
- Y02E 50/30: Fuel from waste, e.g. synthetic alcohol or diesel
- Y02P 20/129: Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
- Y02P 20/133: Renewable energy sources, e.g. sunlight
- Y02P 20/145: the feedstock being materials of biological origin
- Y02P 20/50: Improvements relating to the production of bulk chemicals
- Y02P 30/20: using bio-feedstock
- Y02T 50/678: Aviation using fuels of non-fossil origin
- C01B: NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; {METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C}
- B01J: CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- C07C: ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C10G: CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION (cracking to hydrogen or synthesis gas C01B; cracking or pyrolysis of hydrocarbon gases to individual hydrocarbons or mixtures thereof of definite or specified constitution C07C; cracking to cokes C10B); RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10J: PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES (synthesis gas from liquid or gaseous hydrocarbons C01B; underground gasification of minerals E21B43/295); CARBURETTING AIR OR OTHER GASES
- C10K: PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10L: FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
- F24S: SOLAR HEAT COLLECTORS; SOLAR HEAT SYSTEMS (for producing mechanical power from solar energy F03G6/00)
- Y02B: CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02E: REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02P: CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02T: CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION

## Abstract

A method, apparatus, and system for a solar-driven chemical plant that may include a solar thermal receiver having a cavity with an inner wall, where the solar thermal receiver is aligned to absorb concentrated solar energy from one or more of 1) an array of heliostats, 2) solar concentrating dishes, and 3) any combination of the two. Some embodiments may include a solar-driven chemical reactor having multiple reactor tubes located inside the cavity of solar thermal receiver, wherein a chemical reaction driven by radiant heat occurs in the multiple reactor tubes, and wherein particles of biomass are gasified in the presence of a steam (H2O) carrier gas and methane (CH4) in a simultaneous steam reformation and steam biomass gasification reaction to produce reaction products that include hydrogen and carbon monoxide gas using the solar thermal energy from the absorbed concentrated solar energy in the multiple reactor tubes.

## Claims

### Claim 1

A chemical reactor driven by radiant heat with an exit temperature of product gases greater than 900 degrees C., comprising:
a radiant heat-driven chemical reactor having multiple reactor tubes located inside a cavity of a thermal receiver configured to gasify particles of biomass in a presence of steam (H2O) to produce a low CO2 synthesis gas that includes hydrogen, carbon monoxide gas, and less than 7% CO2 by total volume generated in a gasification reaction of the particles of biomass using thermal energy from the radiant heat, where the chemical reactor is in fluid communication with a source of the steam, wherein the multiple reactor tubes and the thermal receiver are configured to cooperate such that heat is radiantly transferred to the particles of biomass in order to provide enough energy required for the gasification reaction of the particles of biomass to drive the gasification reaction primarily with radiant heat to produce the low CO2 synthesis gas;
a steam reformer in fluid communication with a source of methane-based gas, where the steam reformer is configured to produce reformate that includes hydrogen and carbon monoxide gas;
a mixer in fluid communication with the chemical reactor and steam reformer that is configured for mixing of the reformate and biomass gasification products to produce a combined low CO2 synthesis gas having a molar H2:CO ratio of between 2.0-3.0, as well as eliminates any need for a component downstream of the chemical reactor to perform a water-gas-shift reaction;
an on-site fuel synthesis reactor in fluid communication with an outlet of the mixer;
a lock hopper containing the particles of biomass; and
a splitting device configured to supply the particles of biomass from the lock hopper to two or more feed lines in an entrained-flow biomass feed system, wherein the entrained-flow biomass feed system is configured to use an entrainment carrier gas to move the particles of biomass into the radiant heat driven chemical reactor, where the two or more feed lines are configured to supply the particles of biomass having an average smallest dimension the particles of equal to or less than 2000 um to the chemical reactor.

### Claim 2 (depends on 1)

The chemical reactor of claim 1, wherein the thermal receiver has cavity walls and is aligned to absorb energy from a heat source.

### Claim 3 (depends on 2)

The chemical reactor of claim 2, where the radiant heat-driven chemical reactor is configured for the particles of biomass to be gasified simultaneously with the methane-based gas undergoing steam reformation in the same chemical reactor, wherein the steam reacts with both the particles of biomass and the methane-based gas, but the biomass and methane-based gas do not react with each other, and wherein a steam (H2O) to carbon molar ratio is in a range of 1:1 to 1:4, wherein the radiant heat-driven chemical reactor has a downdraft geometry with the multiple reactor tubes in a vertical orientation that are located inside the thermal receiver, and wherein the chemical reactor is configured to convert carbonaceous biomass materials into the carbon monoxide and hydrogen by reacting the particles of biomass with the steam in a biomass gasification reaction and the steam with the methane-based gas at high temperatures, 700-1500 degrees C., which then results in the combined low CO2 synthesis gas.

### Claim 4 (depends on 2)

The chemical reactor of claim 2,
where the thermal receiver is configured to gasify the particles of biomass simultaneously with the methane undergoing steam reformation in the same chemical reactor, wherein the methane comes from natural gas, and the particles of biomass and the natural gas are co-fed with heated steam to dry reform the methane with CO2 either contained within the natural gas or fed as a separate feedstock, such that even if some CO2 is present in the natural gas, consisting mainly of methane, the CO2 and CH4 react using a high heat of 750-1300 degrees C. via dry reforming to produce the hydrogen and carbon monoxide, and
wherein the particles of biomass and the methane are co-fed with the steam at the temperature ranges of 750-1300 degrees C. in stoichiometric proportions to produce a molar ratio of H2:CO in a range from 1.0 to 3.0.

### Claim 5 (depends on 1)

The chemical reactor of claim 1, wherein the thermal receiver is configured to support a steam reforming process at a temperature of 700-1500 degrees C. such that the water-gas-shift reaction that is equilibrium favored at lower temperatures is avoided, and thus prevents extra CO2 creation from the water-gas-shift reaction, where the steam reformer is configured to perform the reaction using the methane-based gas with a steam reforming reaction which allows the gasification reaction in the chemical reactor to generate a desired molar ratio for liquid fuels and chemical synthesis without the water-gas-shift reaction.

### Claim 6 (depends on 1)

The chemical reactor of claim 1, wherein the multiple reactor tubes and thermal receiver are configured to cooperate such that heat is radiantly transferred to the particles of biomass in order for a combination of i) the particles of biomass having the average smallest dimension of equal to or less than 2000 um to the chemical reactor, ii) an operating temperature of the chemical reactor greater than 1100 degrees C. supplied by a heat source, and iii) the thermal energy primarily being driven by the radiant heat to produce the low CO2 synthesis gas at an outlet of the chemical reaction having a substantial tar destruction to less than below 50 mg/m^3 in the reaction products that include the hydrogen and carbon monoxide gas, wherein tar formation is mitigated at an approximately 1100-1300 degrees C. operating temperature.

### Claim 7 (depends on 1)

The chemical reactor of claim 1,
wherein the multiple reactor tubes are made of materials that are oxidation resistant and steam resistant; and
wherein the reformate has a 3:1 H2:CO ratio and the biomass gasification products have a 1:1 H2:CO ratio, so less biomass is needed to achieve a syngas product with an approximate 2.1-2.8:1H2:CO ratio that is appropriate for liquid fuels and chemical synthesis than if the particles of biomass were gasified without the methane-based gas.

### Claim 8 (depends on 4)

The chemical reactor of claim 4, wherein within the multiple reactor tubes the methane-based gas is co-fed with the particles of biomass such that the particles of biomass facilitate a radiation heat transfer to raise a temperature in the multiple reactor tubes to a level to reform the methane and cause a biomass gasification reaction such that the steam reforming of the methane and the dry reforming of the methane is combined with the biomass gasification reaction; and
wherein the energy from a heat source is transferred to walls of the thermal receiver and walls of the multiple reactor tubes such that heat is radiantly transferred to the particles of biomass, and then the particles of biomass transfer the heat effectively to the methane and steam molecules.

### Claim 9 (depends on 1)

The chemical reactor of claim 1,
wherein the entrained-flow biomass feed system is configured to use the entrainment carrier gas comprising natural gas, steam, air, and/or any combination of these and to supply a variety of sources of biomass feedstock fed as particles into the radiant heat-driven chemical reactor;
wherein the particle size distribution of the biomass feedstock has a general range of between 500 um and 1000 um; and a use of a simple multiple reactor tube design with radiant heat driving the biomass gasification reaction allows the process to be feedstock flexible, with no major equipment redesign required to change feedstocks; and
wherein the variety of sources includes two or more types of biomass that can be fed, individually or in combinational mixtures, from the group consisting of cellulose, lignin, forestry wastes and forestry thinnings, by controlling particle size of the stock biomass feedstock and operating temperature range of the multiple reactor tubes.

### Claim 10 (depends on 2)

The chemical reactor of claim 2, further comprising:
a control system configured to control the thermal receiver temperature by factoring a biomass feed rate against available energy from the heat source such that the temperature in the thermal receiver is maintained at a desired setpoint in the range of 800-1600 degrees C. by a balance of energy consumed by the gasification reaction and reactant/product sensible heat, and thermal losses from the thermal receiver by radiation, convection and/or conduction; and
wherein the control system 1) keeps the temperature high enough (1000-1300 degrees C. in the chemical reactor) for a substantially entire conversion of the particles of biomass to product gases and an elimination of tar products to a concentration of less than 200 mg/m^3, and 2) keeps the temperature in the chemical reactor low enough (<1600 degrees C.) for walls of the multiple reactor tubes to not structurally weaken or significantly reduce thermal receiver efficiency.

### Claim 11 (depends on 1)

The chemical reactor of claim 1, wherein the on-site fuel synthesis fuel reactor has a supply input to receive the combined low CO2 syngas containing the hydrogen molecules and carbon monoxide molecules from the radiant heat-driven chemical reactor, where the on-site fuel synthesis fuel reactor is configured to use the syngas in a hydrocarbon fuel synthesis process which is catalytically reformed to produce chemicals.

### Claim 12

A radiant heat-driven reactor located inside a receiver, comprising:
a cavity that transforms radiant energy into thermal energy, where the receiver encloses multiple reactor tubes of the radiant heat-driven reactor, and the reactor tubes are configured for reactant gases consisting of 1) methane, 2) natural gas, 3) steam, or 4) any combination of the three to pass through a heat transfer aid configured to cause a steam methane reaction using the thermal energy from the radiant energy;
wherein the heat transfer aid is configured to heat the reactant gases, where the heat transfer aid is one or more of the following located inside each reactor tube: a fluidized bed of inert particles, a reticulate porous ceramic (RPC) foam, a ceramic monolith, ceramic tubes or aerogels, open structured packed rings including Raschig rings, gauze or wire constructed of a high temperature-resistant material, and any combination of these; and
wherein radiation is a primary mode of heat transfer to the heat transfer aids from the walls of the reactor tubes, and conduction, convection, or some combination of the two is a secondary mode of heat transfer.

### Claim 13 (depends on 12)

The radiant heat-driven reactor of claim 12, further comprising:
a moving bed of carbonaceous feedstock through which a gasification agent flows in a co-current or counter-current configuration to achieve gasification and the moving bed is heated with the thermal energy.

### Claim 14 (depends on 12)

The radiant heat-driven reactor of claim 12, further comprising:
a source of the methane in fluid communication with the radiant heat-driven reactor;
a source of biomass in fluid communication with the radiant heat-driven reactor; and
a first reactor tube that is a graphite reaction tube with an external SiC coating configured to operate at up to 1500 degrees C., wherein the radiant heat-driven reactor is configured to add the methane to the biomass such that the energy requirement of the radiant heat-driven reactor to produce an equivalent amount of syngas is lower, and the biomass is gasified at a high enough temperature using a heated transport tube reactor, such that tar formation is substantially reduced to less than 200 mg/m^3.

### Claim 15 (depends on 12)

The radiant heat-driven reactor of claim 12, further comprising:
a source of the natural gas in fluid communication with the radiant heat-driven reactor; and
one or more high temperature oxidizers configured to oxidize the natural gas such that the radiant heat-driven reactor produces 5% to 10% of a high H2syngas (>2:1 H2:CO ratio) on demand that is combined with syngas from a biomass gasification reaction such that the high H2 syngas is used to raise an amount of H2 present in the combined syngas to a desired H2:CO ratio.