Biogenic activated carbon and methods of making and using same - Patent Application 20070122997

Abstract

To provide a biogenic activated carbon.SOLUTION: There is provided a biogenic activated carbon composition comprising, on a dry basis, about 55 wt.% or more total carbon, about 15 wt.% or less hydrogen, and about 1 wt.% or less nitrogen. The activated carbon composition is characterized by an Iodine Number higher than about 500, and optionally the composition is responsive to an externally applied magnetic field. There is also provided a biogenic activated carbon composition comprising, on a dry basis, about 55 wt.% or more total carbon, about 15 wt.% or less hydrogen, and about 1 wt.% or less nitrogen. The activated carbon composition is characterized by an Iodine Number higher than about 500, and optionally at least a portion of the carbon is present in the form of graphene.SELECTED DRAWING: Figure 31

Description

[Technical Field]

[0001] Priority claims This international patent application is a continuation of U.S. Provisional Patent Application No. 61 / 643,741, filed May 7, 2012. No. 61 / 721,827, filed November 2, 2012; and U.S. Provisional Patent Application No. 20 / 2013,424, filed November 2, 2013. This application claims the benefit of priority from U.S. Provisional Patent Application No. 61 / 737,514, filed December 14, 2012. No. 6,299,499, each of which is incorporated herein by reference in its entirety.

[0002] The present disclosure generally relates to processes, systems, and apparatus for the production of biogenic activated carbon. , relates to biogenic activated carbon and uses of biogenic activated carbon, including emission control. [Background technology]

[0003] Activated carbon was first produced commercially in the early 20th century, initially to decolorize sugars, and later It was used to remove taste and odor from water. Granular activated carbon was first used for gas masks. developed and later used for various additional purposes such as solvent recovery and air purification. The processes for producing activated carbon generally require large energy inputs and have low yields. Many processes involve the pyrolysis of carbonaceous raw materials followed by the activation of the pyrolysis solids. Pyrolysis typically involves two distinct steps: decomposition and decomposition. Activation involves the direct heating of a carbonaceous substrate in an oxygen environment. It involves the application of steam or carbon dioxide to increase the area. Summary of the Invention

[0004] In one embodiment, the present disclosure provides a cellulose fiber having a total carbon content of about 55% by weight or more, about 15% by weight or more, on a dry basis. providing a biogenic activated carbon composition comprising about 1% by weight or less of hydrogen and about 1% by weight or less of nitrogen; The aforementioned activated carbon composition has an Iodine Number greater than about 500. Optionally, the composition is responsive to an externally applied magnetic field.

[0005] In another embodiment, the present disclosure provides a cellulose fiber having, on a dry basis, about 55% by weight or more total carbon, about 15% by weight or more total carbon, and about 1% by weight or less of hydrogen and about 1% by weight or less of nitrogen. The activated carbon composition is characterized by an iodine value greater than about 500, and optionally, the activated carbon At least a portion of the carbon nanotubes is present in the form of graphene.

[0006] In another embodiment, the present disclosure provides a cellulose fiber having, on a dry basis, about 55% by weight or more total carbon, about 15% by weight or more total carbon, % or less by weight of hydrogen, about 1% or less by weight of nitrogen, and about 0.0001% to about 5% by weight of A biogenic activated carbon composition is provided that includes iron, wherein at least a portion of the carbon is selected from the group consisting of graphene, and the activated carbon composition is characterized by an iodine value greater than about 500, The composition responds to an externally applied magnetic field.

[0007] In another embodiment, the present disclosure provides a cellulose fiber having, on a dry basis, about 55% by weight or more total carbon, about 15% by weight or more total carbon, % or less by weight of hydrogen, about 1% or less by weight of nitrogen, and about 0.1% to about 5% by weight of iron. The present invention provides a biogenic activated carbon composition comprising an iodine content greater than about 500. The composition is characterized by a valence and is responsive to an externally applied magnetic field.

[0008] In another embodiment, the present disclosure provides a cellulose fiber having, on a dry basis, about 55% by weight or more total carbon, about 15% by weight or more total carbon, and about 1% by weight or less of hydrogen and about 1% by weight or less of nitrogen. The activated carbon composition is characterized by an iodine value greater than about 500, and the activated carbon composition is characterized by an iodine value greater than about 500. Some of them exist in the form of graphene.

[0009] In another embodiment, the present disclosure provides a biobased iodine-containing product characterized by an iodine value greater than about 500. The present invention provides a graphene-containing product.

[0010] In another embodiment, the present disclosure provides a composition comprising graphene, The carbon, on a dry basis, is greater than or equal to about 55% by weight total carbon, less than or equal to about 15% by weight hydrogen, and less than or equal to about 1 % by weight or less of nitrogen, and at least a portion of said carbon is derived from a biogenic activated carbon composition. exists in the form of graphene.

[0011] In another embodiment, the present disclosure provides a continuous process for producing biogenic activated carbon. The process includes: (a) providing a carbon-containing feedstock comprising biomass; (b) optionally drying said feedstock to remove at least a portion of the moisture from said feedstock; and (c) removing said feed in one or more indirectly heated reaction zones. The feedstock is mixed with a vapor stream containing a substantially inert gas and at least one of water or carbon dioxide. and an activator containing the solid, condensable vapor, and non-condensable vapor in countercurrent mechanical contact with the and generating a condensable gas (said condensable vapor and said non-condensable gas are said vapor streams). (d) removing at least a portion of said vapor stream from said reaction zone to separate (e) generating a separated steam stream or a thermally treated steam stream thereof; and / or by adding at least a portion of the resulting mixture to the feedstock prior to step (c). (f) recycling the activated carbon to the gas inlet of the reaction zone(s) described above; and recovering at least a portion of said solids from said reaction zone(s) by

[0012] In another embodiment, the present disclosure provides a continuous process for producing biogenic activated carbon. The process includes: (a) providing a carbon-containing starting feedstock comprising biomass; and (b) optionally drying said carbon-containing feedstock to remove at least part of the moisture therefrom. (c) removing a portion of said feed in one or more indirectly heated reaction zones. The feedstock is mechanically conveyed and the feedstock is mixed with a steam stream containing a substantially inert gas and water. or carbon dioxide in countercurrent contact with an activator comprising a solid, generating condensable vapors and non-condensable gases (including the aforementioned condensable vapors and the aforementioned non-condensable gases) (d) removing at least one of said vapor streams from said reaction zone; (e) removing a portion of the carbon-containing slag from an external source to generate a separated vapor stream; a liquid or vapor stream to said feedstock prior to step (c) and / or to said reaction (f) introducing into the gas inlet of the zone(s) a biogenic activated carbon as described above. and recovering at least a portion of said solids from the zone(s).

[0013] In another embodiment, the present disclosure provides a method for producing graphene-containing biogenic activated carbon. a continuous process for producing a carbon-containing starting feed comprising: (a) a carbon-containing starting feed comprising biomass; (b) optionally drying said carbon-containing feedstock to produce said carbon-containing feedstock; (c) removing at least a portion of the moisture from the containing feedstock; and (d) using one or more indirectly reacting In a heated reaction zone, the feedstock is mechanically conveyed to substantially a vapor stream containing an essentially inert gas and at least one of water or carbon dioxide; Countercurrently contacting the activated carbon with an activator to generate solids, condensable vapors, and non-condensable gases. and (said condensable vapor and said non-condensable gas enter said vapor stream); (d) said removing at least a portion of said vapor stream from said reaction zone to generate a separated vapor stream. (e) removing at least one of said separated vapor streams or a thermally treated form thereof; a portion of which is added to said feedstock prior to step (c) and / or to said reaction zone(s). (f) recycling said solids from said reaction zone(s) to said gas inlet of said reaction zone(s). and recovering at least a portion of the solid, wherein the solid is a graphene-containing biogenic active material. Contains charcoal.

[0014] In another embodiment, the present disclosure provides a method for producing graphene-containing biogenic activated carbon. a continuous process for producing a carbon-containing starting feed comprising: (a) a carbon-containing starting feed comprising biomass; (b) optionally drying said carbon-containing feedstock to form said feedstock; (c) removing at least a portion of the moisture from the raw material; and (d) using one or more indirectly heated In the reaction zone, the feedstock is mechanically conveyed and the feedstock is substantially inert. a vapor stream containing an activating gas and an activating agent containing at least one of water or carbon dioxide; and (iii) generating solids, condensable vapors, and non-condensable gases. (d) said reaction zone; (e) said condensable vapor and said noncondensable gas entering said vapor stream; removing at least a portion of said vapor stream from the region to generate a separated vapor stream; (e) transferring at least a portion of said separated vapor stream or a thermally treated form thereof to to said feedstock and / or to the gases of said reaction zone(s) prior to step (c). (f) biogenic carbon, which is recycled to the inlet to increase the surface area of ​​the carbon in said solid; recovering at least a portion of said solids from said reaction zone(s) as activated carbon; and wherein the biogenic activated carbon comprises, on a dry basis, about 55% by weight or more of total carbon, about 15% by weight or less of hydrogen and about 1% by weight or less of nitrogen, and At least a portion of the carbon is present in the form of graphene, and the biogenic activated carbon composition has a carbon content of about 5 The aforementioned biogenic activated carbon is characterized by an iodine value higher than 0.00 and is not susceptible to externally applied magnetic fields. Respond to the situation.

[0015] In another embodiment, the present disclosure provides a method for reducing at least one contaminant from a gas phase exhaust stream. and (a) removing at least one contaminant from a sample. (b) providing a gas-phase effluent stream containing an additive and a biogenic active ingredient; and (c) treating the gas-phase effluent stream with the additive and a biogenic active ingredient. (c) contacting the activated carbon particles with the activated carbon composition to generate contaminant-adsorbing particles; Separating at least a portion of said contaminant-adsorbed particles from said gas-phase effluent stream to reduce contaminants. and producing a small gas-phase exhaust stream.

[0016] In another embodiment, the present disclosure provides a method for reducing mercury emissions using a biogenic activated carbon composition. The method includes the steps of: (a) providing a gas phase effluent stream containing mercury; b) transferring the gas phase effluent stream to an activated carbon containing biogenic activated carbon composition comprising iron or an iron-containing compound; (c) contacting the mercury-adsorbed carbon particles with the mercury-adsorbed carbon particles; and (d) using electrostatic precipitation to obtain the mercury-adsorbed carbon particles. separating at least a portion of said mercury-adsorbed carbon particles from said gas-phase effluent stream to reduce mercury; and producing a gas-phase exhaust stream.

[0017] In another embodiment, the present disclosure provides a process for producing energy, comprising: (a) providing a carbon-containing feedstock comprising a biogenic activated carbon composition; and (b) converting said carbon into a carbon-containing feedstock. and oxidizing a nitrogen-containing feedstock to produce a gas phase exhaust containing energy and at least one pollutant. and generating a stream, wherein the biogenic activated carbon composition is capable of removing at least one contaminant. At least a part of the object is adsorbed.

[0018] In another embodiment, the present disclosure provides a method for purifying a liquid using a biogenic activated carbon composition. The present invention provides a method for detecting a contaminant in a liquid, the method comprising: (a) providing a liquid containing at least one contaminant; (b) contacting said liquid with activated carbon particles comprising an additive and a biogenic activated carbon composition. and generating contaminant-adsorbed carbon particles and a contaminant-reduced liquid.

[0019] In another embodiment, the present disclosure provides a method for removing at least a portion of sulfur contaminants from a liquid. The method includes: (a) providing a liquid containing sulfur contaminants; (b) removing the sulfur contaminants from the liquid; contacting the liquid with activated carbon particles comprising an additive and a biogenic activated carbon composition. and after step (b), at least a portion of the activated carbon particles contain sulfur contaminants.

[0020] In another embodiment, the present disclosure provides a process for reducing the concentration of sulfate in water. The process comprises: (a) providing a volume or stream of water containing sulfate; and (b) contacting the water with activated carbon particles comprising an additive and a biogenic activated carbon composition. nothing.

[0021] In another embodiment, the present disclosure provides a method for removing sulfur contaminants from a gas-phase exhaust stream. The method further comprises: (a) providing a gas-phase effluent stream containing at least one sulfur contaminant; and (b) treating the gas-phase exhaust stream with activated carbon particles comprising the additive and the biogenic activated carbon composition. (c) contacting said activated carbon particles from said gas phase effluent stream after step (b). and separating at least a portion of the

[0022] In another embodiment, the present disclosure provides a method for reducing one or more contaminants from a gas or liquid. The present invention provides a method for removing or contaminating a gas containing one or more contaminants, the method comprising: (a) removing a gas containing one or more contaminants; (b) providing a gas or liquid stream; and (b) dissolving said gas or liquid stream in a solution of about 1000 ppm or less on a dry basis. 55% by weight or more total carbon, about 15% by weight or less hydrogen, and about 1% by weight or less nitrogen; and contacting the activated carbon composition with a biogenic activated carbon composition having an iodine value of at least about 500. wherein the composition is responsive to an externally applied magnetic field.

[0023] In another embodiment, the present disclosure provides a method for reducing one or more contaminants from a gas or liquid. The present invention provides a method for removing or contaminating a gas containing one or more contaminants, the method comprising: (a) removing a gas containing one or more contaminants; (b) providing a gas or liquid stream; and (b) dissolving said gas or liquid stream in a solution of about 1000 ppm or less on a dry basis. 55% by weight or more total carbon, about 15% by weight or less hydrogen, and about 1% by weight or less nitrogen; and contacting the activated carbon composition with a biogenic activated carbon composition having an iodine value of at least about 500. wherein at least a portion of said carbon is present in the form of graphene.

[0024] In another embodiment, the present disclosure provides a method for reducing contaminants from a liquid or gas, or The present invention provides a method for removing carbon dioxide particles, the method comprising: (a) removing, on a dry basis, at least about 55% by weight of total carbon dioxide particles; , about 15% by weight or less of hydrogen, and about 1% by weight or less of nitrogen. (b) obtaining any of the carbon atoms, wherein at least a portion of said carbon atoms is present in the form of graphene; (c) isolating said graphene from said biogenic activated carbon composition; and The liquid or gas may be separated or combined with a portion of the biogenic activated carbon composition. and contacting the graphene.

[0025] In another embodiment, the present disclosure provides a method of using graphene, said method comprising: (a) on a dry basis, about 55% by weight or more total carbon, about 15% by weight or less hydrogen, and about Obtaining a biogenic activated carbon composition containing 1% by weight or less of nitrogen (at least one of said carbons) (b) optionally, a biogenic activated carbon composition as described above, wherein the activated carbon is present in part in the form of graphene; (c) separating said graphene from adhesives, sealants, coatings, paints, inks, Composite materials, catalysts, catalyst supports, battery electrodes, fuel cell electrodes, graphene-based circuits or memory systems, energy storage materials or devices, supercapacitors, electrostatic Dissipative sinks, materials or devices for electron or ion transport, high bandwidth communication systems , infrared sensors, chemical sensors, biological sensors, electronic displays, voltaic cells, or in graphene aerogel, in isolated form, or in the aforementioned biogenic activated carbon composition. The present invention also includes using graphene as a part of the above. [Brief explanation of the drawings]

[0026] [Figure 1] 1 illustrates a multi-reactor embodiment of the system of the present disclosure.

[0027] [Figure 2] 1 illustrates a single reactor, multi-zone embodiment of the system of the present disclosure.

[0028] [Figure 3] 1 illustrates one embodiment of a zero oxygen continuous feed mechanism suitable for use in connection with the present disclosure.

[0029] [Figure 4] 1 illustrates another embodiment of a single reactor, multi-zone biomass processing unit suitable for use in connection with the present disclosure.

[0030] [Figure 5] 1 illustrates one embodiment of a carbon recovery unit suitable for use in connection with the present disclosure.

[0031] [Figure 6] 1 shows an embodiment of one embodiment of a single reactor biomass processing unit of the present disclosure, optionally with a dryer.

[0032] [Figure 7] 1 illustrates an embodiment of a pyrolysis reactor system of the present disclosure, optionally with a dryer and gas inlet.

[0033] [Figure 8] 1 shows an embodiment of a single reactor biomass processing unit of the present disclosure with a gas inlet and optionally a cooler.

[0034] [Figure 9] 1 shows an embodiment of a single reactor biomass processing unit system of the present disclosure, optionally with a dryer and deaerator, and an inert gas inlet.

[0035] [Figure 10]1 shows an embodiment of a multi-reactor system of the present disclosure, optionally with a dryer and degasifier, and an inert gas inlet.

[0036] [Figure 11] 1 illustrates an embodiment of a multi-reactor system of the present disclosure, optionally with a dryer and cooler, and a material concentration unit.

[0037] [Figure 12] 1 shows an embodiment of a multi-reactor system of the present disclosure, optionally with a dryer, degasser, cooler, and inert gas inlet.

[0038] [Figure 13] 1 shows an embodiment of a multi-reactor system of the present disclosure, optionally with a dryer and degasifier, an inert gas inlet, and a cooler.

[0039] [Figure 14] 1 shows the dispersion of magnetic particles in biogenic activated carbon according to the present disclosure.

[0040] [Figure 15] 1 shows biogenic activated carbon with an iron halide additive prepared according to the present disclosure attracted to a magnet.

[0041] [Figure 16] 1 shows the change in gas component concentration over time when passed through a plug of biogenic activated carbon according to the present disclosure.

[0042] [Figure 17] 1 shows carbon dioxide adsorption over time for a plug of biogenic activated carbon according to the present disclosure.

[0043] [Figure 18] 1 shows a graph illustrating the effect of retention time on fixed carbon content of a biogenic activated carbon product produced according to one embodiment of the present disclosure.

[0044] [Figure 19]1 shows a graph illustrating the effect of pyrolysis temperature on fixed carbon content of a biogenic activated carbon product produced according to one embodiment of the present disclosure.

[0045] [Figure 20] 1 shows a graph illustrating the effect of biomass particle size on fixed carbon content of a biogenic activated carbon product produced according to one embodiment of the present disclosure.

[0046] [Figure 21] 1 illustrates an embodiment of a single reactor biomass processing unit of the present disclosure for producing biogenic activated carbon.

[0047] [Figure 22] 1 illustrates an embodiment of a two-reactor biomass processing unit of the present disclosure for producing biogenic activated carbon.

[0048] [Figure 23] 1 is a transmission electron micrograph of an exemplary activated carbon having an iodine number of 2029. The dark curved areas are graphene crystallites.

[0049] [Figure 24] 1 is a transmission electron micrograph of an exemplary activated carbon having an iodine number of 2029. The dark curved areas are graphene crystallites.

[0050] [Figure 25] A transmission electron micrograph of activated carbon with an iodine number of 2029. The parallel lines across the image are atomically thin layers of graphene.

[0051] [Figure 26] 1 is a transmission electron micrograph of activated carbon with an iodine number of 2029. The dark curved areas are graphene crystallites.

[0052] [Figure 27]A transmission electron micrograph of activated carbon with an iodine number of 716. The parallel lines across the image are atomically thin layers of graphene.

[0053] [Figure 28] A transmission electron micrograph of activated carbon with an iodine number of 716. The parallel lines across the image are atomically thin layers of graphene within the graphite.

[0054] [Figure 29] This is a transmission electron micrograph of activated carbon with an iodine number of 716. The roughly square object in the bottom center is a reduced version of Figure 28. The lighter colored areas contain small graphene crystallites.

[0055] [Figure 30] 28 and 29. Lighter areas represent small graphene crystallites.

[0056] [Figure 31] A transmission electron micrograph of activated carbon with an iodine number of 806. The parallel lines across the image are atomically thin layers of graphene, and the shorter curved segments are graphene crystallites. DETAILED DESCRIPTION OF THE INVENTION

[0057] The detailed description will enable any person skilled in the art to make and use the disclosure. , several embodiments, adaptations, variations, alternatives, and uses of the present disclosure are described. These and other embodiments, features, and advantages are set forth in the following description of the present disclosure in conjunction with the accompanying drawings. This will become apparent to those skilled in the art upon reference to the detailed description of the present invention.

[0058] As used in this specification and the appended claims, the singular forms "a," "an," and "an" are used interchangeably. and "the" include plural referents unless the context clearly dictates otherwise. Unless otherwise stated, all technical and scientific terms used herein are of ordinary skill in the art to which this disclosure belongs. has the same meaning as commonly understood by

[0059] Unless otherwise indicated, the reaction conditions, stoichiometries, etc. used in the specification and claims All numbers expressing concentrations of ingredients, etc. are preceded in all instances by the term "about." Therefore, unless otherwise indicated, the following The numerical parameters set forth in the specification and attached claims are approximations and should not be construed as limiting the scope of the invention. At least, this may vary depending on the particular analytical technique.

[0060] For this purpose, "biogenic" refers to biomass that is renewable on timescales of months, years, or decades. means materials (whether feedstocks, products, or intermediates) containing elements such as carbon that can be used for Non-biological materials may be non-renewable or may last for centuries or May be renewable over time scales of thousands, millions, or even longer geological timescales It is noted that biogenic materials may include a mixture of biogenic and non-biogenic sources. I want to be.

[0061] For this purpose, "reagent" is intended to mean a material in its broadest sense. Reagents can be fuels, chemicals, materials, compounds, additives, blend components, solvents, etc. A reagent is not necessarily a chemical agent that causes or participates in a chemical reaction. A reagent may or may not be a chemical reactant and is consumed in a reaction. A reagent may be consumed or not. A reagent may be a chemical catalyst for a particular reaction. can cause adjustment of the mechanical, physical, or hydrodynamic properties of the material to which it can be added For example, a reagent may be introduced into a metal to impart certain strength properties to the metal. Reagents may be of sufficient purity (in this context , typically carbon purity).

[0062] Graphene is a single layer of carbon atoms densely packed in a two-dimensional honeycomb lattice, unlike other Graphene is the basic building block of multi-dimensional graphite-like materials. They can be folded into zero-dimensional fullerenes, rolled into one-dimensional nanotubes, or stacked. It can be synthesized into three-dimensional graphite, i.e., graphene is a single layer of atomic carbon. However, any number of layers (1, 2, 3, 4, 5, 6, 7, 8, 9, 10, or more, etc.) may be present in any particular portion of the graphene-containing sample. Graphene is typically, but not necessarily, planar, and is a single layer of graphene. , and multilayer graphene, which is a related sp 2 Among its forms, including graphitic allotropes In one embodiment, graphene refers to any of the graphenes of the type having a hexagonal arrangement of sp 2 Graphene is a one-atom-thick planar sheet of bonded carbon atoms. is a hexagonally arranged sp 2 A one atom thick planar sheet of bonded carbon atoms In another embodiment, graphene is a carbon-carbon polymer having a length of about 0.142 nm. Unless the context indicates otherwise, all references to graphene refer to both monolayer and It contains precisely multiple layers of carbon atoms. Also, all references to graphene should be interpreted as meaning "biogenic graphene." should be considered synonymous with "laphen."

[0063] Biogenic activated carbon is the initial feedstock utilized to produce biogenic activated carbon. The biogenic activated carbon provided herein has a relatively high carbon content. Since the typical carbon content of biomass does not exceed about 50% by weight, it is usually about half its weight. More typically, depending on the composition of the feedstock, biomass contains more than 1000 carbon atoms by weight. The source activated carbon is at least 55% by weight, at least 60% by weight, at least 65% by weight, At least 70% by weight, at least 75% by weight, at least 80% by weight, 85% by weight, at least 90% by weight, at least 95% by weight, at least 96% by weight, at least 97% by weight %, at least 98% by weight, at least 99% by weight of carbon.

[0064] Notwithstanding the foregoing, for practical purposes, the term "biogenic activated carbon" may refer to various In various embodiments, the materials that can be produced by the processes and systems of the present disclosure include: The term "carbon content," or any other concentration limit, is used herein to describe the should not be attributed to the term itself, but rather to specific embodiments and their equivalents. For example, the very nature of the work that is subject to the disclosed process shall be attributed only to the The starting material, which has a relatively low initial carbon content, is highly enriched in carbon compared to the starting material. (high carbon yield), but still relatively little carbon (low carbon purity) ( It is understood that biogenic activated carbon (containing up to about 50% carbon by weight) can be produced.

[0065] "Pyrolysis" and "pyrolyze" are roughly It refers to the thermal decomposition of carbonaceous materials. In decomposition, the oxygen required to complete combustion is about 10% or less, about 5% or less, about 1% or less % or less, about 0.5% or less, about 0.1% or less, or about 0.01% or less, etc. In some embodiments, there is less oxygen than is required to complete the reaction. The pyrolysis is carried out in the absence of oxygen.

[0066] Exemplary changes that may occur during pyrolysis include any of the following: (i) a change in the heat source; (ii) heat transfer from the feedstock increases the temperature within the feedstock; and (ii) primary pyrolysis at this higher temperature. The reaction begins, releasing volatiles and forming char; (iii) heat to a cooler solid. The hot volatiles flow facilitates heat transfer between the hot volatiles and the cooler unpyrolyzed feedstock. (iv) condensation of some of the volatiles in the cooler portions of the feedstock; Subsequent secondary reactions can produce tar; (v) while the autocatalytic secondary pyrolysis reaction proceeds, (vi) The primary pyrolysis reaction occurs simultaneously in competition; (vi) further pyrolysis, reformation, water-gas synthesis Free radical reactions, free radical recombination, and / or dehydration may also occur, which depend on residence time, temperature, is a function of the temperature, pressure, and pressure profile.

[0067] Pyrolysis can at least partially dehydrate the feedstock. The solution is more than about 50%, more than about 75%, more than about 90%, more than about 95%, more than about 99% of the water from the feedstock. , or removes more than 99%.

[0068] As mentioned above, some variations of the present disclosure involve multiple reactors or multiple zones within a single reactor. Optimizing carbon yield and product quality through pyrolysis while modifying and modifying feedstocks be designed and capable of operating in a manner that maintains flexibility and adaptability to the requirements of the product and It is premised, at least to some extent, on the discovery that

[0069] Generally speaking, the temperature and residence time are selected to achieve a relatively slow pyrolysis chemistry. A potential benefit is the substantial preservation of cell walls contained in the biomass structure. This means that the final product retains some, most, or all of the shape and strength of the starting biomass. To maximize this potential benefit, the cell wall is mechanically Utilizing equipment that does not break down or otherwise convert biomass particles into small particles Various reactor configurations are discussed below after the process description.

[0070] Additionally, if the feedstock is a milled or sized feedstock such as wood chips or pellets, If the feedstock is a powder, it may be desirable for the feedstock to be carefully milled or sized. First, careful processing preserves the strength and cell wall integrity present in natural feedstock sources (e.g., wood). This means that the final product tends to retain some of the shape and strength of the starting biomass. It may also be important if some, most, or all of the data should be retained.

[0071] In various embodiments, the vascular structure of woody feedstock is preserved to produce biogenic activated carbon. By way of example and not limitation, various implementations may be implemented. In some embodiments, the feedstock is heated for an extended period of time, for example, 1 hour or more, about 2 hours or more, about 3 hours or more. , about 4 hours or more, about 5 hours or more, about 6 hours or more, about 7 hours or more, about 8 hours or more, about 9 hours or more, about 10 hours or more, about 11 hours or more, about 12 hours or more, about 13 hours or more, about 14 hours Over 15 hours, Over 16 hours, Over 17 hours, Over 18 hours, Over 19 hours or more, about 20 hours or more, about 21 hours or more, about 22 hours or more, about 23 hours or more, or about 2 Prepared by drying the feedstock for a period of at least four hours, It allows water and gas to exit the biomass without destroying the tube bundle structure. In embodiments, pyrolysis (e.g., flash pyrolysis) can be performed over a period of minutes or hours. In contrast, the slow heat generation rate during the heating process disrupts the vascular structure of the feedstock. By way of example and not limitation, allowing water and gas to exit the biomass without breaking it down. The temperature ramp rate during the pyrolysis step is in the range of about 1°C / min to about 40°C / min, for example, about 1°C / min. / min, about 2°C / min, about 4°C / min, about 5°C / min, about 10°C / min, about 15°C / min, about 20°C / The heating rate may be about 25°C / min, about 30°C / min, about 35°C / min, or about 40°C / min. In some embodiments, the temperature increase occurs in a preheat zone to produce a preheated feedstock. In some embodiments, the temperature increase occurs primarily or entirely in the preheat zone, and the preheated In some embodiments, the temperature of the preheated feedstock is In some embodiments, the temperature increase occurs in the carbonization zone or pyrolysis zone. In some embodiments, the temperature increase occurs at least partially in the carbonization zone. In some embodiments, the reaction mixture is generated primarily or entirely in a preheating zone, a pyrolysis zone, or a pyrolysis zone. The pre-pyrolysis zone, carbonization zone, or pyrolysis zone is where the temperature is increased during pyrolysis from an initial low temperature to a maximum temperature. In some embodiments, the temperature is increased over time to a higher final temperature. In some embodiments, the temperature increase is linear or substantially linear over time. Therefore, the temperature increase rate is determined by the temperature during preheating, prepyrolysis, and / or carbonization or pyrolysis. At least a small amount of carbonization or pyrolysis is carried out during at least a portion of the thermal, pre-pyrolysis, and / or carbonization or pyrolysis steps. at least partially nonlinear, e.g., logarithmic or substantially logarithmic, over time In various embodiments, additives may be used prior to drying or pyrolysis to increase or decrease the , reducing gas formation that can damage the vascular structure of the feedstock during pyrolysis. In this method, prior to pyrolysis, the dried feedstock is used to crush the wood and reduce its strength. It is more sensitive to the vascular structure of wood than other sizing techniques such as chipping or shearing wet wood. Use a saw or other cutting device designed to be less destructive to the cutter. In such embodiments, the biogenic activated carbon product is Higher strength index (e.g., CSR) than comparable unprepared biogenic activated carbon products value).

[0072] In various embodiments, the feedstock is prepared by milling biomass. forming a plurality of biomass fragments that are substantially uniform in size and shape; For example and without limitation, biomass may be processed to produce particles of substantially uniform particle size (e.g., mesh size). Alternatively, biomass can be processed to produce sawdust of substantially Chips with uniform dimensions (e.g., about 1 inch x about 1 / 2 inch x about 1 / 8 inch cross section) In another embodiment, the feedstock can be milled from biomass. and a length of material having substantially uniform width and depth dimensions or diameter, (e.g., a wooden stick, a wooden board, or a wooden dowel). , further milling the length of material having a substantially uniform width and depth or diameter to form a substantially and producing feedstock fragments of substantially uniform length and substantially uniform size and shape. For example, a uniform diameter (e.g., about 1-1 / 8 inches) can be obtained. The resulting wood can be cut into pieces of substantially uniform length (e.g., about 1.5 inches). The resulting feedstock fragments are of substantially uniform shape (cylindrical) and substantially uniform size. It has dimensions of approximately 1-1 / 8 inches in diameter by approximately 1.5 inches in length. Organisms prepared from feedstocks consisting of fragments of substantially uniform shape and size, The original activated carbon product is produced from feedstock fragments of substantially non-uniform shape and / or size. It is produced in a higher mass yield than comparable biogenic activated carbon products prepared.

[0073] Referring now generally to FIGS. 1-13, several exemplary multi-reactor embodiments of the present disclosure are shown. Block flow diagrams are illustrated. Each diagram is discussed in turn below. Figures 1-13 It is intended to represent some illustrative embodiments, but not all contemplated embodiments, of the present disclosure. It should be understood that various additional non-illustrated embodiments and Combinations of several of the components and features discussed herein are also contemplated. As will be appreciated, any of the multiple reactors discussed herein may be independently The BPU may comprise multiple zones, or alternatively within a single reactor. These figures each show different alternative embodiments. However, all other considerations in this disclosure are to be construed in accordance with the illustrated embodiments and the It should be understood that the above may be applied to each of the embodiments.

[0074] Referring now generally to FIG. 1, a block flow diagram of a multi-reactor embodiment of the present disclosure is illustrated. This embodiment can utilize two or more different reactors. Three reactors are shown. Although shown in the solution embodiment, any different number of reactors may be used. Each reactor is transported at least through a material transport unit 304 (shown in FIG. 3). In one embodiment, the material transport unit 304 is connected to one other reactor. Atmospheric and temperature conditions are controlled.

[0075] In the illustrated embodiment, the raw material 109, such as biomass, is optionally dried and The dimensions are determined outside the system and optionally the material is fed to the first stage in a low-oxygen atmosphere using the material feed system 108. The mixture is introduced into a reactor 100. As discussed in more detail below and illustrated in FIG. Thus, the material supply system 108 maintains an oxygen level in the ambient air at the system of about 3% or more. The raw material 109 is then cooled to room temperature after the oxygen level is reduced in the first reactor. The raw material enters the first reactor 112 via a material transport unit 304. The material transport unit includes an encapsulated jacket or sleeve through which The steam and off-gas from the reactor are sent directly to preheat the biomass. or sent to a process gas heater and / or heat exchanger before The gas is either sent to be used for preheating or pyrolysis of the gas.

[0076] In the illustrated embodiment, raw material 109 is first transported to a material transport unit 304. The feedstock passes from the feed system 108 to the first reactor of the BPU 112.

[0077] As discussed in more detail below, in one embodiment, the first reactor 112 is 132 and any other reactors in the system to recover waste heat 132 and Energy is stored via a waste heat recovery system. The waste heat released in the system 12 is used to dry the raw material 109 either in the system or outside the system. activating a steaming bin or another suitable heating mechanism configured to heat the food; In this case, other by-products of the waste heat, such as substantially heated inert gas, are released to other parts of the system. can be used to further concentrate the material at any point in the process.

[0078] In the illustrated embodiment, biomass 109 enters a first reactor 112, where The temperature rises from a range of about ambient temperature to about 150°C to a temperature of about 100°C to about 200°C. In one embodiment, the temperature of the first reactor 112 does not exceed 200°C. As will be discussed in more detail, the first reactor 112 is heated and simultaneously feeds biomass 1 23. In one embodiment, the exhaust gas 120 may include an output mechanism for capturing and venting the exhaust gas 120 from the exhaust gas 123. In this case, the off-gas 120 is extracted for optional later use. Therefore, the heating sources used for the various zones within BPU 102 can be electric or gas. In this configuration, the heat sources used for the various reactors of the BPU 102 are the same as those in the other reactors of the unit 102. In various embodiments, the heat is indirect or can be waste gas from the reactor or an external source. do.

[0079] After preheating the first reactor 112, the material transport unit 304 transports the preheated material 123 through The reactor 114 is then passed through an optional second reactor 114. In one embodiment, the reactor 114 is In one embodiment, reactor 114 is different from reactor 112. The material transport unit 304 transports the material through a high temperature steam sealed system (e.g., air lock). 2 reactor 114, which prevents gas from leaking and at the same time allows the material transport unit 3 In one embodiment, the second reactor 1 The inside of 14 is heated to a temperature of about 100°C to about 600°C or about 200°C to about 600°C. In another embodiment, the second reactor 114 is carbonized and simultaneously preheated. The first reactor 102 is used to capture and vent the gases 122 released from the material 123. In one embodiment, the gas 122 is stored in a In one illustrative embodiment, the off-gas 120 from the first reactor 112 is extracted for further purification. and off-gas 122 from the second reactor 114 are combined into one gas stream 124 Once carbonized, the carbonized biomass 125 exits the second reactor 114 and is sent to a The third reactor 116 is again the third reactor 112 or 114. They may be the same reactor or they may be different.

[0080] In one embodiment, when the biogenic activated carbon product 125 enters the third reactor 116 The carbonized biomass 125 is heated (actively or passively) to a specified temperature range as described above. ) is cooled to form carbonized biomass 126. In one embodiment, the carbonized biomass 1 The temperature of 25 is reduced in the third reactor under substantially inert atmospheric conditions. In this embodiment, the third reactor cools the carbonized biomass 125 with an additional water cooling mechanism. To the extent that carbonized biomass 126 does not spontaneously combust when exposed to oxygenated air, It should be understood that cooling may occur within the reactor 116. In one such embodiment, The third reactor 116 reduces the temperature of the carbonized biomass to below 200°C. In an embodiment, the third reactor is a reactor for stirring and uniformly cooling the carbonized biomass. Cooling may be provided by water or other liquids, either directly or indirectly. Cooling can occur either directly or indirectly with air or other cooled gases. It should be understood that the above may occur in any of the above ways, or in any combination thereof.

[0081] In some embodiments (not shown), one or more additional coolers or chillers It should be understood that a variety of mechanisms may be used to further reduce the temperature of the carbonized biomass. In various such embodiments, the cooler may be connected to other reactors 11 along the material transport system. 2, 114, 116. In some embodiments, the cooler is In some embodiments, the cooler is the same as the reactors 112, 114, 116. In other embodiments, the cooler may be, for example, a direct or indirect cooler with water or other liquid. It may be cooled either indirectly or directly with other gases, or or a combination of the above, such as a screw, an auger, a conveyor (specifically, in one embodiment, (belt conveyor), drum, screen, pan, countercurrent bed, vertical tower, jacket In various embodiments, the cooling element may be a paddle with a cooling screw, a cooling screw, or a combination thereof. Coolant may be water spray, a stream of cooled inert gas, liquid nitrogen, or ambient air (if below ignition temperature). It may include a device for capturing flash steam generated by water spray or for introducing saturated steam. By capturing the superheated steam generated when the fuel is introduced and heated by the carbonized biomass, It should be appreciated that heat may be recovered from this step by

[0082] As illustrated in FIGS. 1 and 5, the gas phase separator unit 200 comprises at least one The BPU 102 includes an input and a plurality of outputs. At least one input is connected to the first reactor 1 of the BPU 102. 12 and the outlet port of the second reactor 114. One of the multiple outputs is a carbon capture unit 104, and another of the outputs is connected to a collection device, or It is connected to further processing equipment such as an acid hydrogenation unit 106 or a distillation column. In this configuration, the gas phase separator separates the on-stream gas from the first reactor 112 and the second reactor 114. The fumes 120, 122 are processed to produce a condensate 128 and a concentrated gas 204. In some embodiments, the condensables are used for energy recovery (134) (e.g., dryers, reactors, etc.). used either for carbon enrichment (in a gas heater or process gas heater) or other carbon enrichment. In various embodiments, the non-condensables (e.g., CO) can be used for energy recovery ( 34) (e.g., in a dryer, reactor, or process gas heater) As an inert gas in processes (e.g., degassing units, reactors, BPUs, or In a cooler, which will be discussed in more detail, or for carbon enrichment.

[0083] In various embodiments, the condensate 128 may contain acetic acid, methanol, furfural, and the like. In another embodiment, the concentrated effluent produced by the gas-phase separator 200 includes polar compounds. The condensed gas 204 is at least a non-polar gas, such as carbon monoxide, terpenes, methane, diacids, etc. In one embodiment, the gas phase separator comprises a fractionation column. In this embodiment, the acetic acid is sent to an optional acid hydrogenation unit via line 128. In this embodiment, methanol and / or furfural may be added to any further line(s). ) 136 to a distillation / treatment unit 138.

[0084] In various embodiments, as discussed in more detail below, the carbon recovery unit itself In various other embodiments, the material is concentrated in a carbon capture unit. In some such embodiments, the carbon dioxide is concentrated in a separate material concentration unit. The material recovery unit is a container for storing carbonized material, and a separate material concentration unit is a gas It should be understood that this is a unit where gas is introduced to concentrate the material.

[0085] In the illustrated embodiment, the carbon recovery unit 500 also concentrates the carbonized biomass 126. The carbonized biomass 126 exits the third reactor along the material transport unit 304. , and enters the carbon recovery unit 500. In various embodiments, the carbon dioxide gas is , and as discussed above, the carbon recovery unit 500 is connected to the gas phase separator 200. In one embodiment, the enriched gas 204 is directed to a carbon recovery unit. and combined with biogenic activated carbon product 126 to produce a high carbon biogenic activated carbon product. In another embodiment, carbon enriched gas from an external source is also fed to the carbon recovery unit. The final high-carbon biomass produced was then directed to the slag and combined with the carbonized biomass126. In various embodiments, the carbonized biomass is added to the activated carbon product. 126 is the reduced temperature carbonized biomass. The carbon-enriched gas from the timber processing facility can be co-located near the facility, as can gas from an external source. It can be used as follows.

[0086] Referring now generally to FIG. 2, a block diagram of a single reactor, multi-zone embodiment of the present disclosure is shown. In the illustrated embodiment, a raw material 209 such as biomass is optionally The material is introduced into the reactor 200 under a low-oxygen atmosphere using the material supply system 108 described above. As discussed in more detail below, the material supply system 108 The oxygen level in the surrounding air is reduced to about 3% or less. After this, the material enters the BPU 202 within the enclosed material transport unit 304. The material transport unit includes an encapsulated jacket or sleeve through which Steam and off-gas from reactor 200 are routed and used to preheat the biomass. do.

[0087] In the illustrated embodiment, the raw materials are first transferred to a material supply on a material transport unit 304. From the system 108, the BPU 202 moves to an optional drying zone 210. An optional drying zone 210 heats the raw material to remove water and other impurities before passing to the preheating zone 212. In one embodiment, the interior of the optional drying zone 210 is at about ambient temperature. The raw material 209 is heated to a temperature of about 150°C to about 150°C. The moisture may be removed, for example, from the optional drying zone 210. In another embodiment, the optional In another embodiment, the drying zone is adapted to extract steam and vapor. The vapors and steam from the optional drying zone are extracted for any subsequent use. As shown, the steam or vapor extracted from any drying zone may be used to feed the material through the material feed system. In one embodiment, the material supply system may be used in a suitable waste heat recovery system. The steam and vapor used in the system preheats the raw materials, while the oxygen level is controlled by the material feed. In another embodiment, the biomass is dried outside the reactor. and the reactor does not include a drying zone.

[0088] As discussed in more detail below, in one embodiment, the optional drying zone 210 comprises: 2. The cooling zone 216 is configured to recover waste heat 232 and to incorporate a suitable waste heat recovery system. In one embodiment, the energy released within the cooling zone 216 is stored through the system. and configured to dry raw material 209 in an optional drying zone 210 using the waste heat generated by the drying process. After drying for the desired time, the dried biomass 221 is It exits the drying zone 210 and enters the preheating zone 212 .

[0089] In the illustrated embodiment, dried biomass 221 is introduced into the first (preheating) zone 21. 2, where the temperature ranges from about ambient temperature to about 150°C to about 100°C to about 200°C. In one embodiment, the temperature of the first / preheat zone 212 is increased to a temperature range of 200 If the preheat zone 212 is too hot or not hot enough, the dry It should be understood that mass 221 may be misprocessed before entering the second band 214. As discussed in more detail below, the preheat zone 212 simultaneously preheats and dehydrates the An output mechanism for capturing and discharging off-gas 220 from the biomass 221 may be included. In this embodiment, the off-gas 220 is extracted for optional later use. In an embodiment, the heat sources used for the various zones within BPU 202 are electric or gas. In one embodiment, the heat sources used for the various zones of the BPU 202 are 202 or waste gas from an external source. It is contiguous.

[0090] After the preheat zone 212, the material transport unit 304 passes the preheated material 223 and In one embodiment, the material transport unit 304 Passing through the second / pyrolysis zone via a steam sealing system (airlock, etc. (not shown) ,This prevents (or minimizes) gas leakage and at the same time, 304 through the high temperature pyrolysis zone. In one embodiment, the pyrolysis zone The inside of 214 is heated to a temperature of about 100℃ to about 600℃ or about 200℃ to about 500℃. In another embodiment, the pyrolysis zone 214 is simultaneously carbonized and preheated. A preheating zone 21 is provided to capture and vent gases 222 released from the biomass 223. 2. In one embodiment, gas 222 is In one illustrated embodiment, the off-gas 220 from the preheating zone 212 and and off-gas 222 from pyrolysis zone 214 are combined into one gas stream 224 Once carbonized, the carbonized biomass 225 exits the second / pyrolysis zone 214 and is fed to the third / pyrolysis zone 214. A temperature reduction or cooling zone 216 is entered.

[0091] In one embodiment, as the carbonized biomass 225 enters the cooling zone 216, The mass 225 is cooled to a specified temperature range of about 20°C to 25°C (about room temperature) as described above. The BPU 20 is then cooled to a temperature of 1000 W. 2 includes multiple cooling zones. In one embodiment, cooling zone 216 is a cooling zone for cooling the carbonized biomass. In one embodiment, the cooling zone is used to agitate and homogenize the material. In various embodiments, one of the cooling zones includes a mixer for cooling the cooling water. One or more reside outside of BPU 202.

[0092] As illustrated in FIGS. 2 and 5, the gas phase separator unit 200 comprises at least one In this illustrative embodiment, at least one input is At the discharge ports of the first / preheating zone 212 and the second / pyrolysis zone 214 of the BPU 202 One of the outputs is connected to a carbon capture unit 500 (to concentrate the material). Another output is connected to a collection device or oxygen / hydrogen 206 or further processing equipment such as a distillation column. 2, the gas phase separator separates the first / preheating zone 212 and the second / pyrolysis zone 214. The off-gases 220, 222 are treated to produce a condensate 228 and a concentrated gas 204. In one embodiment, the condensate 228 comprises polar compounds such as acetic acid, methanol, and furfural. In one embodiment, the enriched gas 2 produced by the gas-phase separator 200 In one embodiment, the gas phase separator comprises a fractionation column. In one embodiment, acetic acid is supplied to optional acid hydrogenation unit 2 via line 228. In another embodiment, the methanol and / or furfural are optionally Optional further line(s) 236 are sent to a distillation / treatment unit 238 .

[0093] In the illustrated embodiment, the carbonized biomass is cooled along the material transfer unit 304. The refrigeration reactor / zone exits and enters the carbon recovery unit 500. In various embodiments, As illustrated in more detail in and discussed above, the carbon capture unit 500 is configured to capture and process gas-phase It also includes an input 524 connected to the separator 200. In one embodiment, the enriched gas 204 is The high carbon dioxide is then directed to a carbon recovery unit 500 where it is combined with the biogenic activated carbon product 226. In another embodiment, carbon from an external source is added to produce a natural, biogenic activated carbon product 136. The enriched gas is also directed to a carbon recovery unit 500 where it is combined with the biogenic activated carbon product 226. In various embodiments, the activated carbon is added to the biogenic activated carbon product. The gas drawn from the carbon recovery unit 500 at reference 234 is used in an energy recovery system and / or optionally used in a system for further carbon enrichment. In various embodiments, gas drawn from one or more zones of the BPU 202 is Optionally used in energy recovery systems and / or systems for further carbon enrichment Illustratively, the system 200 may be co-located near a lumber processing facility, Carbon enriched gas from the equipment can be used as the gas from the external source.

[0094] Referring now generally to FIG. 3, one embodiment of a material delivery system of the present disclosure is illustrated. As mentioned above, the high oxygen levels in the ambient air surrounding the raw materials as they are processed can result in undesirable combustion or oxidation of the raw materials, which can affect the quantity and quality of the final product. In one embodiment, the material supply system is a closed system. , including one or more manifolds configured to purge oxygen from the air surrounding the raw material. In one embodiment, an oxygen level of about 0.5% to about 1.0% is used during preheating, pyrolysis / carbonization. The primary goal of a closed material supply system is to by reducing the concentration of It should be understood that after the oxygen level has decreased, the biomass is In various embodiments, the recovered process energy is used to Preheating of the inert gas and then discharging the preheated inert gas into the BPU, reactor, or It will be appreciated that introduction into the trimming reactor makes the system more efficient.

[0095] In some embodiments, a trimming reactor is included in the system. In one embodiment of the reactor, the pyrolysis material from the BPU is separated for further pyrolysis. into a further reactor where heated inert gas is introduced to produce a higher fixation In various embodiments, the secondary process creates a product having a carbon level. , e.g., drums, tanks, barrels, bins, totes, pipes, sacks, presses, or rolls In various embodiments, the final vessel may be a transfer vessel for the carbonized biomass. In some embodiments, the inert gas may be extracted from the BPU. The gas is then heated through a heat exchanger which extracts heat from the gas that is burned in the process gas heater. It's hot.

[0096] As seen in FIG. 3, the closed material supply system 108 includes a raw material supply hopper 3 00, material transport unit 304, and oxygen purge manifold 302.

[0097] In one embodiment, the raw material supply hopper 300 is raw or pre-sized. Any suitable air outlet configured to receive the wet / dried biomass 109 / 209. The raw material supply hopper 300 is an open container or an air-closed container. 4, which in one embodiment is a screw that is operably rotated by a drive source. or an Auger system. In one embodiment, the raw material 109 / 209 is a gravity-fed The material transport unit 304 is supplied by a feed system. 4 is made so that the screw or auger 305 is enclosed in a suitable enclosure 307 It should be understood that in one embodiment, the enclosure 307 is substantially cylindrical. In embodiments, the material delivery system may include a screw, an auger, a conveyor, a drum, a screen, chute, drop chamber, air conveying device (also known as rotary airlock or double or triple flap airlock).

[0098] Raw materials 109 / 209 are fed from raw material feed hopper 300 to material transport unit 304 When this occurs, the auger or screw 305 rotates, forcing the raw material 109 / 209 through an oxygen purged manifold. The raw material 109 / 209 reaches the oxygen purge manifold 302. Then, the ambient air between the raw materials 109 / 209 in the material transport unit 304 is about 20.9% It should be understood that the oxygen purge manifold 302 contains , located in proximity to or around the material transport unit 304. In the oxygen fold manifold, the enclosure 30 of the material transport unit 304 7 includes a plurality of gas inlet ports 310a, 310b, 310c and a plurality of gas outlet ports. Includes 308a, 308b, and 308c.

[0099] The oxygen purge manifold 302 includes at least one gas inlet line 312 and at least one The oxygen purge manifold 30 has one gas outlet line 314. In various embodiments, the oxygen purge manifold 30 At least one gas inlet line 312 of the two gas inlets is connected to a plurality of gas inlet ports 310a, 310b. Similarly, in various embodiments, At least one gas outlet line 314 of the oxygen purge manifold 302 is connected to a plurality of gas outlet ports. In one embodiment, the ports 308a, 308b, and 308c are in operative communication with each other. In this case, a gas inlet line 312 supplies an inert gas to gas inlet ports 310a, 310b, 310c. It should be understood that the device is configured to pump the blood to 0c. In one embodiment, the inert gas is nitrogen that is substantially free of oxygen. The reactive gas flows countercurrent to the biomass.

[0100] As will be appreciated, the introduction of the inert gas 312 into the enclosed material transport unit 304 , pushing ambient air out of the enclosed system. During operation, the inert gas 312 is When introduced into the first gas inlet port 310a, the amount of oxygen-enriched ambient air is At this point, the oxygen concentration is about 2% or less, about 1% or less, and about Desired levels of 0.5% or less oxygen, or about 0.2% or less oxygen, are not achieved It should be understood that in various embodiments, the encapsulated system Inert gas 3 is used to purge the required amount of oxygen from the air surrounding the raw material 109 in the system. 12 additional injections should be made. In one embodiment, a second gas inlet port 310b is filled with inert gas 312 after injection at the first gas inlet port 310a. pump into the system, thereby extracting more of the remaining oxygen from the enclosed system. After injecting the inert gas 312 once or twice to purge the oxygen 314, It should be understood that a desired level of low oxygen may be achieved. If the desired oxygen level is still not achieved after two inert gas injections, A third injection of inert gas 312 at inlet 310c is introduced into the enclosed system at gas outlet 308c. 3. Purge the system of any remaining undesired amounts of oxygen 314. If desired, further inlet / outlet In various embodiments, the oxygen level is controlled throughout the material delivery system. The flow rate is monitored throughout to allow calibration of the amount and location of the inert gas injection.

[0101] In an alternative embodiment, the heat, steam, and gases recovered from the reactor are used in a feed system. The feedstock is then directed to the feedstock where they are enclosed in a jacket and isolated from direct contact with the feed material. However, the feed is indirectly heated before being introduced into the reactor.

[0102] In an alternative embodiment, the heat, steam, and gases recovered from the drying zone of the reactor are are directed into the feed system where they are enclosed in a jacket and are in direct contact with the feed material. The feed is separated from the catalyst but is indirectly heated before being introduced into the reactor.

[0103] In one embodiment, gas inlet ports 310a, 310b, 310c and their corresponding Gas outlet ports 308a, 308b, 308c are arranged in two vertical rows through the material transport unit 304. It should be understood that the planes are slightly offset from one another. In this embodiment, the inlet port 310a and corresponding outlet port 308a are connected to the material transport unit. The material transport unit 304 is driven by an amount approximately equivalent to the pitch of the Auger 305 in the feed 304. In various embodiments, the atmosphere surrounding the raw material 109 / 209 After the air is sufficiently deoxygenated, it is fed from the material feed system 108 to the BPU 102. In various embodiments, oxygen levels are monitored throughout the material delivery system. This allows for calibration of the amount and location of the inert gas injection.

[0104] In one embodiment, the raw material 109 / 209 and the subsequently dried biomass Biomass 221, preheated biomass 123 / 223, carbonized biomass 125 / 225, and The carbonized biomass 126 / 226 is fed to reactor 1 along a continuous material transport unit 304. It should be understood that the reaction mixture moves through the reactor 02 (or multiple reactors). Therefore, the material transport units that transport this material are different at different stages of the process. In this case, the reactor, zone, or process of moving material through the reactor is continuous. In one such embodiment, the velocity of the material transport unit 304 is adjusted so that the material is transported through the reactor ( 304. The material transport unit 304 may be configured to move through the are suitably calibrated and calculated by the controller and processor associated with the

[0105] In another embodiment, reactor 102 or multiple reactors (112 / 114 / 116) The controller associated with the sensor may include one or more feedback sensors, a detected gas (e.g. , any FTIR derived), measured parameters, thermometers, or reactor processes and other suitable variations may be configured to adjust the speed of the material transport unit 304 based on the In various embodiments, any suitable water supply in operable communication with the controller and processor. A temperature sensor or gas sensor is installed in the zone / reactor or in each zone / reactor. It can be integrated at any suitable location between reactors or along the material transport unit 304. In one embodiment, the controller and processor receive the information from the sensor or gauge. This information is used to optimize the speed and efficiency of the BPU 100 / 200. In this case, the control associated with the reactor 102 or multiple reactors (112 / 114 / 116) The controller is configured to operate the material transport unit 304. In one embodiment, The controller associated with reactor 102 or multiple reactors (112 / 114 / 116) , the concentration of gas inside the material transport unit 304 or any of these reactors; In one embodiment, the controller is configured to monitor various Based on one or more readings measured by the sensor, Applied to the velocity, gas input to the material transport unit, and material in the material transport unit configured to regulate heat.

[0106] 2 and 4, one embodiment of the BPU 102 is illustrated. It should be understood that the graphical representation of U 202 corresponds substantially to BPU 202 of FIG. In various embodiments, the BPU 202 is enclosed in a kiln shell to provide the necessary fuel for the reactor process. It should also be understood that the abundant amounts of heat required can be controlled and manipulated. In one embodiment, the kiln shell of the BPU 202 has four zones 210, 212, 214 and 216. In an embodiment, the kiln includes four separate zones. Each of the four bands 210, 212, 214, and 216 of the BPU 202 has at least Also includes one entrance flight and at least one exit flight. As shown, within each band in such an embodiment, there are entrance flights and exit flights. Flights can coordinate the control of feedstock, gas, and heat flows into and out of the zone. A supply of inert air may be introduced into the inlet flight and purged. The trapped air can be extracted from a corresponding exit flight. One or more of the exit flights of the band within 202 may be adjacent to other entrance flights or Connected to one or more of the exit flights.

[0107] In one embodiment, the raw material 209 is deoxygenated in the material supply system 108. The mixture is then introduced into the BPU 202, specifically into the first of four zones, the optional drying zone 210. As can be seen in FIG. 4, the drying zone is formed by an inlet flight 422b and an outlet flight 422c. In one embodiment, the drying zone is heated to a temperature of about 80°C to about 150°C. The biomass is then heated to remove water or other moisture from the raw material 209. zone or preheating zone 212 where the biomass is preheated as described above.

[0108] In another embodiment, the optionally dried and preheated material is passed through a third zone or In one embodiment, the carbonization is performed at a temperature of about 200°C to about 700°C, e.g. , about 200°C, about 210°C, about 220°C, about 230°C, about 240°C, about 250°C, about 26 0℃, approx. 270℃, approx. 280℃, approx. 290℃, approx. 300℃, approx. 310℃, approx. 320℃, approx. 330℃, approximately 340℃, approximately 350℃, approximately 360℃, approximately 370℃, approximately 380℃, approximately 390℃ , about 400℃, 410℃, about 420℃, about 430℃, about 440℃, about 450℃, about 460℃ ℃, about 470℃, about 480℃, about 490℃, about 500℃, about 510℃, about 520℃, about 5 30℃, approximately 540℃, approximately 550℃, approximately 560℃, approximately 570℃, approximately 580℃, approximately 590℃, Approximately 600°C, approximately 610°C, approximately 620°C, approximately 630°C, approximately 640°C, approximately 650°C, approximately 660 This occurs at temperatures of about 670°C, about 680°C, about 690°C, or about 700°C. In this configuration, the carbonization zone of the reactor 421 is configured so that the gases produced during carbonization are extracted. In another embodiment, the gas generated during carbonization is optionally In one embodiment, the carbonization temperature is 100°C / 200°F. Minimize or eliminate carbon dioxide production and maximize the carbon content of carbonized biomass. It is selected to be

[0109] In another embodiment, the carbonized biomass is subjected to a temperature reduction zone or cooling zone (third zone ) and allow it to be passively cooled or actively cooled. In the form, the carbonized biomass solids are heated at temperatures of room temperature ±10, 20, 30, or 40°C. The mixture is cooled to 100°C.

[0110] In various embodiments, the BPU includes multiple gas introduction and extraction probes. In the embodiment of the BPU illustrated in FIG. 408, 410, 412, and 414, and a plurality of gas extraction probes 400, 4 In various embodiments, each gas introduction One of the input probes and one of each gas extraction probe are 210, 212, 214, and 216. In various alternative embodiments, the BPU 202 may include two sub-bands for each of a plurality of bands. Any suitable number of gas introduction probes, including two or more gas extraction probes, may be used. It should also be understood that this includes gas introduction probes and gas extraction probes.

[0111] In the illustrated embodiment, the drying zone 210 includes a gas introduction probe 412 and a gas In one embodiment, the gas introduction probe 412 is associated with the extraction probe 402. , nitrogen is introduced into the drying zone 210, and the gas extraction probe 402 extracts the gas from the drying zone 210. In various embodiments, a gas introduction probe 412 introduces gas into the drying zone 210. It should be understood that the method is configured to introduce the mixture. The gas selected is oxygen. In various embodiments, as described in more detail above, A gas extraction probe 402 extracts gas from the drying zone 210 and supplies it to a heat or energy recovery system. It should be understood that the data is reused in the system.

[0112] In the illustrated embodiment, the preheat zone 212 includes a gas introduction probe 414 and a gas In one embodiment, the gas introduction probe 414 is associated with the extraction probe 400. , nitrogen is introduced into the preheating zone 212, and the gas extraction probe 400 extracts the gas from the preheating zone 212. In various embodiments, a gas introduction probe 414 introduces gas into the preheat zone 212. It should be understood that the gas mixture may be introduced. The gas extracted by the extraction probe 400 comprises carbon-enriched off-gas. As mentioned above, the gases extracted from the preheating zone 212 and pyrolysis zone 214 may be, for example, It should be understood that the carbon dioxide is reintroduced into the material later in the process in a carbon recovery unit. In certain embodiments, the gas extracted from any of the reactor zones is trimmed. Energy recovery in the dryer or process gas heater for further pyrolysis in the reactor The wastewater is either used for harvesting or used in a carbon enrichment unit.

[0113] In the illustrated embodiment, the pyrolysis zone 214 includes a gas introduction probe 410 and a gas In one embodiment, the gas introduction probe 410 is associated with the gas extraction probe 404. introduces nitrogen into the pyrolysis zone 214, and the gas extraction probe 404 extracts nitrogen from the pyrolysis zone 214. In various embodiments, a gas introduction probe 410 is provided in the pyrolysis zone 21. It should be understood that the gas mixture is configured to be introduced into the gas supply passage 4. Thus, the gas extracted by the gas extraction probe 404 comprises carbon-enriched off-gas. In the process, as described above, the carbon enriched gas extracted from the pyrolysis zone 214 is used to It should be understood that the material may be reintroduced later in the process. As described in more detail in , the gas 400 extracted from the preheating zone 212 and the pyrolysis The gases 404 extracted from zone 214 are combined before being reintroduced into the material.

[0114] In the illustrated embodiment, the cooling zone 116 includes a gas introduction probe 408 and a gas In one embodiment, the gas introduction probe 408 is associated with the extraction probe 406. , nitrogen is introduced into the cooling zone 116, and the gas extraction probe 406 extracts the gas from the cooling zone 116. In various embodiments, a gas introduction probe 408 introduces gas into the cooling zone 116. It should be understood that the above-described configuration is configured to introduce the mixture. As will be described in more detail, a gas extraction probe 406 extracts gas from the cooling zone 116. It should be understood that the heat generated by the process may be reused in a heat or energy recovery system.

[0115] The gas introduction probe and gas extraction probe of the various embodiments described above may be connected to the controller and and operate with multiple sensors to measure the gases introduced into each zone and the It is understood that the present invention is configured to regulate the level and concentration of gas extracted from the zone. sea ​​bream.

[0116] In various embodiments, the gas introduction probe and gas extraction probe are resistant to high temperature fluctuations. In one embodiment, the gas introduction probe is made of a suitable pipe configured to The nozzle and gas extraction probe include a plurality of openings through which gas is introduced or extracted. In various embodiments, the plurality of openings are below the inlet and gas extraction probe. In various embodiments, each of the plurality of openings is substantially It extends over a long distance.

[0117] In one embodiment, the gas introduction probes are directed through each zone to one of the BPUs 202. In one such embodiment, the four gas introduction probes each extend from the side. , extending from one side of the BPU to each respective zone. In such an embodiment, four gases are added to enrich the oxygen levels. A plurality of openings for each of the introduction probes are associated with that particular gas introduction probe. It should be understood that the IF signal is placed only within each designated band.

[0118] For example, referring to FIG. 4, the gas introduction probes are arranged from the left side of the drying zone to the Each of the four gas introduction probes extends through one of the drying zones. The dry zone gas introduction probe terminates within the dry zone. The remaining three gas introduction probes are All travel through the preheat zone, and the preheat zone gas introduction probe terminates within the preheat zone. The remaining two gas introduction probes move through the pyrolysis zone and are connected to the pyrolysis zone gas introduction probes. The probe terminates in the pyrolysis zone. The cooling zone gas introduction probe moves into the cooling zone and In various embodiments, the gas introduction probe is the only one that terminates within the cooling zone. It will be understood that the extraction probe is configured similarly to the gas introduction probe described in this example. The gas inlet probe and the gas extractor probe should be installed on either side of the BPU. It should also be understood that starting from the side.

[0119] In various embodiments, the gas introduction probe is configured in a multi-port configuration as described in the example above. In order to save space, the electrodes are arranged concentrically with one another. In this state, each of the four inlet probes / ports is For example, in one embodiment, the dry zone gas introduction probe has a maximum diameter of a preheat zone gas inlet probe / port located within the inner diameter of the drying zone inlet probe / port; The pyrolysis zone gas inlet probe is then placed within the inner diameter of the preheat zone gas inlet probe. and the cooling zone gas introduction probe is positioned within the pyrolysis zone gas introduction probe. In one exemplary embodiment, a suitable connector connects four gas leads external to the BPU 102. Each of the four gas inlet probes is attached to the The air entering the room is individually controlled.

[0120] In one such embodiment, similar to the example above, the dry zone gas introduction probe The other three gas introduction probes terminate in the preheat zone. In a circular configuration or substantially concentric arrangement, only the outermost gas introduction probes are In one such embodiment, the The individual zone gas introductions are effectively controlled independently of each other while the gas introductions are controlled as one continuous gas. Only the lead-in probe line is required. It should be understood that the configuration of is suitable for use in a gas extraction probe in one embodiment.

[0121] In one embodiment, each zone or reactor is a separate zone or reactor. In another embodiment, the apparatus is adapted to extract and collect off-gas from one or more of: The off-gas from each zone / reactor is then collected for disposal, analysis, and / or later use. In various embodiments, each reactor / zone is separated into zones / Contains a gas detection system such as FTIR that can monitor gas formation within the reactor. In another embodiment, the off-gas from the multiple zones / reactors is disposed of, analyzed, and / or or adapted for later use, and in various embodiments, from one or more zones / reactors. The off-gas from the process gas is supplied to a process gas heater. The off-gas from the zone / reactor is fed to a carbon recovery unit. The off-gas from one or more zones / reactors may be subjected to gas phase separation prior to being introduced into the carbon recovery unit. In one embodiment, the gas phase separator comprises a fractionation column. Any known fractionation column may be used. In one embodiment, the off-gas is heated to a suitable temperature. The non-polar and polar compounds are separated using standard fractionation columns or packed columns. In another embodiment, the non-polar compounds or enriched gas from the gas phase separator may be any In various embodiments, the ozone from one or more zones / reactors is extracted for later use. The fumes are fed to a process gas heater. In one embodiment, a preheat zone / reactor, The gases extracted from the pyrolysis zone / reactor and, optionally, the cooling zone / reactor are combined. In various embodiments, the zone / reactor is One or more of these may determine whether or not gas is introduced into the combined stream and how much gas is added. The device is configured to control how much of the gas is introduced into the combined flow.

[0122] As discussed above and generally illustrated in FIG. 5, the off-gas from the BPU 102 / 202 124 / 224 is directed into the gas phase separator 200. In various embodiments, Gas 124 / 224 is gas extracted from the second / pyrolysis zone / reactor 114 / 214. 122 / 222 or the first / preheating zone / reactor 1 combined with either gas flow only 12 / 212. The off-gas 124 / 224 is a gas phase separator. Entering 200, the off-gas 124 / 224 is polar compounds 128 / 228 / 136 / 23 6 and non-polar compounds 204, such as non-polar gases. The gas phase separator 200 is a known fractionation column.

[0123] In various embodiments, concentrated gas extracted from the combined off-gas 124 / 224 The gas phase separator 200 is directed into the carbon recovery unit 500 via an input 524. As discussed above and illustrated in Figures 8 and 11, various In various embodiments, the extracted gas is first introduced into a material enrichment unit and then , which is introduced into a separate carbon recovery unit. In the present embodiment, material enrichment occurs in a carbon recovery unit 500. , gas-phase separator 200 includes multiple outputs. In various embodiments, gas-phase separator 200 One output from the carbon capture unit 500 is connected to the carbon capture unit 500. In one embodiment, a portion of the enriched gas stream is introduced into a carbon recovery unit. A portion is directed to the pump 500, and another portion is directed to a scrubber or other suitable purification device, as desired. In various embodiments, the undesired gas is sent to a carbon recovery unit. The remaining off-gas can be used for energy recovery (e.g. in a process gas heater). or as an inert gas (e.g., in degassing units, reactors, BPUs, or coolers) Similarly, in various embodiments, a carbon recovery unit Off-gas from the , as an inert gas (e.g., in a degassing unit, reactor, BPU, or cooler) ), or in a secondary recovery unit.

[0124] In one embodiment, another output from the gas phase separator extracts polar compounds and Optionally, condense into a liquid component (including multiple different liquid portions). In various embodiments, the liquid includes water, acetic acid, methanol, and furfural. The output liquid can then be stored, disposed of, further treated, or recycled. For example, in one embodiment, the output water is reused and used in another part of the system. It should be understood that the water may be heated or cooled. In one embodiment, the acetic acid, methanol, and furfural that are output are recycled. It should also be understood that the water may be sent to a storage tank for utilization, resale, distillation, or purification.

[0125] As seen in FIG. 5, one embodiment of the carbon capture unit 500 has an upper and a lower portion. In various embodiments where the material enrichment unit is separate from the carbon recovery unit, 5. In the present invention, the material enrichment unit has the features discussed with respect to the carbon recovery unit 500 of FIG. It should be understood that the carbon recovery unit includes similar features. A housing 502 having a portion 502a and a portion 502b configured to carry reactor off-gas. an inlet 524 located at the bottom of the lower portion of the enclosed enclosure, the inlet 524 being configured to carry a concentrated gas stream; an outlet 534 located at the top of the upper portion; a passageway 504 defined between the upper and lower portions of the housing; and a transport system 528 configured to transport the reagent following the passageway, and the housing comprises: The reagent is configured to adsorb at least a portion of the reactor off-gas. In the embodiment, the upper portion includes a plurality of outlets and the lower portion includes a plurality of inlets.

[0126] In one embodiment, the housing 502 is angled at 110 degrees or less, 90 degrees or less, 80 degrees or less, or In one embodiment, the housing 502 is substantially free of corners having an angle of 70 degrees or less. In another embodiment, the housing 502 is substantially free of convex corners. In another embodiment, the housing 50 is substantially free of convex corners that can create 2 is a cube, a rectangular prism, an ellipsoid, a solid ellipsoid, a spheroid, and two bodies with their bases attached. cone, two regular tetrahedrons attached at their bases, and two rectangular pyramids attached at their bases , or is shaped substantially like two isosceles triangular prisms with their bases attached to each other.

[0127] In one embodiment, the upper and lower portions 502a, 502b of the housing 502 are semi-ellipsoidal, semi-elliptical, Rectangular prism, semi-spheroid, semi-spheroid, cone, regular tetrahedron, rectangular pyramid, isosceles triangle Implemented as a square column or a circular-rectangular duct transition, respectively. Qualitatively shaped.

[0128] In another embodiment, the inlet 524 is located at the bottom of the lower portion of the housing 502b and the housing 5 An outlet 534 located at the top of the top of the O2a is configured to connect to a pipe. In this embodiment, the top of the lower part of the housing 502b and the bottom of the upper part of the housing 502a are In another embodiment, the bottom of the housing 502b may be substantially rectangular, circular, or oval. The width between the top of the section and the bottom of the top of the housing 502a is wider than the width of the transport system 528. In one embodiment, the width of the transport system 528 is its height.

[0129] In one embodiment, the carbon capture unit 500 includes a passageway defined between an upper portion and a lower portion. , an entrance opening 506, and an exit opening 508. In one embodiment, the entrance opening The portion and the exit opening are configured to receive a transport system. , the transport system 528 is at least semi-permeable or permeable to the concentrated gas.

[0130] In one embodiment, the inlet opening 506 is an inlet opening 508 having a diameter of 100 mm to reduce gas leakage. The outlet opening 508 includes a sealing mechanism to reduce gas leakage. In one embodiment, the inlet and outlet opening sealing mechanism comprises an airlock. .

[0131] In various embodiments, the lower portion 502b of the carbon recovery unit housing has a narrow circular bottom. a connecting opening, which is connected to the gas phase separator 200 for the transport of the gas flow 204; In various embodiments, the top of the lower part 502b of the housing of the carbon recovery unit 500 is , is substantially rectangular and is substantially wider than the width of the narrow circular bottom connection opening. In this state, the lower part transitions from a circular bottom opening to a rectangular top opening. In one embodiment, the width of the bottom rectangular top opening is approximately 6 feet. (along the direction of the conveyor system). In various embodiments, the carbon capture unit The upper portion of 500 is shaped substantially similarly to the lower portion. The width of the mouth is wider than the top opening of the lower part. The opening width is approximately 6.5 feet (along the direction of the conveyor system). In this embodiment, the upper portion passes through the carbon recovery unit 500 and is not adsorbed by the activated material. The gas trap is configured to capture any gas that passes through it.

[0132] In various embodiments, the configuration of the lower portion of the carbon recovery unit is such that the biogenic activated carbon product retardation and dispersion of gas 204 over the larger surface area of ​​the conveyor carrying 126 / 226 It should be understood that in various embodiments, the lower portion of the carbon capture unit 500 The exact shape of 502b and upper part 502a depends on the angle of gas dispersion from the gas phase separator pipe. In various embodiments, the gas is pumped at a flare ranging from 5 to 30 degrees from vertical. It should be understood that the pump will have a natural tendency to expand when injected. The flare angle is approximately 15 degrees. To prevent air capture or vortex formation, It should be understood that the bottom of the unit is constructed with as few folds and corners as possible. .

[0133] In one embodiment, the carbon recovery unit 500 comprises the gas phase separator 200 described above, and In various embodiments, the carbon The collection unit 500 is connected to the output of the cooling reactor / zone 216 / 116 or BPU 102 / 2. In one embodiment, the cooling reaction The output of the reactor / band 116 / 216 is the active ingredient of biogenic substances processed by BPU102 / 202. In one embodiment, the biogenic activated carbon product 126 / 226 is preferably The carbon dioxide enters the carbon capture unit 500 along a transport system. The top and bottom of the collection unit are connected to each other and define a path for the transport system to travel. In one embodiment, the transport system is constructed of a porous or mesh material. They are configured to allow gas to pass through them. through an opening in the carbon recovery unit 500 and then through the outlet opening of the carbon recovery unit. It should be understood that in some embodiments, the carbon capture unit is configured to Entrances and exits to and from the unit shall be properly sealed with airlocks or another suitable sealing mechanism. The conveyor is sealed to prevent gas from leaking through the opening. Off-gases that are not sent to the recovery unit can be used for energy recovery (e.g., process gas in heaters), or as an inert gas (e.g., in degassing units, reactors, BPUs, or in a refrigerator). , the off-gas from the carbon recovery unit can be used for energy recovery (e.g., process gas in heaters), as an inert gas (e.g., in degassing units, reactors, BPUs, if It can be used either in a gas turbine (e.g., in a cooler) or in a secondary recovery unit.

[0134] In various embodiments, the process comprises the steps of: Using a discharge mechanism, the biogenic activated carbon product 126 / 226 was first cooled in the cooling zone 116 / 21. 6 to the transport system. The activated carbon product 126 / 216 is spread across the width of the conveying system and is used to minimizes focusing and maximizes surface area for gas absorption. Once the composition 126 / 216 has been deposited and suitably spread over the delivery system, various embodiments In the above, the transport system is defined between the lower and uppermost portions of the carbon capture unit 1. Transport the biogenic activated carbon product 126 / 216 through the opening in 04. Carbon Capture Unit In the reactor 104, the biogenic activated carbon product 126 / 216 is separated from the gas phase separator 200. The gas is then adsorbed from the pipe into the bottom of the carbon capture unit 104. After the carbon product is enriched with non-polar gases, the biogenic activated carbon product is enriched with high-carbon biogenic activated carbon. It should be understood that the resulting high carbon, biogenic, activated carbon product is The purified carbon product is the final product of the process disclosed herein and is processed in carbon recovery unit 104. from which it is transported to suitable storage or post-treatment equipment.

[0135] In one embodiment, the concentrated gas 204 is conveyed through a conveyor and a biogenic activated carbon product 126. After passing through / 216, the resulting gas is extracted at the top of the carbon recovery unit 104. In various embodiments, the exhaust gas 134 is passed through a suitable scrubber, stack, or In some embodiments, the exhaust gas is delivered to a secondary carbon capture unit. be utilized in any reusable capacity in the system, including use in knitting, or In various embodiments, the wastewater is not sent to a carbon capture unit. The off-gas can be used for energy recovery (e.g. in a process gas heater), or As an inert gas (e.g., in degassing units, reactors, BPUs, or coolers) Similarly, in various embodiments, the carbon dioxide from the carbon recovery unit may be used in either The off-gas can be inertly recycled for energy recovery (e.g., in a process gas heater). as a reactive gas (e.g., in a degassing unit, reactor, BPU, or cooler), or or in a secondary recovery unit.

[0136] Biogenic activated carbon product 126 / 216 contains abundant carbon, which is converted to non-polar gases. It should be understood that the enriched gas stream 204 strongly favors the adsorption of terpenes, carbon monoxide, It should also be understood to include primarily non-polar gases such as carbon dioxide and methane. In this configuration, when the concentrated gas is directed from the gas phase separator to the carbon recovery unit, the flow of gas The quantity and speed of the conveyor are monitored and controlled, and the biogenic activated carbon product 126 / 216 In another embodiment, the high energy organic The compound is dissolved during carbonization of the biomass and is extracted from the gas phase separator 200 to a carbon recovery unit. 104. The enriched gas 204 may be further processed before being introduced into a carbon recovery unit or material enrichment unit. It is further concentrated with additives.

[0137] As discussed in more detail below, in various embodiments, The residence time of the biogenic activated carbon product 126 / 216 is controlled, and the biogenic activated carbon product It varies based on the composition of 126 / 216 and the gas flow and composition. In this case, the biogenic activated carbon product is passed two or more times through one or more carbon recovery units. In various embodiments, the enriched air output from the gas phase separator and the carbon recovery unit 10 The exhaust air output from 4 may be diverted or diverted to a further carbon capture unit or or further refined or used for energy or inert gases used in this process. will be done.

[0138] With more general reference to Figures 6-13, various embodiments of the present disclosure are illustrated and discussed. The various embodiments and alternatives discussed below with respect to Figures 6-13 are similar to the embodiments of Figures 1-5 described above. It should be understood that the same applies to the embodiment and vice versa.

[0139] Referring now specifically to FIG. 6, this embodiment includes a plurality of different zones, from two to more than two. A BPU may be utilized that includes a single reactor having two zones. Two zones are shown in the illustrative embodiment. Although any different number of bands may be used. is connected to at least one other zone via a material transport unit (not shown). In one embodiment, the material transport unit controls the atmospheric and temperature conditions.

[0140] In one embodiment, specifically illustrated in FIG. 6, system 600 includes a material delivery system 602, BPU 606 including pyrolysis zone 608 and cooling zone 610, cooler 614, etc. and a carbon recovery unit 616. The cooler 614 in FIG. 6 is external to the BPU 606. , it should be understood that this is in addition to the cooling zone 610 present in the BPU 606.

[0141] In various embodiments, the system 600 includes a material supply system 602 and a BPU 606 In various embodiments, the BPU 606 may include multiple zones, including an optional dryer between the zones. In Figure 6, BPU 606 includes a pyrolysis zone 608 and a cooling zone 610. The BPU 606 is configured to transport a substance containing at least condensable vapors and non-condensable gases 612 in multiple zones. to add and remove various substances from multiple zones 608, 610. In various embodiments discussed below, the system also includes at least a plurality of inlets and outlets. Thus, one or more of the multiple zones 608 or 610 are encapsulated by the BPU 606. I want you to understand that.

[0142] Referring now to Figure 7, one embodiment of a system 700 is illustrated and discussed. The system 700 includes a material supply system 702, a preheater 706, a pyrolysis reactor 708, a cooler 71, and a 4, and a single reactor system including a carbon recovery unit 716. In this case, the system 700 does not include any optional connection between the material supply system 702 and the preheater 706. As can be seen in FIG. 7, the pyrolysis reactor 708 in one embodiment includes at least At least one gas inlet 710 and at least one gas inlet 712 for outputting material from the pyrolysis reactor 708. In various embodiments, the output through the outlet 712 The materials include condensable vapors and / or non-condensable gases. One or more pyrolysis reactors 708 It should be understood that the various bands (not discussed in detail herein) may be included. In embodiments, the system 700 may include one or more reactors in addition to the pyrolysis reactor 708. include.

[0143] Referring now to FIG. 8, one embodiment of a single reactor, multi-zone BPU system 800 is illustrated. The system 800 includes a material feed system 802, a pyrolysis zone 810, and and a BPU 808 having a cooling zone 812, a material enrichment unit 818, and a carbon capture unit Similar to the embodiment described above, FIG. 8 illustrates a material supply system 802 and a BP The optional dryer 804 located between the dryer 804 and the water supply 808 is also included. It should be understood that the 06 is removed during the drying process. and an optional cooler 816 before the material concentration unit 818. The material enrichment unit 818 is in communication with the gas outlet 814 of the BPU 808 so that , conveying condensable vapors and non-condensable gases from the BPU. It should be understood that the carbon recovery unit 820 is separate from the material enrichment unit 818. As mentioned above, in various embodiments, the carbon recovery unit 820 of FIG. A suitable container in which the concentrated material is stored after unit 818 and carbon recovery unit 820 does not further concentrate the material.

[0144] In various embodiments, an optional process gas heater 824 is located in the system. , it should be understood that the BPU 808 is attached to the BPU 808. In various embodiments, Steam or other off-gas from 808 may be any of air, natural gas, and nitrogen. In addition to one or more external sources, the gas is input to an optional process gas heater 824. As such, in various embodiments, the air exhaust from the process gas heater 824 is , is input to the dryer 804 as a heat or energy recovery system.

[0145] Referring now to FIG. 9, a BPU 908 of a system 900 in one embodiment is illustrated and discussed. The BPU 908 has multiple zones: a preheat zone 904, a pyrolysis zone 910, and a cooling zone 912. In one embodiment, the BPU 908 includes one of the bands 904, 910, and 914. a material supply system 902 in communication with one or more of zones 904, 910, 914; In various embodiments, the at least one gas inlet 906 is in communication with the As can be seen, one of the zones is a zone containing a substance, in one embodiment, a condensable vapor and / or or at least one outlet 912 for outputting non-condensable gases. In this embodiment, one of the zones may be an outlet for outputting enhanced carbon from the system 900. Also includes.

[0146] While FIG. 9 shows a gas inlet 906 connected to a preheat zone 904, various embodiments may It should be understood that this includes inlets to any combination of these three zones. Although outlet 912 originates from pyrolysis zone 910, various embodiments may use any of these three zones. It should be understood that the present invention includes an exit from one or more of the following combinations: Thus, various contemplated embodiments include inputs and outputs within the BPU, e.g., thermal The outlet of the solution zone 910 then becomes the input to the preheat zone 904. In this case, the reactors in the BPU are each connected to each other via a material supply system as described above. It should be understood that they are connected.

[0147] In various embodiments, the preheat zone 904 of the BPU 908 “bombards” the biomass. configured to supply biomass 902 (or another carbon-containing feedstock) in a manner that This ruptures the cell walls and initiates the rapid decomposition of the solid phase into vapors and gases. In an embodiment, the preheat zone 904 may be considered a mild pyrolysis.

[0148] In various embodiments, the pyrolysis zone 910 of the BPU 908 is configured as the primary reaction zone. where the preheated material undergoes a pyrolysis chemical reaction releasing gases and condensable vapors. This results in solid materials that are high-carbon reaction intermediates. cellulose, and lignin) penetrate the pores or create new nanopores The latter effect is due to the effect of porosity and surface area. Contribute to the creation of

[0149] In various embodiments, the cooling zone 914 of the BPU 908 receives high-carbon reaction intermediates. and cooling the solids, i.e., the temperature of the cooling zone 914 is In the cooling zone 914, chemical reactions and mass transport are complex. In various embodiments, secondary reactions occur in the cooling zone 914. The carbon-containing components may decompose to form additional fixed carbon and / or adsorb carbon. It should be understood that the advanced carbon 916 may be simply a processing step. Rather than the solid devolatilized residue of the cap, organic vapors that can form carbon (e.g., It includes additional carbon deposited from the gas phase, such as by decomposition of carbon monoxide (tar).

[0150] 10-13, various multi-reactor embodiments of the system are illustrated and discussed. As with each embodiment, the system may include a 10, the system 1000 includes: Material supply system 1002, pyrolysis reactor 1012, cooling reactor 1018, cooler 102 0, and carbon recovery unit 1022. As discussed further below, gas source 1 1016 is a gas supply to one or both of the pyrolysis reactor 1012 and the cooling reactor 1018. In various embodiments, the pyrolysis reactor is configured to input at least and an outlet for outputting condensable vapor and / or non-condensable gas. In the present invention, the carbon recovery unit 1022 is an output unit for outputting activated carbon from the system 1000. Includes 1024 mouths.

[0151] In various embodiments illustrated in at least FIGS. 10-13, the illustrated system It should be understood that this includes an optional deaerator and an optional dryer. For example, as represented by the dashed line, optional deaerator 1004 may be connected to material feed system 1002. The pyrolysis reactor 1002 is connected to the system 1000. Similarly, the dryer 1006 connected to the system 1000 between the material supply system 1002 and the pyrolysis reactor 1012. In various embodiments, material from a material supply system is It can flow through any number of different paths through the deaerator, dryer and into the pyrolysis reactor In some embodiments, the dryer 1006 and the deaerator 1004 are also connected to each other. In this case, the material passes through only one of the optional deaerator 1004 and dryer 1006. Please understand that. In some embodiments, referring to FIG. 10, a method for producing biogenic activated carbon is provided. The process for this includes the following steps:

[0152] (a) providing a carbon-containing feedstock comprising biomass;

[0153] (b) optionally drying the feedstock to remove at least a portion of the moisture contained within the feedstock; removing the

[0154] (c) optionally degassing the feedstock to remove any grit contained within the feedstock, if any; removing at least a portion of the interatomic oxygen;

[0155] (d) heating the feedstock in the presence of a substantially inert gas phase at a temperature selected from about 250°C to about 700°C; Pyrolyze for at least 10 minutes at at least one temperature selected to obtain hot pyrolysis solids, condensed generating a condensable vapor and a non-condensable gas;

[0156] (e) removing at least a portion of the condensable vapors and at least a portion of the non-condensable gases from the hot pyrolysis solids; and separating a portion of the mixture.

[0157] (f) cooling the hot pyrolysis solid to generate a cooled pyrolysis solid;

[0158] (g) recovering the biogenic activated carbon containing at least a portion of the cooled pyrolysis solids; Tep.

[0159] Referring now to Figure 11, one embodiment of a multi-reactor system 1100 is illustrated. Similar to the embodiment discussed and illustrated in FIG. 10, this embodiment uses a material supply system The reactor 1102, pyrolysis reactor 1112, cooling reactor 1118, and carbon recovery unit 11 24. In the illustrated embodiment of FIG. 11, the cooler 1120 is optional and includes a material The concentration unit 1122 is located between the optional cooler 1120 and the carbon recovery unit 1124. In various embodiments, a material enrichment unit 1122 further enriches the material. The material is concentrated before continuing to a separate carbon recovery unit 1124 that can either be obtained or not concentrated. It should be understood that in various embodiments, the optional deaerator 1104 and the optional dryer The vessel 1106 is positioned between the material feed system 1102 and the pyrolysis reactor 1112 . In the illustrated embodiment, the pyrolysis reactor 1112 generates condensable vapors and non-condensable gases. and sending the removed material to a material concentration unit 1122. Also includes exit 1114.

[0160] Various embodiments provide for the production of carbon-containing species by subjecting cooled carbon to an environment containing the carbon-containing species. By including a separate material enrichment unit 818, 1122 that enriches the carbon content of , which expands the concept of further carbon formation. If the temperature of this unit is below the pyrolysis temperature , it is expected that the additional carbon is in the form of adsorbed carbonaceous species rather than additional fixed carbon. will be done.

[0161] As will be explained in more detail below, the intermediate addition of one or more phases present in any particular reactor may be used. Force and output (purge or probe) flows, various mass and energy recirculation schemes , various additives that can be introduced anywhere in the process, reaction conditions to adjust product distribution There are numerous options for adjusting process conditions, including both the separation and separation conditions. Zone or reactor specific input and output flows are used for FTIR sampling and dynamic probing. This allows for better process monitoring and control, such as process adjustments.

[0162] The present disclosure differs from fast pyrolysis and from conventional slow pyrolysis. The high quality carbon materials of the present disclosure, including compositions having can be obtained from

[0163] For purposes of this disclosure, "biomass" refers to any biogenic feedstock or biomass. should be interpreted as a mixture of bio- and non-biological feedstocks. The mass includes at least carbon, hydrogen, and oxygen. It can accommodate a wide range of feedstock types, sizes, and moisture contents.

[0164] Biomass includes, for example, plants and plant-derived materials, vegetation, agricultural waste, forestry waste, This includes wood waste, paper waste, animal waste, poultry waste, and municipal solid waste. In various embodiments of the present disclosure that utilize biomass, the biomass feedstock may be wood harvest. Harvest residues, softwood chips, hardwood chips, tree branches, tree stumps, knots, leaves, bark, sawdust , non-standard paper pulp, cellulose, corn, corn stover, wheat straw, rice straw , sugarcane bagasse, switchgrass, Miscanthus, livestock manure, municipal solid waste, municipal sewage, commercial waste Waste, grape pomace, almond shells, pecan shells, coconut shells, coffee grounds Grass pellets, hay pellets, wood pellets, cardboard, paper, carbohydrates, plastic The feedstock may comprise one or more materials selected from the group consisting of lacquer, plaster, and fabric. It's easy to see that the options are virtually limitless.

[0165] Various embodiments of the present disclosure are directed to biomass fuels, such as fossil fuels (e.g., coal or petroleum coke). Carbon-containing feedstocks other than biomass, or any mixture of biomass and fossil fuels (e.g., biomass, In some embodiments, biomass / coal blends are also used. Feedstocks of biomass origin include coal, oil shale, crude oil, asphalt, or solids from crude oil processing ( The feedstock is or contains waste tires, recycled plastics, etc. The materials may include recycled paper, recycled paper, and other waste or recycled materials. The method, apparatus, or system may be used with any carbonaceous feedstock. The feedstock may be a truck, train, ship, barge, tractor trailer, or any other vehicle or can be transported by any known means, such as a vehicle.

[0166] The selection of the particular feedstock(s) is not considered technically critical, but is economically The process is carried out in a manner that tends to favor the and (in some embodiments) there is no screening to remove undesired materials. The feedstock may optionally be dried before processing.

[0167] The feedstocks used may be provided or processed into a wide variety of particle sizes or shapes. For example: The feed material can be a fine powder or a mixture of fine and coarse particles. The form of material in large pieces such as chips, or other forms of wood (e.g. round, cylindrical, square) In some embodiments, the feed materials may be held together using a binder or the like. pellets or other agglomerated forms of particles pressed or otherwise bonded together include.

[0168] It should be noted that particle size reduction is an expensive and energy intensive process. can be sized with significantly lower energy input, i.e., the product rather than the feedstock Reducing the particle size can be more energy efficient, as the process This invention does not require fine starting material and there is not necessarily any particle size reduction during processing. This disclosure provides the ability to process very large fragment feedstock. Notably, in some embodiments, large fragments are sourced, produced, and sold. As mentioned above, some commercial applications of activated carbon products are actually large in size (e.g., several centimeters). Although not necessarily in all embodiments of the present disclosure, smaller Sizing results in more fixed carbon under similar process conditions, and smaller Typically requires a sized activated carbon product and / or a higher fixed carbon content It should be understood that the present invention may be utilized in a number of applications.

[0169] It is desirable to produce a final carbonaceous activated carbon product of biogenic origin that has structural integrity in the form of a cylinder or the like. If so, there are at least two options in this disclosure. First, this process The material produced from the process is collected and then further mechanically processed into the desired form. For example, the product is pressed or pelletized with a binder. Utilizing a feed material that generally retains the desired size and / or shape for the article, and In some embodiments, the object is to use processing steps that do not destroy the basic structure of the The feed and product have similar geometric shapes, such as spheres, cylinders, or cubes.

[0170] The ability to maintain the approximate shape of the feed material throughout the process is important for product strength. This control also avoids pelletizing problems with high fixed carbon materials, Save money.

[0171] The starting feedstock in various embodiments is provided with a range of moisture levels, as will be appreciated. In some embodiments, the feed material is already sufficiently dry that Further drying before pyrolysis is not required. Typically, biomass that normally contains moisture is Biomass is obtained from commercial sources and through a drying step prior to introduction into the pyrolysis reactor. However, in some embodiments, it may be desirable to provide a dried supply. In various embodiments, any biomass will work well, but the material how it was grown, harvested, irrigated, material species selection, and carbon content It should be understood that factors such as amount can affect the process and its products. In various embodiments, by using little fertilizer and phosphorus during propagation, Metal fabrication provides good properties. In various embodiments, low impact shear during harvesting. In various embodiments, less irrigation and smaller Older rings may provide greater strength.

[0172] In various embodiments, additives and / or catalysts are included in the BPU to increase the temperature within the BPU. Select a temperature profile to favor the production of carbon dioxide over carbon monoxide to minimize the It should be understood that this results in more fixed carbon.

[0173] A relatively low oxygen environment (e.g., about 10%, 5%, 3%, or First, uncontrolled combustion is a safety concern. For reasons that should be avoided in pyrolysis reactors, some amount of total carbon oxidation to CO2 The heat released by the exothermic oxidation can support the endothermic pyrolysis chemical reaction. Extensive carbon oxidation, including partial oxidation to ethane, reduces the solid carbon yield.

[0174] In effect, a strictly oxygen-free environment in each reactor(s) or BPU This limitation can be addressed, and in some embodiments In the step (a), the reactor(s) or BPU is substantially free of molecular oxygen in the gas phase. Ensure there is little or no oxygen in the reactor(s) or BPU. To achieve this, air is removed from the feed before it is introduced into the reactor(s) or BPU. It may be desirable to remove or reduce air in the feedstock. There are various ways to do this.

[0175] In some embodiments, as seen in Figures 10, 11, 12, and 13, The oxygen can be removed from the pores of the feedstock by passing through the pores. A degassing unit is utilized where the feedstock is conveyed before or after drying in the presence of another gas that Most gases with less than 21% O by volume can be used with varying degrees of effectiveness. In some embodiments, nitrogen is used. In some embodiments, CO and and / or CO2 are used. Mixtures such as nitrogen and small amounts of oxygen can also be used. Steam may be present in the degassed gas, but adding significant amounts of moisture back into the feed material should be avoided. The effluent from the degassing unit is purged (to the atmosphere or to an exhaust treatment unit). It can be obtained or recycled.

[0176] In principle, the effluent (or part of it) from the degassing unit is the acid removed from the solids. Since the oxygen is now highly diluted, it can be introduced into the pyrolysis reactor itself. In the case where the degassed effluent gas is operated in a countercurrent configuration, the degassed effluent gas is introduced into the last zone of the reactor. It may be advantageous to introduce

[0177] Various types of degassing units can be used. In one embodiment, when drying is performed Degassing after drying avoids the step of scrubbing soluble oxygen from any moisture present. In certain embodiments, the drying and degassing steps are performed in a single unit. Either a combination or a certain amount of degassing is achieved during drying.

[0178] The optionally dried and optionally degassed feedstock is fed to a pyrolysis reactor or reactors. In various embodiments, the material supply system may include, for example, Feed material using any known means, including a screw material feed system or lock hopper. In some embodiments, the material delivery system incorporates an airlock. .

[0179] If a single reactor (such as that of Figures 6, 3, or 4) is used, there may be multiple zones. Multiple zones, such as two, three, four or more zones, can improve overall process performance. To adjust the temperature, solid residence time, gas residence time, gas composition, flow pattern, and and / or may allow for individual control of pressure.

[0180] As noted above, references to a "band" refer to a single physical unit (e.g., a band in Figure 6, 8, or 9). (e.g., those in Figures 7 and 10-13), or physically separate units (e.g., those in Figures 7 and 10-13), or It should be broadly interpreted to include spatial domains in any combination. The distinction of zones within the BPU is due to the structure, e.g., the presence of flights within the BPU or the presence of separate thermal Alternatively or additionally, the heating element may be associated with a distinct heating element for providing the zones. In various embodiments, the distinction between zones within the BPU is at least one of distinct temperature It relates to functions such as fluid flow patterns, solid flow patterns, and degree of reaction. In a batch reactor, a "zone" is an operating regime in time rather than space. An embodiment includes the use of multiple batch BPUs.

[0181] It is understood that there is not necessarily an abrupt transition from one band to another. For example, the boundary between the preheating zone and the pyrolysis zone is somewhat arbitrary and may require a certain amount of heat. Solution may occur in part in the preheat zone, and some amount of "preheating" may continue to occur in the pyrolysis zone. The temperature profile in the BPU, including the zone boundaries within the zone, is typically continuous.

[0182] Some embodiments may utilize preheating and / or gentle heating, as seen, for example, in FIG. In various embodiments, a preheating zone 304 is used that operates under pyrolysis conditions. The temperature of the reaction mixture is about 80°C to about 500°C, for example, about 300°C to about 400°C. In an embodiment, the temperature in the preheat zone 304 ruptures the cell walls and releases them into steam and gases. It is not so high as to shock the biomass material to initiate rapid decomposition of the solid phase. Pyrolysis, also known as flash pyrolysis, is avoided in this disclosure.

[0183] All references herein to zone temperatures refer, in a non-limiting manner, to the bulk solids present. Temperatures that may be applied to the body, or gas phase, or reactor or BPU walls (process side) In each zone, the temperature gradient is both axial and radial. It is understood that the information exists both instantaneously and in time (i.e., upon activation or transiently). Therefore, reference to zone temperatures refers to average temperatures that may affect actual dynamics. or other effective temperature. The temperature may be measured by a thermocouple or other temperature probe. It may be measured directly by the ion exchange method or may be measured or estimated indirectly by other means.

[0184] The second zone, or primary pyrolysis zone, operates under pyrolysis or carbonization conditions. The temperatures in the region are approximately 300°C, 350°C, 400°C, 450°C, 500°C, 550°C, and 600°C. The preheating temperature may be selected from about 250°C to about 700°C, such as 650°C. The extracted biomass undergoes pyrolysis chemical reactions, releasing gases and condensable vapors, resulting in a high-carbon reaction. Leaving a significant amount of solid material as an intermediate. Biomass components (mainly cellulose, hemicellulose) The carbon nanotubes (carbon dioxide, cellulose, and lignin) penetrate the pores or create new pores. The temperature should be at least equal to the residence time in the pyrolysis zone and The reaction temperature depends on the nature of the feedstock and the product properties.

[0185] The cooling zones operate to cool the carbon-rich reaction intermediates to varying degrees. In various embodiments, the temperature of the cooling zone is lower than the temperature of the pyrolysis zone. The temperature of the zone is selected from about 100°C to about 550°C, for example, from about 150°C to about 350°C. do.

[0186] In various embodiments, the chemical reaction continues to occur in the cooling zone. It should be understood that secondary pyrolysis reactions begin in the cooling zone. The components may condense (due to the temperature drop in the cooling zone). However, the temperature Reactions that remain elevated and can form additional fixed carbon from the condensed liquid (secondary pyrolysis) ) or at least form bonds between the adsorbed species and the fixed carbon. One example reaction is the conversion of carbon monoxide to carbon dioxide and fixed carbon (the Boudouard reaction). is.

[0187] The residence time in the zones can vary. For the desired amount of pyrolysis, higher temperatures may be used to increase the reaction time. This allows for a reduction in the residence time in the continuous BPU (reactor). is the volume divided by the volumetric flow rate. The residence time in a batch reactor is the time it takes to heat up to the reaction temperature. This is the batch reaction time after

[0188] It should be recognized that in a multi-phase BPU, there are multiple residence times. In each zone, the residence time (and residence time distribution) of both the solid and vapor phases is For a given device using multiple bands, and with a given throughput, The residence time for the entire zone is generally connected on the solids side, but multiple inlet and outlet ports are provided for individual When utilized in separate zones, residence times can be decoupled on the vapor side. In this case, the solids residence time and vapor residence time are decoupled.

[0189] The residence time of the solids in the preheat zone depends on the temperature and time required to reach the preheat temperature. Depending on the situation, the time can be selected from about 5 minutes to about 60 minutes, such as about 10 minutes. The thermal conductivity, which depends on the physical device as well as the heating parameters, is calculated by preheating a solid to a predetermined temperature. This dictates the minimum residence time required to achieve this.

[0190] The solids residence time in the pyrolysis zone is about 10 minutes, such as about 20 minutes, 30 minutes, or 45 minutes. Depending on the pyrolysis temperature in this zone, the required heat transfer time can be selected from the range of 100 to 120 minutes. There should be sufficient time for the carbonization chemical reaction to occur. For times less than about 10 minutes To remove a large amount of non-carbon elements, the temperature is very high, e.g., above 700°C. This temperature is required to generate vapors and This promotes gas evolution and should be avoided if the desired product is solid carbon. be.

[0191] In the static systems of various embodiments, an equilibrium transformation is reached at a certain point in time. In some embodiments, the vapor is continuously passed over the solid, continuously removing volatiles. When flowing, the equilibrium constraint is removed, allowing pyrolysis and devolatilization, and the reaction rate is zero. Longer times may be sufficient to substantially transform the remaining refractory solids. There is no trend.

[0192] The solids residence time in the cooling zone may be, in various embodiments, from about 5 minutes to about 6 minutes, such as about 30 minutes. Depending on the cooling temperature in this zone, the carbon solid is cooled to a desired temperature. There should be enough time for the carbon to cool. The cooling rate and temperature should be adjusted accordingly. This dictates the minimum residence time required. Additional time is required before a certain amount of secondary pyrolysis is desired. In some cases, this may not be desirable.

[0193] As mentioned above, the residence time of the vapor phase can be selected and controlled separately. The residence time can be selected from about 0.1 minutes to about 10 minutes, such as about 1 minute. The residence time of the steam in the cooling zone can be selected from about 0.1 minutes to about 20 minutes, such as about 2 minutes. The vapor residence time can be selected from about 0.1 minutes to about 15 minutes, such as about 1.5 minutes. While residence time promotes rapid sweep of volatiles from the system, longer vapor residence times , promoting the reaction of the components in the vapor phase with the solid phase.

[0194] The mode of operation of the reactor and the overall system may be continuous, semi-continuous, batch, or any combination thereof. In some embodiments, the BPU is a continuous countercurrent reactor in which solids and vapor flow in substantially opposite directions. The BPU may also be operated in batch mode, for example by periodically introducing a gas phase and distributing the gas in a batch vessel. This involves simulated countercurrent flow of vapor by removing the gas phase from the

[0195] A variety of flow patterns may be desired or observed. Chemical reactions and simultaneous separations may occur in multiple zones. The fluid dynamics can be quite complex, with multiple phases involved within the solids. While the flow of steam can approach plug flow (well mixed in the radial dimension), This can approach perfectly mixed flow (in both the radial and axial dimensions). Multiple inlet and outlet ports for steam can contribute to overall mixing.

[0196] The pressure in each zone can be selected and controlled separately. The force is independently about 1 kPa to about 3000 kPa, such as about 101.3 kPa (standard atmospheric pressure). A true gas extractor for extracting gas when a zone pressure below about atmospheric pressure is desired. When multiple gas inlets and outlets, including void ports, are used, independent zone pressure control is possible. Similarly, in a multi-reactor system, the pressure in each reactor can be independently can be independently selected and controlled.

[0197] The process may, in some embodiments, be conveniently operated at atmospheric pressure. There are many advantages associated with operating at atmospheric pressure, ranging from increased comfort to improved safety. In embodiments, the pyrolysis zone is at about 90 kPa, 95 kPa, 100 kPa, 101 kPa a, operates at pressures of 102 kPa, 105 kPa, or 110 kPa (absolute).

[0198] Vacuum operation (e.g., 10-100 kPa) facilitates rapid sweeping of volatiles from the system When off-gas is supplied to high pressure operation, the pressure is higher (e.g., 100-1000 kPa) can be useful. Elevated pressure also promotes heat transfer, chemical reactions, or separations. It may be useful to

[0199] At least a portion of the condensable vapors and at least a portion of the non-condensable gases from the hot pyrolysis solids. The step of separating the A substantially inert sweep gas may be introduced into one or more of the zones. After this, the condensable vapors and non-condensable gases are carried from the zone(s) in the sweep gas and are transported to the BP Exit U.

[0200] The sweep gas may be, for example, N2, Ar, CO, CO2, H2, H2O, CH4, or other light carbon. The sweep gas may be first preheated before being introduced. or, if obtained from a heated source, possibly cooled.

[0201] The sweep gas removes volatile components from the system before they can condense or further react. By removing them, the volatile components are more completely removed. It is possible to remove volatiles at a rate faster than that obtainable from volatilization at the process temperature. Alternatively, the use of a sweep gas can be used to remove a certain amount of volatiles at a milder temperature. The reason that sweep gas improves volatile removal is that Liquid / vapor phase solution where the desorption mechanism is not simply relative volatility but rather assisted by the sweep gas. The sweep gas is used to sequentially deplete a given volatile species. This not only reduces the mass transfer limit of volatilization, but also reduces the thermodynamic limit, resulting in a more Many volatile species can be vaporized to reach thermodynamic equilibrium.

[0202] Volatile organic carbon from subsequent processing steps is removed to produce a product with high fixed carbon. It is important to remove the charged gas. Without removal, the volatile carbon will dissolve in the pyrolysis solids. adsorb or absorb the pyrolysis solids, thereby producing a purer form of carbon that may be desired. It may require additional energy (cost) to achieve this state. It is also speculated that this increases the porosity of the pyrolysis solids. In embodiments, higher porosity is desirable.

[0203] In certain embodiments, the sweep gas is used with a relatively low process pressure, such as atmospheric pressure. This provides rapid vapor removal without the need for copious amounts of inert gas.

[0204] In some embodiments, the sweep gas flows countercurrently to the flow direction of the feedstock. In other embodiments, the sweep gas flows co-currently to the feed flow direction. In this embodiment, the flow pattern of the solids approaches plug flow, while the sweep gas and gas The gas-phase flow pattern generally approaches fully mixed flow within one or more zones.

[0205] The sweep may be performed in any one or more of the bands. The sweep gas is introduced into the cooling zone and extracted from the cooling zone and / or pyrolysis zone ( In some embodiments, the sweep gas is introduced into the pyrolysis zone. In some embodiments, the oxidized carbon dioxide is introduced into the pyrolysis zone and / or extracted from the preheating zone. In this case, the sweep gas is introduced into the preheating zone and extracted from the pyrolysis zone. In an embodiment, a sweep gas is introduced into each of the preheating zone, pyrolysis zone, and cooling zone. are input and extracted from each of these bands.

[0206] In some embodiments, the zone(s) in which the separation is performed are physically separate from the BPU. Separate units or zones may be placed between the zones if desired. For example, there may be a separation unit installed between the pyrolysis zone and the cooling zone.

[0207] The sweep gas may be introduced continuously, especially if the solids flow is continuous. When operated as a sweep process, the sweep gas is introduced after a certain time or periodically. Even when the pyrolysis reaction is running continuously, the sweep gas may be , can be introduced semi-continuously or periodically, if desired, using suitable valves and controls.

[0208] The volatile-containing sweep gas may exit from one or more zones and, if obtained from multiple zones, may be combined. The resulting gas stream containing various vapors can then be mixed with the various vapors discussed above. As illustrated in FIG. 8, a process gas heater may be supplied with air to control emissions. Any known thermal oxidation unit may be used. In some embodiments, the process Natural gas and air are supplied to the gas heater to substantially destroy the volatiles contained therein. reaches a temperature sufficient for destruction.

[0209] The effluent of a process gas heater is a hot gas stream containing water, carbon dioxide, and nitrogen This eluate stream can be purged directly to the air exhaust if desired. In an embodiment, the energy content of the effluent of a process gas heater, such as a waste heat recovery unit. The energy content can also be recovered by heat exchange with another stream (such as a sweep gas). The energy content can be calculated by dividing the energy content by the unit elsewhere in the process, such as a dryer or reactor. May be utilized by providing or assisting in direct or indirect heating In some embodiments, due to the indirect heating of the dryer (a practical aspect), essentially all The effluent of all process gas heaters is used. The process gas heaters are Other fuels can be used instead.

[0210] The yield of carbonaceous materials varies depending on the factors mentioned above, including the type of feedstock and process conditions. In some embodiments, the net yield of solids as a percentage of the starting feedstock can be , on a dry basis, at least 25%, 30%, 35%, 40%, 45%, 50%, or The rest are terpenes, tars, alcohols, acids, aldehydes, or ketones. Condensable vapors such as benzene and non-condensable gases such as carbon monoxide, hydrogen, carbon dioxide, and methane. The relative amount of condensable vapor compared to non-condensable gases, including water, present is also In some embodiments, the incorporation of additives prior to the pyrolysis step is dependent on the process conditions. This is the same process where additives are added after the pyrolysis step (if at all). In some embodiments, the additive (e.g., Halogen-containing additives are added to moisten the biomass and / or After drying the gas but before pyrolysis, the carbonaceous material (e.g., biogenic activated carbon) The resulting mass yield is determined by either (i) not adding at any time, or (ii) Biogenic activated carbon added after pyrolysis but by an otherwise identical process This exceeds the mass yield of the additive produced.

[0211] In terms of carbon balance, in some embodiments, the percentage of starting carbon in the feedstock The net yield of carbon as a %, or more. For example, in some embodiments, the carbonaceous material may be It contains about 40% to about 70% of the carbon contained in the feedstock. The remaining carbon is To a certain extent, methane, carbon monoxide, carbon dioxide, light hydrocarbons, aromatics, tar, terpenes, This results in the formation of an alcohol, acid, aldehyde, or ketone.

[0212] In an alternative embodiment, some of these compounds are combined with carbon-rich solids. In these embodiments, various Some or all of the resulting gas stream from the reactor containing the vapor is at least The cooled water is also partially condensed and then cooled from the cooling zone and / or a separate cooler. These embodiments are described in more detail below.

[0213] After reaction and cooling in the cooling zone (if present), the carbonaceous solids are introduced into a cooler. In some embodiments, the solid is collected and simply cooled at a slow rate. If the solid is reactive or unstable in air, maintain an inert atmosphere and / or Alternatively, it may be desirable to rapidly cool the solid to a temperature below about 40°C, e.g., ambient temperature. In some embodiments, a water quench is used to rapidly cool the In some embodiments, a fluidized bed cooler is used. The term "pipe," as used herein, should be broadly interpreted to include any pipe, tank, or part thereof. It is understood that a condenser is distinct in form from a cooling unit or cooling reactor. I want to be understood.

[0214] In some embodiments, the process further comprises cooling the warm pyrolysis solids with steam. operating a cooler to thereby generate cold pyrolysis solids and superheated steam. The drying is carried out at least in part with superheated steam obtained from the cooler. The cooler first cools the warm pyrolysis solids with steam to reach the first cooler temperature, and then , and operates to cool with air to reach a second cooler temperature, the second cooler temperature being Reduced flammability risk of warm pyrolysis solids in the presence of air below a cooler temperature of 1 is related to.

[0215] After cooling to ambient conditions, the carbonaceous solids are recovered, stored, and transported to another operating location. be transferred to another location or otherwise disposed of, traded, or sold. Solids can be fed into units to reduce particle size. Mills, shredders Various particle sizes, including grinders, pulverizers, jet mills, pin mills, and ball mills Depletion units are known in the art.

[0216] Screening or some other means for separation based on particle size may be included. Cleaning, if present, can be upstream or downstream of grinding. Some of the material (e.g., large chunks) may be returned to the grinding unit. The cooled effluent may be recovered for separate downstream uses. The resulting pyrolysis solids may be milled into a fine powder, such as a pulverized carbon or activated carbon product, or may be further crushed into a powder. Increase the degree.

[0217] Various additives may be added to the process before, during, or after any of the steps disclosed herein. Additives can be introduced throughout the process, depending on process characteristics such as carbon yield or pyrolysis time / temperature. Process additives selected to improve performance and achieve the desired carbon purity, and bio-initiated The source of activated carbon or a reagent incorporating the activated carbon is selected to improve one or more properties of the downstream product. Certain additives can be broadly classified as process additives, depending on the amount of biomass feedstock. Enhanced process and product properties, including overall yield, of the compared biogenic activated carbon products may be provided.

[0218] Additives may be added at any suitable point during the overall process. The additive may be added before, during, or after the step of drying the feedstock; before, during, or after the pyrolysis step; before, during, or after the separation step; before, during, or after any cooling step; before, during, or after the biogenic activated carbon recovery step before, during, or after the micronization step; before, during, or after the sizing step and / or may be added before, during, or after the packaging step. Additives are transported through feedstock supply equipment, transport trucks, unloading equipment, storage bins, conveyors ( (including open or closed conveyors), dryers, process heaters, or any other unit The additives may be incorporated into or onto the surface of the polymer using any suitable means for introducing the additive. Additives can be added anywhere during the pyrolysis process itself, if desired, after carbonization or Or even after micronization it can be added.

[0219] Thus, one example of a single reactor biomass processing unit consistent with the present disclosure is shown in FIG. The unit 2100 includes a hopper 2104 into which a feedstock 2102 is fed. The hopper 2104 transfers the feedstock 2102 to the reactor 2112 before transporting the feedstock 2102 to the reactor 2112. 2 from the reactor off-gas (e.g., vapor stream 2114) and / or from an external source 2162 Optionally configured to allow for the addition and / or mixing of additives and / or gases The activated carbon 2126 is mechanically transported through the reactor 2112 before exiting the opposite end. Steam, nitrogen, carbon dioxide, or a combination thereof 2152 is used to The vapor stream 2114 is introduced into the reactor 2112 in a countercurrent manner to the passage. 2 and into a hopper 2104 and then into a thermal oxidizer 2124. Optionally, a heat exchanger 2154 is provided to exchange heat from the thermal oxidizer effluent with gas stream 2158. This gas stream 2158 may contain nitrogen and / or carbon dioxide. Gas stream 2158, or a portion thereof, is passed through passage 2160 to reactor 2112, or and / or optionally recycled to the feedstock 2102 before entering the reactor 2112 (as shown). The off-gas 2156 can be disposed of according to standard methods, for example, through a stack. do.

[0220] The embodiment shown in FIG. 22 is a two-reactor biomass processing unit consistent with the present disclosure. The unit 2200 is similar to the processing unit 2100 described above with respect to FIG. It includes a substantially similarly configured first multizone reactor unit 2212A. In this embodiment, the biogenic activated carbon 222 produced by reactor 2212A At least a portion of 6A passes through passage 2202 into hopper 2204 and then into a second reaction vessel 2206. The first reactor 2212A, the thermal oxidizer 2224, and the heat exchanger 2212B are connected to the first reactor 2212A. Optionally, the thermally oxidized and optionally conditioned steam stream 226 produced by the converter 2254 At least a portion of the 2212C is fed countercurrently to the second reactor 2212B. At least a portion of the off-gas from reactor 2212B is recycled via passage 2272. Alternatively, or in addition, the second reactor 2212B may be recycled as heat. The portion of the off-gas that is not recycled is discarded, for example, by the stack via passage 2256B. The biogenic activated carbon product can exit the second reactor 2212B via passage 2226B. Come out.

[0221] In these or other embodiments, the present disclosure provides a method for producing biogenic activated carbon. provides a follow-up process, which (a) providing a starting carbon-containing feedstock comprising biomass; , (b) optionally drying said feedstock; removing at least a portion of the moisture; (c) in one or more indirectly heated reaction zones, The feedstock is mechanically conveyed, and the feedstock is mixed with a vapor stream containing a substantially inert gas and and an activator containing at least one of water and carbon dioxide in countercurrent flow. generating solids, condensable vapors, and non-condensable gases (including the aforementioned condensable vapors and the aforementioned of non-condensable gases enter the aforementioned vapor stream), (d) removing at least a portion of said vapor stream from said reaction zone. generating a separated vapor stream; (e) any of the foregoing separated vapor streams or thermally treated forms thereof. to said feedstock prior to step (c) and / or to said reaction recirculating the gas to the gas inlet of the zone(s); (f) removing the activated carbon from the reaction zone(s) as biogenic activated carbon; and recovering at least a portion of said solids.

[0222] In some embodiments, removing at least a portion of the moisture contained within the feedstock. For example, the feedstock may contain about 8% by weight or about 4% by weight of hydroxybenzoates. It can be dried to contain less than about 12% moisture by weight, such as: In embodiments, no further water is added to the feedstock. It may contain water derived from the moisture contained in the ingredients.

[0223] In some embodiments, the activating agent comprises both water and carbon dioxide. The carbon dioxide ratio can be optimized to increase activation of the solids.

[0224] At least one of the indirectly heated reaction zones is preferably heated to a temperature of from about 700°C to about All of the indirectly heated reaction zones are maintained at a reaction temperature selected from In some embodiments, the reaction temperature is maintained at a maximum of about 950° C. or less.

[0225] In some embodiments, step (d) comprises removing at least one of the condensable vapors from the reaction zone. In some embodiments, step (d) comprises removing a portion of the reaction zone. This includes removing all of the vapor flow from the area.

[0226] In some embodiments, step (e) comprises adding to the gas inlet of the reaction zone, and / or or introducing at least a portion of the separated vapor stream into the feedstock prior to step (c). In some embodiments, step (e) comprises adding a gas to the gas inlet of the reaction zone. and / or adding at least one of the separated vapor streams to the feedstock prior to step (c). This includes incorporating some thermally processed forms.

[0227] In some embodiments, step (e) comprises separating the separated vapor stream or its thermally In some embodiments, the process further comprises further heating the processed form. Step (e) adjusts the gas composition of the separated vapor stream or its thermally treated form. The adjustment of the gas composition further includes adjusting the gas composition by selecting from the group consisting of water, carbon dioxide, nitrogen, and oxygen. The method may include introducing one or more species selected from the group consisting of:

[0228] In some embodiments, the adjusted gas composition may be between 0% and 100% water, e.g., Approximately 0%, approximately 1%, approximately 2%, approximately 3%, approximately 4%, approximately 5%, approximately 6%, approximately 7%, approximately 8%, approximately 9%, Approximately 10%, approximately 11%, approximately 12%, approximately 13%, approximately 14%, approximately 15%, approximately 16%, approximately 17%, Approximately 18%, approximately 19%, approximately 20%, approximately 21%, approximately 22%, approximately 23%, approximately 24%, approximately 25%, Approximately 26%, approximately 27%, approximately 28%, approximately 29%, approximately 30%, approximately 31%, approximately 32%, approximately 33%, Approximately 34%, approximately 35%, approximately 36%, approximately 37%, approximately 38%, approximately 39%, approximately 40%, approximately 41%, Approximately 42%, approximately 43%, approximately 44%, approximately 45%, approximately 46%, approximately 47%, approximately 48%, approximately 49%, Approximately 50%, approximately 51%, approximately 52%, approximately 53%, approximately 54%, approximately 55%, approximately 56%, approximately 57%, Approximately 58%, approximately 59%, approximately 60%, approximately 61%, approximately 62%, approximately 63%, approximately 64%, approximately 65%, Approximately 66%, approximately 67%, approximately 68%, approximately 69%, approximately 70%, approximately 71%, approximately 72%, approximately 73%, Approximately 74%, approximately 75%, approximately 76%, approximately 77%, approximately 78%, approximately 79%, approximately 80%, approximately 81%, Approximately 82%, approximately 83%, approximately 84%, approximately 85%, approximately 86%, approximately 87%, approximately 88%, approximately 89%, Approximately 90%, approximately 91%, approximately 92%, approximately 93%, approximately 94%, approximately 95%, approximately 96%, approximately 97%, It contains about 98%, about 99%, or about 100% water.

[0229] In some embodiments, the adjusted gas composition is 0% to 100% carbon dioxide, For example, about 0%, about 1%, about 2%, about 3%, about 4%, about 5%, about 6%, about 7%, about 8%, Approximately 9%, approximately 10%, approximately 11%, approximately 12%, approximately 13%, approximately 14%, approximately 15%, approximately 16%, approximately 17%, approximately 18%, approximately 19%, approximately 20%, approximately 21%, approximately 22%, approximately 23%, approximately 24%, approximately 25%, approximately 26%, approximately 27%, approximately 28%, approximately 29%, approximately 30%, approximately 31%, approximately 32%, approximately 33%, approximately 34%, approximately 35%, approximately 36%, approximately 37%, approximately 38%, approximately 39%, approximately 40%, approximately 41%, approximately 42%, approximately 43%, approximately 44%, approximately 45%, approximately 46%, approximately 47%, approximately 48%, approximately 49%, approximately 50%, approximately 51%, approximately 52%, approximately 53%, approximately 54%, approximately 55%, approximately 56%, approximately 57%, approximately 58%, approximately 59%, approximately 60%, approximately 61%, approximately 62%, approximately 63%, approximately 64%, approximately 65%, approximately 66%, approximately 67%, approximately 68%, approximately 69%, approximately 70%, approximately 71%, approximately 72%, approximately 73%, approximately 74%, approximately 75%, approximately 76%, approximately 77%, approximately 78%, approximately 79%, approximately 80%, approximately 81%, approximately 82%, approximately 83%, approximately 84%, approximately 85%, approximately 86%, approximately 87%, approximately 88%, approximately 89%, approximately 90%, approximately 91%, approximately 92%, approximately 93%, approximately 94%, approximately 95%, approximately 96%, approximately It contains 97%, about 98%, about 99%, or about 100% carbon dioxide.

[0230] In some embodiments, the adjusted gas composition is between 0% and 100% nitrogen, e.g. ,approximately 0%,approximately 1%,approximately 2%,approximately 3%,approximately 4%,approximately 5%,approximately 6%,approximately 7%,approximately 8%,approximately 9% , about 10%, about 11%, about 12%, about 13%, about 14%, about 15%, about 16%, about 17% , about 18%, about 19%, about 20%, about 21%, about 22%, about 23%, about 24%, about 25% , about 26%, about 27%, about 28%, about 29%, about 30%, about 31%, about 32%, about 33% , about 34%, about 35%, about 36%, about 37%, about 38%, about 39%, about 40%, about 41% , about 42%, about 43%, about 44%, about 45%, about 46%, about 47%, about 48%, about 49% , about 50%, about 51%, about 52%, about 53%, about 54%, about 55%, about 56%, about 57% , about 58%, about 59%, about 60%, about 61%, about 62%, about 63%, about 64%, about 65% , about 66%, about 67%, about 68%, about 69%, about 70%, about 71%, about 72%, about 73% , about 74%, about 75%, about 76%, about 77%, about 78%, about 79%, about 80%, about 81% , about 82%, about 83%, about 84%, about 85%, about 86%, about 87%, about 88%, about 89% , about 90%, about 91%, about 92%, about 93%, about 94%, about 95%, about 96%, about 97% , about 98%, about 99%, or about 100% nitrogen.

[0231] In some embodiments, the adjusted gas composition may be between 0% and 100% oxygen, e.g. ,approximately 0%,approximately 1%,approximately 2%,approximately 3%,approximately 4%,approximately 5%,approximately 6%,approximately 7%,approximately 8%,approximately 9% , about 10%, about 11%, about 12%, about 13%, about 14%, about 15%, about 16%, about 17% , about 18%, about 19%, about 20%, about 21%, about 22%, about 23%, about 24%, about 25% , about 26%, about 27%, about 28%, about 29%, about 30%, about 31%, about 32%, about 33% , about 34%, about 35%, about 36%, about 37%, about 38%, about 39%, about 40%, about 41% , about 42%, about 43%, about 44%, about 45%, about 46%, about 47%, about 48%, about 49% , about 50%, about 51%, about 52%, about 53%, about 54%, about 55%, about 56%, about 57% , about 58%, about 59%, about 60%, about 61%, about 62%, about 63%, about 64%, about 65% , about 66%, about 67%, about 68%, about 69%, about 70%, about 71%, about 72%, about 73% , about 74%, about 75%, about 76%, about 77%, about 78%, about 79%, about 80%, about 81% , about 82%, about 83%, about 84%, about 85%, about 86%, about 87%, about 88%, about 89% , about 90%, about 91%, about 92%, about 93%, about 94%, about 95%, about 96%, about 97% , about 98%, about 99%, or about 100% oxygen. The adjusted gas composition is about 16% or less, about 14% or less, about 12% or less, about 10% or less, about Contains no more than 8%, no more than about 6%, no more than about 4%, or no more than about 2% oxygen.

[0232] The separated vapor stream or its thermally treated form may contain less than about 1% by weight of total , 0.2, 0.5, or 0.8% by weight, etc.) of carbon monoxide and VOC content The gas composition may be adjusted to include, or contain, at least At least about 70% by weight of nitrogen, at least about 75% nitrogen, at least about 80% nitrogen, at least about 85% nitrogen, at least about 90% nitrogen, at least about 95% nitrogen, or about 10 It can be adjusted to contain 0% nitrogen.

[0233] At least a portion of the separated vapor stream or a thermally treated form thereof is subjected to a first a delivery system configured to mechanically feed the feedstock to the indirectly heated reaction zone; Such delivery systems may include, for example, a feed auger or screw. obtain.

[0234] In some embodiments, at least a portion of the activator is added to a separated vapor stream. or from a thermally treated form thereof. Step (e) determines the yield of carbon in the solid. Furthermore, step (e) preferably increases the surface area and iodine number of the solid. In some embodiments, step (f) may include using a biogenic activated carbon. and recovering all of the solids from the reaction zone by

[0235] Additives may optionally be introduced before, during, or after one or more of steps (a) through (f). The additives are acids, bases, salts, metals, metal oxides, metal hydroxides, metal halides. The additive is selected from the group consisting of magnesium, iodine, iodine compounds, and combinations thereof. Sium, manganese, aluminum, nickel, iron, chromium, silicon, boron, cerium, Molybdenum, phosphorus, tungsten, vanadium, iron chloride, iron bromide, magnesium oxide, Lomite, dolomitic lime, fluorite, fluorospar, bentonite, calcium oxide Aluminium, lime, sodium hydroxide, potassium hydroxide, hydrogen bromide, hydrogen chloride, sodium silicate ammonium nitrate, potassium permanganate, organic acids, iodine, iodine compounds, and combinations thereof may be selected from the group consisting of:

[0236] The biogenic activated carbon has at least about 500, 1000, 1500, or 2000 yo The biogenic activated carbon may be characterized by a urea value of at least about 1000 m 2 / g, 1500 m 2 / g, 2000m 2 / g or more.

[0237] In some embodiments, at least a portion of the biogenic activated carbon is in the form of graphene. Biogenic activated carbon can respond to an externally applied magnetic field. The source activated carbon has a higher electrical conductivity and / or capacitance than the starting carbon-containing feedstock. It is possible.

[0238] In some embodiments, the biogenic activated carbon is responsive to an externally applied magnetic field. In some embodiments, the magnetic properties of the biogenic activated carbon are at least in part due to In another embodiment, the magnetic field is due to the presence of a magnetic metal, such as iron, or a compound thereof. The carbonaceous material may contain iron, iron compounds, other magnetic metals or their compounds, ores, metalloids or their compounds. the existence of a compound or another non-graphene material that itself responds to an externally applied magnetic field Nevertheless, it responds to an externally applied magnetic field. In this study, biogenic activated carbon was used to remove iron, iron compounds, other magnetic metals or their compounds, ores, semi-conductors, and other metals. A metal or its compound, or another non-metallic material that responds to an externally applied magnetic field. The nanowires respond to an externally applied magnetic field beyond the extent that can be attributed to the presence of the nanowire material.

[0239] In certain embodiments, the process involves depositing graphene on a substrate in two or three dimensions. of the separated vapor stream or its thermally treated form into the reactor to grow In such a process, the method further comprises introducing at least a portion of The carbon contained therein is deposited on a substrate (such as silicon) to form a monolayer of carbon. or a three-dimensional object.

[0240] The liquid or vapor stream from the external source can vary widely. Exemplary vapor streams include CO, CO2 , CH4, light hydrocarbons, tar, etc. An exemplary liquid stream may contain heavier hydrocarbons (o olefins or aromatics), methanol, ethanol, or heavier alcohols, External sources may include, for example, adjacent or co-located It can be a VOC off-gas stream from a chemical or fuel plant, as well as a liquid / vapor stream. External sources and recirculated gases within the system, i.e., separated vapor streams or their thermal equivalents. Combinations are also possible, including mixtures in processed form.

[0241] In some embodiments, the present disclosure provides a continuous process for producing graphene. This process provides

[0242] (a) providing a starting carbon-containing feedstock comprising biomass; ,

[0243] (b) optionally drying said feedstock; removing at least a portion of the moisture;

[0244] (c) in one or more indirectly heated reaction zones, The feedstock is mechanically conveyed, and the feedstock is mixed with a vapor stream containing a substantially inert gas and and an activator containing at least one of water and carbon dioxide in countercurrent flow. generating solids, condensable vapors, and non-condensable gases (including the aforementioned condensable vapors and the aforementioned of non-condensable gases enter the aforementioned vapor stream),

[0245] (d) removing at least a portion of said vapor stream from said reaction zone. generating a separated vapor stream;

[0246] (e) any of the foregoing separated vapor streams or thermally treated forms thereof. to said feedstock prior to step (c) and / or to said reaction recirculating the gas to the gas inlet of the zone(s);

[0247] (f) removing the solid from the reaction zone(s) as graphene; and recovering at least a portion of the body.

[0248] In some embodiments, the solid recovered in step (f) comprises a graphene-containing The graphene-containing biogenic activated carbon is For example, the graphene in biogenic activated carbon may contain fractions of graphene that differ significantly compared to the graphene in activated carbon. The mass (or molar) ratio of carbon present as phenes to total carbon is about 0.0001 to about 1, For example, about 0.001, about 0.005, about 0.01, about 0.005, about 0.1, about 0.1 5, approx. 0.2, approx. 0.25, approx. 0.3, approx. 0.4, approx. 0.5, approx. 0.6, approx. 0.7, approx. 0 It can be 0.8, about 0.9, about 0.95, or even higher.

[0249] It should also be noted that graphene content is not necessarily uniform throughout the biogenic activated carbon. In some embodiments, (without being limited by the hypothesis) The enzymes are grown from pyrolyzed feedstock or carbon-containing vapors passing through pyrolyzed feedstock. It is believed that graphene may reside primarily at or near the surface of the resulting solid. In other embodiments, sufficient heat and mass transport into the solid can result in graphene Formation can occur essentially throughout the solid.

[0250] The process further separates graphene from the graphene-containing biogenic activated carbon. Separation can be achieved by mechanical means such as a centrifuge, a magnetic separator, or an electrostatic precipitator, respectively. This may be achieved by optical, magnetic, or electrical means.

[0251] In some embodiments, the solid is further treated to increase the graphene content in the solid. For example, a catalyst can be introduced to enhance graphene growth. to fabricate or transfer graphene onto a substrate or device. It can be done.

[0252] In some embodiments, the external source of carbon increases the surface area and / or These are introduced to increase the yield and / or increase the graphene content. In some of the embodiments, a continuous process for producing biogenic activated carbon teeth,

[0253] (a) providing a starting carbon-containing feedstock comprising biomass; And,

[0254] (b) optionally drying said feedstock to obtain said feedstock; removing at least a portion of the moisture from the

[0255] (c) in one or more indirectly heated reaction zones, a vapor stream comprising a substantially inert gas; and countercurrently contacting the mixture with an activator comprising at least one of water and carbon dioxide. , solids, condensable vapors, and non-condensable gases (as described above, condensable vapors and (The non-condensable gases enter the vapor stream.)

[0256] (d) removing at least a portion of said vapor stream from said reaction zone; removing the vapor to generate a separated vapor stream;

[0257] (e) any of said separated vapor streams or their thermally treated forms. at least a portion of the form into said feedstock prior to step (c) and / or recirculating the gas to the gas inlet of the reaction zone(s);

[0258] (f) removing at least one of said solids from said reaction zone(s); and recovering at least a portion of the solid, said solid comprising graphene-containing biogenic activated carbon. nothing.

[0259] In one embodiment, a continuous process for producing graphene-containing biogenic activated carbon is provided. S,

[0260] (a) providing a starting carbon-containing feedstock comprising biomass; And,

[0261] (b) optionally drying said feedstock to obtain said feedstock; removing at least a portion of the moisture from the

[0262] (c) in one or more indirectly heated reaction zones, a vapor stream comprising a substantially inert gas; and countercurrently contacting the mixture with an activator comprising at least one of water and carbon dioxide. , solids, condensable vapors, and non-condensable gases (as described above, condensable vapors and (The non-condensable gases enter the vapor stream.)

[0263] (d) removing at least a portion of said vapor stream from said reaction zone; removing the vapor to generate a separated vapor stream;

[0264] (e) any of said separated vapor streams or their thermally treated forms. at least a portion of the form into said feedstock prior to step (c) and / or recirculating the gas to the gas inlet of the reaction zone(s);

[0265] (f) removing at least one of said solids from said reaction zone(s); and recovering at least a portion of the solid, said solid comprising graphene-containing biogenic activated carbon. nothing.

[0266] In some embodiments, the process further comprises treating the solids recovered in step (f). In some embodiments, the method further comprises: The process may further comprise using at least a portion of the solid recovered in step (f) to form a substrate or device. The method further includes fabricating graphene on the chair.

[0267] In some embodiments, graphene or graphene-containing biogenic activated carbon is , responding to an externally applied magnetic field. In some embodiments, graphene or Graphene-containing biogenic activated carbons have electrical conductivity values ​​and / or conductivity values ​​that exceed those of carbon-containing feedstocks. Or has a capacitance value.

[0268] In some embodiments, the present disclosure provides a method for producing graphene-containing biogenic activated carbon. a continuous process for producing a cellulose acetate solution, the process comprising:

[0269] (a) providing a starting carbon-containing feedstock comprising biomass;

[0270] (b) optionally drying said feedstock to remove at least a portion of the moisture from said feedstock; and

[0271] (c) mechanically moving said feedstocks through one or more indirectly heated reaction zones; and mixing the feedstock with a vapor stream containing a substantially inert gas and water or carbon dioxide. and a countercurrent activator containing at least one of a solid, a condensable vapor, and and non-condensable gases (the aforementioned condensable vapors and the aforementioned non-condensable gases are into the steam stream),

[0272] (d) removing at least a portion of said vapor stream from said reaction zone to form a separated vapor generating a flow;

[0273] (e) treating at least a portion of said separated vapor stream or a thermally treated form thereof; to said feedstock and / or to the gases of said reaction zone(s) prior to step (c). recirculating the carbon dioxide gas to the inlet to increase the surface area of ​​the carbon in said solid;

[0274] (f) removing at least one of said solids from said reaction zone(s) as biogenic activated carbon; and recovering a portion of the biogenic activated carbon, said biogenic activated carbon comprising, on a dry basis, about 55% by weight of the activated carbon. or more total carbon, about 15% by weight or less hydrogen, and about 1% by weight or less nitrogen, At least a portion of the biogenic activated carbon is present in the form of graphene, and the biogenic activated carbon is The charcoal composition is characterized by an iodine value greater than about 500, and the biogenic activated charcoal is Responds to an applied magnetic field from

[0275] In some variations, the present disclosure provides a process for producing a biogenic activated carbon product. This process provides

[0276] (a) providing a carbon-containing feedstock comprising biomass;

[0277] (a') adding an additive to said feedstock to produce an enriched feedstock; ,

[0278] (b) optionally drying the fortified feedstock to produce a dried fortified feedstock; To do,

[0279] (c) optionally degassing the fortified feedstock or the dried fortified feedstock; If present, it may be present in the fortified feedstock or in the dry fortified feedstock. removing at least a portion of the interstitial oxygen;

[0280] (d) in a pyrolysis zone, step (a') in the presence of a substantially inert gas, (b), or (c), or any combination thereof. The feedstock is subjected to pyrolysis at a temperature selected from about 250°C to about 700°C for at least about 10 minutes. pyrolysis to generate hot pyrolysis solids, condensable vapors, and non-condensable gases;

[0281] (e) removing at least a portion of the condensable vapors and at least a portion of the non-condensable gases from the hot pyrolysis solids; and to separate a part of it.

[0282] (f) In a cooling zone, the hot pyrolysis solid is cooled to about 1000 K in the presence of a substantially inert gas. Cool at a cooling zone temperature below the decomposition temperature for at least about 5 minutes to generate warm pyrolysis solids. And,

[0283] (g) Further cooling of the warm pyrolysis solids in an optional cooler separate from the cooling zone. generating a cold pyrolysis solid;

[0284] (h) of biogenic origin, containing at least a portion of warm pyrolytic or cold pyrolytic solids; recovering the activated carbon product;

[0285] (i) micronizing the biogenic activated carbon composition to form the biogenic activated carbon composition; and reducing the average particle size of the

[0286] Some embodiments provide a process for producing a biogenic activated carbon composition, comprising: This process is

[0287] (a) providing a carbon-containing feedstock comprising biomass;

[0288] (a') adding an additive to said feedstock to produce an enriched feedstock; ,

[0289] (b) optionally drying the fortified feedstock to produce a dried fortified feedstock; To do,

[0290] (c) optionally degassing the fortified feedstock or the dried fortified feedstock; If present, it may be present in the fortified feedstock or in the dry fortified feedstock. removing at least a portion of the interstitial oxygen;

[0291] (d) in a pyrolysis zone, step (a') in the presence of a substantially inert gas, (b), or (c), or any combination thereof. The feedstock is heated at a pyrolysis temperature selected from about 250°C to about 700°C for at least 10 minutes. decomposing to generate hot pyrolysis solids, condensable vapors, and non-condensable gases;

[0292] (e) removing from said hot pyrolysis solids at least a portion of said condensable vapors and said non-condensable vapors; Separating at least a portion of the condensable gas;

[0293] (f) in a cooling zone, in the presence of said substantially inert gas, The solution is cooled to a temperature below the aforementioned pyrolysis temperature for at least 5 minutes to form a warm pyrolysis solution. generating a solid;

[0294] (g) cooling said warm pyrolysis solids in any cooler separate from said cooling zone; Instead, generating a cold pyrolysis solid;

[0295] (h) recovering a biogenic activated carbon composition containing at least a portion of said cold pyrolysis solids; To collect and

[0296] (i) micronizing the biogenic activated carbon composition to form the biogenic activated carbon composition; and reducing the average particle size of the

[0297] In some embodiments, the process may further comprise adding an additive prior to the pyrolysis step. In such an embodiment, the resulting biogenic activated carbon comprises an additive. produced without or with additives added during or after the pyrolysis step, Can be produced in higher mass yields than biogenic activated carbon produced by otherwise identical methods In a related embodiment, the biogenic activated carbon product is a comparable biogenic activated carbon product. In some embodiments, the process produces a biogenic activated carbon product when additives are added before the pyrolysis step In some embodiments, the result is a much lower energy input. The resulting biogenic activated carbon is free of additives (either added during or after the pyrolysis step). (with added additives) but produced by an otherwise identical process It has a higher fixed carbon content compared to biogenic activated carbon. In this case, the additives were the same except that the additives were added during or after the pyrolysis step. Compared to process-produced biogenic activated carbon, the overall In some embodiments, the bioavailability of the biomolecules is such that the bioavailability of the biomolecules is more complete and / or uniformly distributed. The activated carbons were otherwise identical except that the additive was added either before or after the pyrolysis step. Compared with biogenic activated carbon produced by a single process, the When combined, fewer additives are required to achieve the desired performance characteristics.

[0298] In some embodiments, the additive is a metal, a metal oxide, a metal hydroxide, or For example, the additive may be magnesium, manganese, aluminum, or a combination thereof. Sodium, nickel, chromium, silicon, boron, cerium, molybdenum, phosphorus, tungste Vanadium, iron halide, iron chloride, iron bromide, magnesium oxide, dolomite, dolomite Lomite lime, fluorite, fluorospar, bentonite, calcium oxide, lime, and combinations thereof, but are in no way limited to these.

[0299] In some embodiments, the additive is selected from an acid, a base, or a salt thereof. For example, additives include sodium hydroxide, potassium hydroxide, magnesium oxide, hydrogen bromide, salt Hydrogen chloride, sodium silicate, potassium permanganate, organic acids (e.g., citric acid), or may be selected from, but is in no way limited to, these combinations.

[0300] In some embodiments, the additive is selected from a metal halide. Halides are compounds formed between metals and halogens (fluorine, chlorine, bromine, iodine, and astatine). Halogens can form many compounds with metals. Halides are generally formed by direct combination of a basic metal salt with a hydrohalic acid, or by a more Generally, it is obtained by neutralization. In some embodiments, the additive is an iron halide. Iron chloride (FeCl2 and / or Fe Cl3), iron bromide (FeBr2 and / or FeBr3), or hydrates thereof; and any combination thereof.

[0301] In some variations, the biogenic activated carbon composition comprises, on a dry basis: include:

[0302] 55% by weight or more total carbon;

[0303] 15% by weight or less of hydrogen,

[0304] not more than 1% by weight of nitrogen;

[0305] not more than 0.5% by weight of phosphorus;

[0306] not more than 0.2% by weight of sulfur;

[0307] Acids, bases, salts, metals, metal oxides, metal hydroxides, metal halides, iodine, iodine The additive is selected from the group consisting of:

[0308] In some embodiments, the additive is iodine or an iodine compound, or iodine and one or more iodine compounds. When the additive contains iodine, it is Absorbed or intercalated molecules I2, physically or chemically adsorbed molecules I2, absorbed or is an intercalated atom I, a physically or chemically adsorbed atom I, or any combination of these. A combination of these may be present in the biogenic activated carbon composition.

[0309] When the additive contains one or more iodine compounds, these may include iodide ion, hydrogen iodide, , iodide salts, metal iodides, ammonium iodide, iodine oxide, triiodide ion, triiodide Iodide salts, metal triiodides, ammonium triiodide, iodate ion, iodate salts, phosphate Iodide, iodoform, iodic acid, methyl iodide, iodinated hydrocarbons, periodic acid, Periodic acid, metaperiodic acid, and combinations thereof, salts, acids, bases, or derivatives thereof The conductive material may be selected from the group consisting of conductors.

[0310] In some variations, the biogenic activated carbon composition is prepared by at least the following steps: Generated by processes including:

[0311] (a) providing a carbon-containing feedstock comprising biomass;

[0312] (b) optionally drying the feedstock to remove at least a portion of the moisture contained within the feedstock; removing the

[0313] (c) optionally degassing the feedstock to remove any grit contained within the feedstock, if any; removing at least a portion of the interatomic oxygen;

[0314] (d) in a pyrolysis zone, in the presence of a substantially inert gas, Hot pyrolysis is carried out at a pyrolysis temperature selected from 700°C to about 700°C for at least 10 minutes. generating solids, condensable vapors, and non-condensable gases;

[0315] (e) removing at least a portion of the condensable vapors and at least a portion of the non-condensable gases from the hot pyrolysis solids; and separating a portion of the mixture.

[0316] (f) in a cooling zone, in the presence of a substantially inert gas, the hot pyrolysis solid is cooled to about 1000 K. Cool below the decomposition temperature for at least 5 minutes to generate a warm pyrolysis solid. Tep and

[0317] (g) In a cooling unit separate from the cooling zone, the warm pyrolysis solids are cooled to a cool temperature. generating pyrolysis solids;

[0318] (h) recovering a biogenic activated carbon composition comprising at least a portion of the cold pyrolysis solids. Steps and

[0319] (i) micronizing the biogenic activated carbon composition to reduce the average particle size of the biogenic activated carbon composition; The reducing step.

[0320] In some variations, the process for producing the biogenic activated carbon composition comprises:

[0321] (a) providing a carbon-containing feedstock comprising biomass;

[0322] (b) optionally drying the feedstock to remove at least a portion of the moisture contained within the feedstock; Removal and

[0323] (c) optionally degassing the feedstock to remove any grit contained within the feedstock, if any; removing at least a portion of the interatomic oxygen;

[0324] (d) in a pyrolysis zone, in the presence of a substantially inert gas, Hot pyrolysis is carried out at a pyrolysis temperature selected from 700°C to about 700°C for at least 10 minutes. generating solids, condensable vapors, and non-condensable gases;

[0325] (e) removing at least a portion of the condensable vapors and at least a portion of the non-condensable gases from the hot pyrolysis solids; and to separate a part of it.

[0326] (f) in a cooling zone, in the presence of a substantially inert gas, the hot pyrolysis solid is cooled to about 1000 K. Cool below the decomposition temperature for at least 5 minutes to generate warm pyrolysis solids. And,

[0327] (g) In a cooling unit separate from the cooling zone, the warm pyrolysis solids are cooled to a cool temperature. generating a pyrolysis solid;

[0328] (h) recovering a biogenic activated carbon composition comprising at least a portion of the cold pyrolysis solids. And,

[0329] (i) micronizing the biogenic activated carbon composition to reduce the average particle size of the biogenic activated carbon composition; and reducing

[0330] The additive is introduced before, during, or after one or more of steps (a) to (i). The additives are acids, bases, salts, metals, metal oxides, metal hydroxides, metal halides, iodides, etc. The iodine may be selected from iodine, an iodine compound, or a combination thereof.

[0331] In some embodiments, the additive is iodine or iodine, optionally dissolved in a solvent. Contains iodine compounds, or a combination of iodine and one or more iodine compounds. A variety of solvents for iodine compounds are known in the art, including but not limited to: Alkyl halides such as n-propyl bromide or n-butyl iodide are preferred (although not Alcohols such as methanol or ethanol can be used. In embodiments, a tincture of iodine can be used to introduce additives into the composition. .

[0332] In some embodiments, the additive is selected from the group consisting of hydroxybenzoates, ... It involves iodine introduced as a solid that sublimes to iodine vapor. At room temperature, iodine is a solid. Upon heating, iodine sublimes into vapor. Therefore, solid iodine particles are not bioactive. Any stream, vessel, pipe, or container (e.g., a barrel or bag) that also contains a soluble carbon composition. Upon heating, the iodine particles sublimate and the I2 vapor penetrates the carbon particles, Thus, iodine can be incorporated as an additive onto the surface of the particles and potentially within the particles.

[0333] In one embodiment, the present disclosure provides a method for reducing at least one contaminant from a gas phase exhaust stream. and a method for adding or removing a fluorine-containing compound, the method comprising:

[0334] (a) providing a gas-phase exhaust stream containing at least one contaminant;

[0335] (b) contacting the gas phase effluent stream with activated carbon particles containing an additive and a biogenic activated carbon composition; contacting the surface of the substrate with the contaminant-adsorbing particles to generate the contaminant-adsorbing particles;

[0336] (c) separating at least a portion of said contaminant-adsorbed particles from said gas-phase effluent stream; and producing a gas-phase exhaust stream having reduced contaminants.

[0337] In some embodiments, the activated carbon particles further comprise an additive. In some embodiments, step (b) includes adding the additive directly to said gas-phase effluent stream. In some embodiments, the additive is an acid, a base, a salt, a metal, a metal oxide, a metal hydroxide. The group consisting of iodides, metal halides, iodine, iodine compounds, and combinations thereof In some embodiments, the additive is selected from magnesium, manganese, aluminum, Aluminum, nickel, iron, chromium, silicon, boron, cerium, molybdenum, phosphorus, thiamin ungsten, vanadium, iron chloride, iron bromide, magnesium oxide, dolomite, dolomite Lime, fluorite, fluorospar, bentonite, calcium oxide, lime, sodium hydroxide Thorium, potassium hydroxide, hydrogen bromide, hydrogen chloride, sodium silicate, potassium permanganate an organic acid, an iodine compound, an iodine compound, or a combination thereof; In some embodiments, the contaminants are mercury, boron, selenium, arsenic, The metal is selected from the group consisting of compounds, salts thereof, and mixtures thereof. In some embodiments, the contaminants are hazardous air pollutants. In some embodiments, the contaminant is a volatile organic compound. Nitrogen oxides, carbon monoxide, carbon dioxide, hydrogen sulfide, sulfur dioxide, sulfur trioxide, methane, ethane, ethylene, ozone, ammonia, and combinations thereof. It is a non-condensable gas that is generated.

[0338] In some embodiments, the contaminant-adsorbed carbon particles may be contaminant-adsorbed, such as carbon dioxide, nitrogen oxides, mercury, or the like. , sulfur dioxide, their absorbed forms, their adsorbed forms, their reacted forms or mixtures thereof.

[0339] In some embodiments, the gas phase exhaust stream comprises the biogenic activated carbon composition described above. Derived from, resulting from, or produced by the combustion of fuel. In this embodiment, the gas phase exhaust stream is produced by co-combustion of coal and the biogenic activated carbon composition. Derived from, arising from, or produced by.

[0340]

[0341] In some embodiments, the method further comprises (d) treating the contaminant-adsorbed carbon particles to The method further comprises regenerating said activated carbon particles.

[0342] In some embodiments, the method further comprises (d') burning said contaminant-adsorbed carbon particles. generating energy.

[0343] In one embodiment, a method for reducing mercury emissions using a biogenic activated carbon composition includes:

[0344] (a) providing a gas phase effluent stream containing mercury;

[0345] (b) separating the gas-phase effluent stream from a biogenic activated carbon composition containing iron or an iron-containing compound. contacting the mercury-adsorbed carbon particles with activated carbon particles to generate mercury-adsorbed carbon particles;

[0346] (c) removing at least said mercury-adsorbed carbon particles from said gas-phase effluent stream using electrostatic precipitation; and separating a portion of the mercury-reduced gas phase effluent stream.

[0347] In some embodiments, the presence of the iron or iron-containing compound in the activated carbon particles is Enhance the aforementioned electrostatic precipitation during step (c), thereby improving mercury control.

[0348] In some embodiments, the method further comprises (d) disposing of the other electrostatic charges formed in step (c). and separating at least a portion of the mercury-adsorbed carbon particles from the precipitate. In an embodiment, step (d) comprises exposing said mercury-adsorbed carbon particles to a magnetic field. include.

[0349] In some embodiments, the process for generating energy comprises:

[0350] (a) providing a carbon-containing feedstock comprising a biogenic activated carbon composition;

[0351] (b) oxidizing said carbon-containing feedstock to produce energy and at least one pollutant; generating a gas phase exhaust stream containing the dye, wherein the biogenic activated carbon composition comprises at least At least a portion of each of the contaminants is adsorbed.

[0352] In some embodiments, the carbon-containing feedstock is free of at least one contaminant or In some embodiments, the carbon-containing feedstock further comprises a precursor of biomass. In some embodiments, the carbon-containing feedstock further comprises coal. In some embodiments, the carbon-containing feedstock is derived essentially from the aforementioned biogenic activated carbon composition. In some embodiments, the at least one contaminant is mercury, boron, selenium, or the like. arsenic, compounds thereof, salts thereof, and mixtures thereof. In some embodiments, the at least one contaminant is a hazardous air pollutant. In some embodiments, at least one Pollutants include nitrogen oxides, carbon monoxide, carbon dioxide, hydrogen sulfide, sulfur dioxide, sulfur trioxide, The group consisting of methane, ethane, ethylene, ozone, ammonia, and combinations thereof In some embodiments, the biogenic activated carbon composition comprises a non-condensable gas selected from the group consisting of: The composition may contain additives such as acids, bases, salts, metals, metal oxides, metal hydroxides, metal halides, iodides, etc. The iodine-containing compound may be selected from the group consisting of iodine, iodine compounds, and combinations thereof. In some embodiments, the additives include magnesium, manganese, aluminum, nickel, Kel, iron, chromium, silicon, boron, cerium, molybdenum, phosphorus, tungsten, vanadium Sodium, iron chloride, iron bromide, magnesium oxide, dolomite, dolomitic lime, fluoride Fluorospar, bentonite, calcium oxide, lime, sodium hydroxide, hydroxide Potassium, hydrogen bromide, hydrogen chloride, sodium silicate, potassium permanganate, organic acids, iodine The iodine is selected from the group consisting of iodine, iodine compounds, and combinations thereof.

[0353] In any of the methods of use disclosed herein, the biogenic activated carbon composition comprises at least about Heat value of 5,000 BTU / lb, e.g., about 5,000, at least about 6,000, at least at least about 7,000, at least about 8,000, at least about 9,000, at least about 10,000, at least about 11,000, at least about 12,000, or about 12, It may have a heat value of over 100,000 BTU / lb.

[0354] In any of the methods of use disclosed herein, the biogenic activated carbon composition disclosed herein may be used anywhere in the fuel delivery, fuel storage, fuel preparation, or fuel mixing process. in fuel yards, storage bins, on conveyors, in mixers, and during filling. Alternatively, or in addition, biologically derived Activated carbon is burned either in a mixture with or independently of other fuel source(s). For example and without limitation, in some embodiments, a biogenic active agent may be added to the zone. The charcoal composition may be added at or before the combustion zone, at or before the burner end, and / or The oxygen-containing feedstock is provided prior to or simultaneously with the step of oxidizing the oxygen-containing feedstock.

[0355] In one embodiment, a method for purifying a liquid with a biogenic activated carbon composition includes:

[0356] (a) providing a liquid containing at least one contaminant;

[0357] (b) contacting said liquid with activated carbon particles containing an additive and a biogenic activated carbon composition; and (b) subjecting the carbon particles to a treatment to produce contaminant-adsorbed carbon particles and a contaminant-reduced liquid.

[0358] In some embodiments, the activated carbon particles include the additives described above. In this embodiment, the additive may be an acid, a base, a salt, a metal, a metal oxide, a metal hydroxide, a metal halogen The iodide is selected from the group consisting of iodides, iodine, iodine compounds, and combinations thereof. In some embodiments, the additives include magnesium, manganese, aluminum, nickel, Iron, chromium, silicon, boron, cerium, molybdenum, phosphorus, tungsten, vanadium Iron, iron chloride, iron bromide, magnesium oxide, dolomite, dolomitic lime, fluorite , Fluorospar, Bentonite, Calcium oxide, Lime, Sodium hydroxide, Calcium hydroxide Sodium, hydrogen bromide, hydrogen chloride, sodium silicate, potassium permanganate, organic acids, iodide The iodine compound is selected from the group consisting of iodine, iodine compounds, and combinations thereof. In an embodiment, the at least one contaminant is arsenic, boron, selenium, mercury, or a compound thereof. The metal is selected from the group consisting of compounds thereof, salts thereof, and mixtures thereof. In some embodiments, the at least one contaminant comprises an organic compound. In some embodiments, at least one contaminant comprises a halogen. In some embodiments, the at least one contaminant comprises hydrogen sulfide. One or more contaminants include chlorinated by-products. One contaminant includes a pesticide or herbicide. In some embodiments, the liquid is water. Includes.

[0359] In some embodiments, the method further comprises treating the contaminant-adsorbed carbon particles to form the activated carbon particles described above. In some embodiments, the method further comprises regenerating the particles. It further includes burning the particles to generate energy.

[0360] In one embodiment, the present disclosure provides a method for removing at least a portion of sulfur contaminants from a liquid. and the method comprises:

[0361] (a) providing a liquid containing sulfur contaminants;

[0362] (b) contacting said liquid with activated carbon particles containing an additive and a biogenic activated carbon composition; and

[0363] After step (b), at least a portion of the activated carbon particles contain sulfur contaminants.

[0364] In some embodiments, sulfur contaminants include elemental sulfur, sulfuric acid, sulfurous acid, sulfur dioxide, Sulfur trioxide, sulfate anion, bisulfate anion, sulfite anion, bisulfite anion amines, thiols, sulfides, disulfides, polysulfides, thioethers, thioesters, thioacetates sulfoxides, sulfones, thiosulfinates, sulfimides, sulfoximides, Sulfondiimines, sulfur halides, thioketones, thioaldehydes, sulfur oxides, thio Carboxylic acids, thioamides, sulfonic acids, sulfinic acids, sulfenic acids, sulfonium, thioamides xosulfonium, sulfurane, persulfuran, derivatives thereof, salts thereof, and In some embodiments, the sulfur contamination is selected from the group consisting of sulfur contamination and combinations thereof. In some embodiments, the additive is a sulfate in anionic and / or salt form. Additives include acids, bases, salts, metals, metal oxides, metal hydroxides, metal halides, iodine, iodine compounds, and combinations thereof. In this embodiment, the additives are magnesium, manganese, aluminum, nickel, iron, chromium , silicon, boron, cerium, molybdenum, phosphorus, tungsten, vanadium, iron chloride, Iron bromide, magnesium oxide, dolomite, dolomitic lime, fluorite, fluorospa -, bentonite, calcium oxide, lime, sodium hydroxide, potassium hydroxide, bromide water Iodine, hydrogen chloride, sodium silicate, potassium permanganate, organic acids, iodine, iodine compounds In some embodiments, the compound is selected from the group consisting of: In some embodiments, step (b) comprises filtering and / or percolating the liquid. In step (b), the liquid is permeated with the activated carbon particles and the additive. In some embodiments, step (b) comprises contacting the membrane with the liquid. In some embodiments, the method comprises administering the activated carbon particles directly to the body. (c) further comprising settling said activated carbon particles having said sulfur contaminants from said liquid. In some embodiments, the liquid comprises wastewater. Wastewater is generated from metal mining, acid mine drainage, mineral processing, municipal sewerage treatment, pulp and paper manufacturing, and energy In some embodiments, the process is selected from the group consisting of ethanol production. In some embodiments, the liquid is a natural body of water.

[0365] In one embodiment, the present disclosure provides a process for reducing the concentration of sulfate in water. This process provides

[0366] (a) providing a quantity or stream of water containing sulfate;

[0367] (b) contacting said water with activated carbon particles containing an additive and a biogenic activated carbon composition; This includes making the

[0368] In some embodiments, before step (a), the water has a concentration of greater than about 50 mg / L sulfate, and after step (b), the water contains a sulfate concentration of about 50 mg / L or less. In some embodiments, after step (b), the water has a sulfur concentration of about 10 mg / L or less. In some embodiments, the water is a wastewater stream. In this context, wastewater streams include metal mining, acid mine drainage, mineral processing, municipal sewerage treatment, and pulp and paper manufacturing. and ethanol production. In some embodiments, the water is a natural body of water. are acids, bases, salts, metals, metal oxides, metal hydroxides, metal halides, iodine, iodine In some embodiments, the compound is selected from the group consisting of: In this case, additives include magnesium, manganese, aluminum, nickel, iron, chromium, and potassium. Ion, boron, cerium, molybdenum, phosphorus, tungsten, vanadium, iron chloride, bromide Iron, magnesium oxide, dolomite, dolomitic lime, fluorite, fluorospar, Bentonite, calcium oxide, lime, sodium hydroxide, potassium hydroxide, hydrogen bromide, Hydrogen chloride, sodium silicate, potassium permanganate, organic acids, iodine, iodine compounds, and combinations thereof.

[0369] In one embodiment, the present disclosure provides a method for removing sulfur contaminants from a gas-phase exhaust stream. ,This method is

[0370] (a) providing a gas-phase effluent stream containing at least one sulfur contaminant;

[0371] (b) contacting the gas phase effluent stream with activated carbon particles containing an additive and a biogenic activated carbon composition; Touching and

[0372] (c) after step (b), removing at least one of said activated carbon particles from said gas-phase effluent stream; and separating the portions.

[0373] In some embodiments, the sulfur-containing contaminants include elemental sulfur, sulfuric acid, sulfurous acid, sulfur dioxide, and the like. Yellow, sulfur trioxide, sulfate anion, bisulfate anion, sulfite anion, bisulfite anion Anions, thiols, sulfides, disulfides, polysulfides, thioethers, thioesters, thioamines Cetals, sulfoxides, sulfones, thiosulfinates, sulfimides, sulfoximines sulfondiimines, sulfur halides, thioketones, thioaldehydes, sulfur oxides, Thiocarboxylic acids, thioamides, sulfonic acids, sulfinic acids, sulfenic acids, sulfonium , oxosulfonium, sulfurane, persulfurane, salts thereof, derivatives thereof, and and combinations thereof. In some embodiments, the gas The phase effluent stream is derived from or produced from the combustion of a fuel containing the biogenic activated carbon composition. In some embodiments, the gas phase exhaust stream is , resulting from or arising from the co-combustion of coal and the aforementioned biogenic activated carbon composition; In some embodiments, the additive is an acid, a base, a salt, a gold metals, metal oxides, metal hydroxides, metal halides, iodine, iodine compounds, and the like In some embodiments, the additive is selected from the group consisting of malate, maltodextrin, methylparaben ... Magnesium, manganese, aluminum, nickel, iron, chromium, silicon, boron, cerium Iron, molybdenum, phosphorus, tungsten, vanadium, iron chloride, iron bromide, magnesium oxide , dolomite, dolomitic lime, fluorite, fluorospar, bentonite, calcium oxide Calcium, lime, sodium hydroxide, potassium hydroxide, hydrogen bromide, hydrogen chloride, sodium silicate Sodium, potassium permanganate, organic acids, iodine, iodine compounds, and combinations thereof In some embodiments, step (c) is selected from the group consisting of filtration. In some embodiments, step (c) comprises electrostatic precipitation. In one embodiment, step (c) comprises scrubbing.

[0374] In one embodiment, the present disclosure provides a method for reducing one or more contaminants from a gas or liquid. or a method for removing the same, the method comprising:

[0375] (a) providing a gas or liquid stream containing one or more contaminants;

[0376] (b) treating said gas or liquid stream to produce a gas or liquid stream having, on a dry basis, not less than about 55% by weight total carbon, not less than about 1 5% by weight or less hydrogen, and about 1% by weight or less nitrogen, and at least about 500% iodide. and contacting the activated carbon with a biogenic activated carbon composition containing a base metal, the composition being exogenously It responds to an applied magnetic field.

[0377] In one embodiment, the present disclosure provides a method for reducing one or more contaminants from a gas or liquid. or a method for removing the same, the method comprising:

[0378] (a) providing a gas or liquid stream containing one or more contaminants;

[0379] (b) treating said gas or liquid stream to produce a gas or liquid stream having, on a dry basis, not less than about 55% by weight total carbon, not less than about 1 5% by weight or less hydrogen, and about 1% by weight or less nitrogen, and at least about 500% iodide. and contacting the carbon with a biogenic activated carbon composition containing a base value. Some exists in the form of graphene.

[0380] In one embodiment, the present disclosure provides a method for reducing or removing contaminants from a liquid or gas. The method further comprises the steps of:

[0381] (a) on a dry basis, about 55% by weight or more total carbon and about 15% by weight or less hydrogen; and Obtaining a biogenic activated carbon composition containing less than about 1% by weight of nitrogen (at least one of the aforementioned carbons) some of which exist in the form of graphene),

[0382] (b) optionally isolating said graphene from said biogenic activated carbon composition; ,

[0383] (c) the liquid or gas in separated form or the aforementioned biogenic activated carbon composition. and contacting the graphene as part of the process.

[0384] In some embodiments, the liquid is water.

[0385] In one embodiment, the present disclosure provides a composition comprising graphene, the graphene comprising , on a dry basis, about 55% by weight or more total carbon, about 15% by weight or less hydrogen, and about 1% by weight % or less of nitrogen, wherein at least a portion of said carbon is derived from a biogenic activated carbon composition comprising: In some embodiments, the composition is used as an adhesive, sealant, or the like. , coatings, paints, inks, composite material components, catalysts, catalyst supports, battery electrode components, fuel cell electrodes Polar components, graphene-based circuit or memory system components, energy storage materials, Supercapacitor components, static dissipative sinks, electron or ion transport materials, high Band communication system components, infrared sensor components, chemical sensor components, biological sensor components a graphene aerosol component, an electronic display component, a voltaic cell component, or contained in the gel.

[0386] In one embodiment, the present disclosure provides a method of using graphene, the method comprising:

[0387] (a) on a dry basis, about 55% by weight or more total carbon and about 15% by weight or less hydrogen; and Obtaining a biogenic activated carbon composition containing less than about 1% by weight of nitrogen (at least one of the aforementioned carbons) some of which exist in the form of graphene),

[0388] (b) optionally isolating said graphene from said biogenic activated carbon composition; ,

[0389] (c) incorporating said graphene in isolated form or in said biogenic activated carbon composition. This includes use in adhesives, sealants, coatings, paints, or inks as part of a product. nothing.

[0390] In one embodiment, the present disclosure provides a method of using graphene, the method comprising:

[0391] (a) on a dry basis, about 55% by weight or more total carbon and about 15% by weight or less hydrogen; and Obtaining a biogenic activated carbon composition containing less than about 1% by weight of nitrogen (at least one of the aforementioned carbons) some of which exist in the form of graphene),

[0392] (b) optionally isolating said graphene from said biogenic activated carbon composition; ,

[0393] (c) incorporating said graphene in isolated form or in said biogenic activated carbon composition. as a part of a product, or as a component in a composite material, to improve the mechanical or electrical properties of said composite material. and adjusting the optical properties.

[0394] In one embodiment, the present disclosure provides a method of using graphene, the method comprising:

[0395] (a) on a dry basis, about 55% by weight or more total carbon and about 15% by weight or less hydrogen; and Obtaining a biogenic activated carbon composition containing less than about 1% by weight of nitrogen (at least one of the aforementioned carbons) some of which exist in the form of graphene),

[0396] (b) optionally isolating said graphene from said biogenic activated carbon composition; ,

[0397] (c) incorporating said graphene in isolated form or in said biogenic activated carbon composition. Use as part of a product as a catalyst, catalyst support, battery electrode material, or fuel cell electrode material This includes:

[0398] In one embodiment, the present disclosure provides a method of using graphene, the method comprising:

[0399] (a) on a dry basis, about 55% by weight or more total carbon and about 15% by weight or less hydrogen; and Obtaining a biogenic activated carbon composition containing less than about 1% by weight of nitrogen (at least one of the aforementioned carbons) some of which exist in the form of graphene),

[0400] (b) optionally isolating said graphene from said biogenic activated carbon composition; ,

[0401] (c) incorporating said graphene in isolated form or in said biogenic activated carbon composition. and use in graphene-based circuits or memory systems as part of an article. Includes.

[0402] In one embodiment, the present disclosure provides a method of using graphene, the method comprising:

[0403] (a) on a dry basis, about 55% by weight or more total carbon and about 15% by weight or less hydrogen; and Obtaining a biogenic activated carbon composition containing less than about 1% by weight of nitrogen (at least one of the aforementioned carbons) some of which exist in the form of graphene),

[0404] (b) optionally isolating said graphene from said biogenic activated carbon composition; ,

[0405] (c) incorporating said graphene in isolated form or in said biogenic activated carbon composition. as part of an object, as an energy storage material or supercapacitor component This includes the following.

[0406] In one embodiment, the present disclosure provides a method of using graphene, the method comprising:

[0407] (a) on a dry basis, about 55% by weight or more total carbon and about 15% by weight or less hydrogen; and Obtaining a biogenic activated carbon composition containing less than about 1% by weight of nitrogen (at least one of the aforementioned carbons) some of which exist in the form of graphene),

[0408] (b) optionally isolating said graphene from said biogenic activated carbon composition; ,

[0409] (c) incorporating said graphene in isolated form or in said biogenic activated carbon composition. Used as part of a static dissipative sink in a liquid or vapor fuel delivery system. This includes using

[0410] In one embodiment, the present disclosure provides a method of using graphene, the method comprising:

[0411] (a) on a dry basis, about 55% by weight or more total carbon and about 15% by weight or less hydrogen; and Obtaining a biogenic activated carbon composition containing less than about 1% by weight of nitrogen (at least one of the aforementioned carbons) some of which exist in the form of graphene),

[0412] (b) optionally isolating said graphene from said biogenic activated carbon composition; ,

[0413] (c) incorporating said graphene in isolated form or in said biogenic activated carbon composition. and using the same as part of a product as an electron or ion transport material.

[0414] In one embodiment, the present disclosure provides a method of using graphene, the method comprising:

[0415] (a) on a dry basis, about 55% by weight or more total carbon and about 15% by weight or less hydrogen; and Obtaining a biogenic activated carbon composition containing less than about 1% by weight of nitrogen (at least one of the aforementioned carbons) some of which exist in the form of graphene),

[0416] (b) optionally isolating said graphene from said biogenic activated carbon composition; ,

[0417] (c) incorporating said graphene in isolated form or in said biogenic activated carbon composition. As part of the product, the present invention includes use in high bandwidth communication systems.

[0418] In one embodiment, the present disclosure provides a method of using graphene, the method comprising:

[0419] (a) on a dry basis, about 55% by weight or more total carbon and about 15% by weight or less hydrogen; and Obtaining a biogenic activated carbon composition containing less than about 1% by weight of nitrogen (at least one of the aforementioned carbons) some of which exist in the form of graphene),

[0420] (b) optionally isolating said graphene from said biogenic activated carbon composition; ,

[0421] (c) incorporating said graphene in isolated form or in said biogenic activated carbon composition. as part of an article, as a component of an infrared, chemical, or biological sensor; Includes.

[0422] In one embodiment, the present disclosure provides a method of using graphene, the method comprising:

[0423] (a) on a dry basis, about 55% by weight or more total carbon and about 15% by weight or less hydrogen; and Obtaining a biogenic activated carbon composition containing less than about 1% by weight of nitrogen (at least one of the aforementioned carbons) some of which exist in the form of graphene),

[0424] (b) optionally isolating said graphene from said biogenic activated carbon composition; ,

[0425] (c) incorporating said graphene in isolated form or in said biogenic activated carbon composition. and using the same as part of an article, as a component of an electronic display.

[0426] In one embodiment, the present disclosure provides a method of using graphene, the method comprising:

[0427] (a) on a dry basis, about 55% by weight or more total carbon and about 15% by weight or less hydrogen; and Obtaining a biogenic activated carbon composition containing less than about 1% by weight of nitrogen (at least one of the aforementioned carbons) some of which exist in the form of graphene),

[0428] (b) optionally isolating said graphene from said biogenic activated carbon composition; ,

[0429] (c) incorporating said graphene in isolated form or in said biogenic activated carbon composition. and using the same as part of an article as a component of a solar cell.

[0430] In one embodiment, the present disclosure provides a method of using graphene, the method comprising:

[0431] (a) on a dry basis, about 55% by weight or more total carbon and about 15% by weight or less hydrogen; and Obtaining a biogenic activated carbon composition containing less than about 1% by weight of nitrogen (at least one of the aforementioned carbons) some of which exist in the form of graphene),

[0432] (b) optionally isolating said graphene from said biogenic activated carbon composition; ,

[0433] (c) incorporating said graphene in isolated form or in said biogenic activated carbon composition. and using the same as part of an article to form a graphene aerogel.

[0434] In one embodiment, a method for reducing emissions using a biogenic activated carbon composition is provided. ,This method is

[0435] (a) providing activated carbon particles comprising a biogenic activated carbon composition;

[0436] (b) providing a gas-phase exhaust stream containing at least one selected contaminant;

[0437] (c) Additives selected to assist in the removal of selected contaminants from the gas-phase effluent stream. Providing things and

[0438] (d) introducing activated carbon particles and additives into the gas phase exhaust stream to reduce the concentration of selected contaminants; and adsorbing at least a portion of the contaminant onto activated carbon particles, thereby forming contaminant-adsorbed carbon particles in the gas-phase effluent stream. and

[0439] (e) separating at least a portion of the contaminant-adsorbed carbon particles from the gas-phase effluent stream to determine whether the contaminants are present in the contaminant-adsorbed carbon particles; and producing a reduced gas phase exhaust stream.

[0440] In some embodiments, the biogenic activated carbon composition comprises 55% or more by weight total carbon; Not more than 15% by weight hydrogen, not more than 1% by weight nitrogen, not more than 0.5% by weight phosphorus, and not more than 0.2% by weight The additive may be provided as part of activated carbon particles. Alternatively, the additive may be introduced directly into the gas phase exhaust stream.

[0441] Additives (to assist in the removal of selected contaminants from gas phase effluent streams) include acids, Bases, salts, metals, metal oxides, metal hydroxides, metal halides, iodine, iodine compounds or a combination thereof. In some embodiments, the additive iodine or an iodine compound, or iodine and one or more iodine compounds, optionally dissolved in a solvent; Contains a combination of uric acid compounds.

[0442] In some embodiments, the selected contaminants are mercury, boron, selenium, arsenic, etc. and any compounds, salts, and mixtures thereof. In some embodiments, the selected pollutant is a hazardous air pollutant or In some embodiments, the selected contaminant is nitrogen oxides. carbon monoxide, carbon dioxide, hydrogen sulfide, sulfur dioxide, sulfur trioxide, methane, ethane, a non-condensing agent selected from the group consisting of ethylene, ozone, ammonia, and combinations thereof; It is a condensed gas.

[0443] In some embodiments, the contaminant-adsorbed carbon particles are in an adsorbed form. , or in reacted form, the group consisting of carbon dioxide, nitrogen oxides, mercury, and sulfur dioxide The present invention relates to a method for treating a bacterial infection comprising the steps of:

[0444] In some embodiments, the gas phase exhaust stream is a mixture of a fuel containing a biogenic activated carbon composition. In certain embodiments, the gas phase exhaust stream is derived from coal and biogenic activated carbon. It results from the co-combustion of charcoal compositions.

[0445] In some embodiments, the separating in step (e) comprises filtering, e.g., A woven fabric filter may be utilized. In some embodiments, in step (e), Separation methods include electrostatic deposition. Scrub cleaning (including wet or dry scrubbing) is also used. Optionally, the contaminant-adsorbed carbon particles can be reacted to regenerate the activated carbon particles. In some embodiments, the contaminant-adsorbed carbon particles can be thermally decomposed, either catalytically or non-catalytically. The contaminant-adsorbed carbon particles, or their regenerated form, are burned to produce energy. and / or may be gasified to provide synthesis gas.

[0446] In some embodiments, biogenic activated carbon compositions are used to reduce mercury emissions The method is:

[0447] (a) a biogenic activated carbon composition containing an additive that includes iodine or an iodine-containing compound; providing activated carbon particles comprising:

[0448] (b) providing a gas phase effluent stream containing mercury;

[0449] (c) introducing activated carbon particles into the gas phase effluent stream to deposit at least a portion of the mercury onto the activated carbon particles; thereby generating mercury-adsorbed carbon particles in the gas phase exhaust stream;

[0450] (d) separating at least a portion of the mercury-adsorbed carbon particles from the gas-phase effluent stream using electrostatic precipitation; and separating the mercury-reduced gas phase exhaust stream.

[0451] In some variations, a process for producing energy is provided, the process comprising: Process is

[0452] (a) providing a carbon-containing feedstock comprising a biogenic activated carbon composition;

[0453] (b) oxidizing a carbon-containing feedstock to generate energy and a gas-phase exhaust stream; Including and

[0454] The presence of biogenic activated carbon compositions within the carbon-containing feedstock may result in the formation of activated carbon as a by-product of oxidation. or for adsorbing at least one contaminant derived from a carbon-containing feedstock. effective, thereby reducing pollutant emissions,

[0455] The biogenic activated carbon composition may be a mixture of acids, bases, salts, metals, metal oxides, metal hydroxides, metal an additive selected from a halide, iodine, an iodine compound, or a combination thereof; Further includes:

[0456] In some embodiments, the contaminant or its precursor is contained within a carbon-containing feedstock. In some embodiments, the contaminants are produced as a by-product of oxidation. The contained feedstock, in various embodiments, may be biomass, coal, or another carbonaceous feedstock. This also includes the fee.

[0457] The contaminants selected were mercury, boron, selenium, arsenic, and any compounds thereof; metals selected from the group consisting of salts, and mixtures thereof; hazardous air pollutants; volatile organic compounds or nitrogen oxides, carbon monoxide, carbon dioxide, hydrogen sulfide, sulfur dioxide, sulfur trioxide, The group consisting of methane, ethane, ethylene, ozone, ammonia, and combinations thereof The gas may be a non-condensable gas selected from:

[0458] In some variations, the method of purifying a liquid with a biogenic activated carbon composition includes:

[0459] (a) providing activated carbon particles comprising a biogenic activated carbon composition;

[0460] (b) providing a liquid containing at least one selected contaminant;

[0461] (c) providing an additive selected to assist in the removal of selected contaminants from the liquid; To do,

[0462] (d) contacting the liquid with the activated carbon particles and the additive to form at least one selected At least a portion of the contaminants are adsorbed onto the activated carbon particles, thereby forming the contaminant-adsorbed carbon particles and and generating a reduced contaminant liquid.

[0463] The biogenic activated carbon composition, in some embodiments, comprises 55% or more by weight total carbon; Not more than 15% by weight hydrogen, not more than 1% by weight nitrogen, not more than 0.5% by weight phosphorus, and not more than 0.2% by weight Contains less than % sulfur.

[0464] The additive may be provided as part of the activated carbon particles and / or introduced directly into the liquid. Additives include acids, bases, salts, metals, metal oxides, metal hydroxides, metal halides, and iodine. , iodine compounds, or combinations thereof.

[0465] In some embodiments, the additive may be an absorbed or intercalated molecule, I2, or a physical or chemically adsorbed molecules I2, absorbed or intercalated atoms I, physical or chemical , or a combination thereof, present in the biogenic activated carbon composition. Contains iodine.

[0466] In some embodiments, the additive is iodide ion, hydrogen iodide, an iodide salt, Metal iodides, ammonium iodide, iodine oxide, triiodide ion, triiodide salt, gold Group triiodides, ammonium triiodides, iodate ions, iodate salts, polyiodides, Iodoform, iodic acid, methyl iodide, iodinated hydrocarbons, periodic acid, orthoperiodine Acid, metaperiodic acid, and combinations, salts, acids, bases, or derivatives thereof Iodine-containing compounds, such as (but not limited to) iodine-containing compounds selected from the group Includes compounds.

[0467] Additives result in a final product with a higher energy content (energy density) The increase in energy content can be attributed to the total carbon, fixed carbon, volatile carbon, or even water. Alternatively, or in addition, the increase in energy content may be due to the use of non-combustible materials. Or it may be due to the removal of materials that have a lower energy density than carbon. In the form, the additives may be in favor of solid and gas formation or in favor of solid formation, Reduces the degree of liquid formation.

[0468] In various embodiments, the additive is a starting biomass or a biomass that has been treated prior to pyrolysis. Biomass is chemically modified to reduce cell wall rupture for greater strength / integrity. In some embodiments, the additive reduces the fixed carbon content of the biomass feedstock prior to pyrolysis. may increase.

[0469] Additives affect yield strength, compressive strength, tensile strength, fatigue strength, impact strength, elastic modulus, bulk modulus or may result in a final biogenic activated carbon product with improved mechanical properties such as shear modulus. Additives are not additives that merely by their presence (e.g., the additive itself imparts strength to the mixture). due to some transformation occurring within the additive phase or the resulting mixture. For example, reactions such as vitrification can be performed on biogenic activated carbon containing additives. This may occur within the composition, thereby improving its final strength.

[0470] Chemical additives can be applied to wet or dry biomass feedstock. It may be applied as a powder, spray, mist, liquid, or vapor. The additive is sprayed with a liquid solution (such as an aqueous solution or a solvent) or placed in a tank, bottle, bag, or Alternatively, it may be introduced by immersion in another container.

[0471] In certain embodiments, a soaking pretreatment is used, and the solid feedstock is subjected to the following steps per batch: or continuously for a time sufficient for the additive to penetrate the solid feed material. The patient is immersed in a bathtub containing

[0472] In some embodiments, the additive applied to the feedstock contributes to the energy required for pyrolysis. These or other In embodiments, the additives applied to the feedstock are further described below with respect to composition. As such, the carbonaceous product may be provided with the functionality desired for its intended use.

[0473] In some embodiments, the process for producing biogenic activated carbon comprises warm Pyrolysis solids or cold pyrolysis solids are sized (e.g., sorted, screened, classified, etc.) ) to form a sized pyrolyzed solid. The resulting pyrolysis solids are suitable for applications requiring activated carbon products with certain particle size characteristics. It can be used as follows.

[0474] Throughput, or process capacity, can range from small laboratory-scale units to any pipe size. Biorefineries can vary widely in scale from batch, demonstration, or semi-industrial to full industrial scale. In various embodiments, the process capacity is at least about 1 kg / day, 10 kg / day, day, 100kg / day, 1 ton / day (all in metric tons), 10 ton / day, 1 00 tons / day, 500 tons / day, 1000 tons / day, 2000 tons / day or more is.

[0475] In some embodiments, a portion of the solids produced is present at the front end of the process, i.e. , can be recycled to a drying unit or degassing unit, or can be recycled to a BPU or reactor The treated solids can be recycled directly to the front end by going through the process again. The amount of fixed carbon in the body can be high. The liquid and gas streams can be independently recycled, carried on to subsequent steps, or or may be removed / purged from the process at any time.

[0476] In some embodiments, the pyrolysis material is recovered and then recycled for further pyrolysis. to separate reactors to create products with higher carbon purity. In embodiments, the secondary process may be carried out in a simple container such as a steel drum, and the heating An inert gas (such as heated N2) is passed through it. These include process tanks, barrels, bins, totes, cloth bags, and roll-offs. This secondary sweep gas with the product can be sent to, for example, a process gas heater or can be sent to the main To cool the final product, for example, an inert gas tank initially at ambient temperature may be used. A separate stream of gas may be passed through the solids to cool them and then returned to the inert gas preheat system. In various embodiments, the secondary process is carried out in a separate carbonization or pyrolysis reactor. where a preheated, substantially inert gas is input to pyrolyze the material and drive carbonization. Move.

[0477] Some embodiments of the present disclosure provide a biogenic activated carbon production system, M is,

[0478] (a) a material feed system configured to introduce a carbon-containing feedstock;

[0479] (b) a material feed system configured to remove moisture contained within the carbon-containing feedstock; an optional dryer disposed in operable communication with the stem;

[0480] (c) a biomass processing unit including a plurality of zones disposed in operable communication with the dryer; The biomass processing unit is in operative communication with a spatially separated cooling zone. The biomass processing unit contains at least one pyrolysis zone arranged in a outlets for removing condensable vapors and non-condensable gases from the

[0481] (d) an external cooler disposed in operable communication with the biomass processing unit;

[0482] (e) a carbon recovery unit disposed in operable communication with the cooler.

[0483] Some embodiments of the present disclosure provide a biogenic activated carbon production system, M is,

[0484] (a) a material feed system configured to introduce a carbon-containing feedstock;

[0485] (b) a material feed system configured to remove moisture contained within the carbon-containing feedstock; an optional dryer disposed in operable communication with the stem;

[0486] (c) a dryer configured to heat and / or gently pyrolyze the feedstock; an optional preheater disposed in operable communication with the

[0487] (d) a preheater configured to pyrolyze the feedstock; a pyrolysis reactor having a

[0488] (e) a cooling device in operative communication with the pyrolysis reactor configured to cool the pyrolysis solids; a cooler disposed therein;

[0489] (f) a carbon recovery unit disposed in operable communication with the cooler;

[0490] The system comprises at least one means for removing condensable vapors and non-condensable gases from solids. It also consists of one gas outlet.

[0491] The material supply system uses a screw material supply system or an Auger mechanism to connect the BPU and material. The reactors may be physically integrated and feed solids may be introduced into one of the reactors or zones.

[0492] In some embodiments, the system is disposed in operative communication with the pyrolysis zone. The pyrolysis zone, cooling zone, and preheating zone (if present) are Each may be located within a single BPU or may be located in separate BPUs.

[0493] Optionally, the dryer may be configured as a drying zone within the BPU. U (i.e., configured as an additional cooling zone, or (may be integrated with a cooling zone).

[0494] The system may include a purging means for removing oxygen from the system. The gas supply means may include one or more inlets for introducing a substantially inert gas, as well as a gas supply means for supplying a substantially inert gas from the system. and one or more outlets for removing substantially inert gas and migrated oxygen from the In some embodiments, the purging means is in operative communication between the dryer and the BPU. It is a deaerator arranged in such a way that

[0495] The BPU may be configured with at least a first gas inlet and a first gas outlet. The gas inlet and the first gas outlet may be positioned in communication with different zones or the same zone.

[0496] In some embodiments, the BPU includes a second gas inlet and / or a second gas outlet. In some embodiments, the BPU may be configured with a third gas inlet and / or In some embodiments, the BPU may be configured with a fourth gas outlet. In some embodiments, the B Each zone present in the PU may consist of a gas inlet and a gas outlet.

[0497] The gas inlets and outlets not only allow the introduction and withdrawal of steam, but also, in particular, the gas The outlet (probe) is located throughout the various stages of the process, up to all stages of the process. and also allows for accurate process monitoring and control potentially including all stages of the process Accurate process monitoring requires dynamic and historical adjustment of process conditions. This is expected to result in improved yields and efficiencies over a period of time.

[0498] In some embodiments (see generally FIG. 4), the reactive gas probe is Such a reaction gas probe is disposed in operable communication with the decomposition zone. To determine the degree of selectivity, or other process monitoring, gases are extracted and analyzed. Then, based on the measurement results, the process can be , e.g., feed rate, inert gas sweep rate, temperature (of one or more zones), The temperature can be controlled or adjusted by adjusting the pressure (of the heating zone), additives, etc.

[0499] As intended herein, "monitoring and controlling" via a reactive gas probe refers to monitoring and controlling the reactive gas. including any one or more sample extractions via gas probes, as necessary or desirable When considered as such, well-known principles of process control (feedback, feedforward, Optionally, manufacturing process or equipment adjustments based on measurement results can be performed using proportional integral induction logic, etc. should be construed to include.

[0500] The reactive gas probe can be configured to extract a gas sample in several ways. For example, the sampling line is designed so that when the sampling line is opened, a certain amount of gas is thermally decomposed. The pressure may be lower than that of the pyrolysis reactor so that it can be easily extracted from the zone. The sampling line may be under vacuum, for example, if the pyrolysis zone is at near atmospheric pressure. Typically, a reactive gas probe has one gas output or a portion thereof (e.g., a gas output lamp). It is associated with the line that splits off from the inn.

[0501] In some embodiments, both the gas input and gas output are inert gases in the zone. Periodically introduce gas and withdraw inert gas from the gas output with a process sample ("sample"). Such an arrangement is useful for process gas probes. It can be used in zones that do not have separate gas inlets / outlets for substantially inert gases. or the reactive gas probe has a separate gas inlet / outlet in addition to the process inlet and outlet. The sampling inactive material is introduced and extracted periodically for sampling. The reactive gas (in embodiments utilizing a sample sweep) may be used to improve analytical accuracy or resolution, if desired. It may also differ from the process inert gas due to any reason for the introduction of analytical tracers.

[0502] For example, the concentration of acetic acid in the gas phase of the pyrolysis zone is measured using a gas probe to measure the sample. This can then be analyzed by suitable techniques, such as gas chromatography (GC), Mass spectrometry (MS), GC-MS, or Fourier transform infrared spectroscopy (FTIR) The CO and / or CO2 concentration in the gas phase is analyzed e.g. The terpene concentration in the gas phase can be measured and used as an indicator of the pyrolysis selectivity of the liquid phase. It can be measured and used as an indicator of thermal decomposition selectivity for the body, etc.

[0503] In some embodiments, the system includes a cooling zone, or a drying zone (if present). ) or at least one preheat zone (if present) disposed in operable communication with the Further included is a further gas probe.

[0504] A gas probe in the cooling zone can be used to determine, for example, the extent of any further chemical reactions occurring in the cooling zone. A gas probe in the cooling zone can be useful for determining the temperature. This may also be useful as a means of measuring the temperature (e.g., in addition to thermocouples placed in the cooling zone). The resulting measurements can be a correlation between cooling temperature and the measured amount of a particular species. The correlation may be made separately or may be established after a period of process operation.

[0505] A gas probe in the drying zone determines the degree of drying, for example by measuring the water content. A gas probe in the preheat zone can be useful to determine, for example, any It can be useful to determine the extent of mild pyrolysis.

[0506] In certain embodiments, the cooling zone comprises a gas inlet and the pyrolysis zone comprises a gas an outlet configured to generate a gas phase flowing substantially countercurrently to the solid phase; Alternatively, or in addition, the preheat zone (if present) may comprise a gas outlet to allow the solid phase Alternatively or additionally, a gas phase may be generated that flows substantially countercurrently to the Additionally, the drying zone may be configured with a gas outlet to generate a substantially countercurrent flow. .

[0507] The pyrolysis reactor or reactors may be any suitable reactor capable of carrying out a pyrolysis process. Exemplary reactor configurations include a fixed bed reactor, a fluidized bed reactor, an entrained bed reactor, and a reactors, augers, rotating cones, rotary ram kilns, calciners, roasters, moving bed reactors, transport beds reactors, ablative reactors, rotating cone, or microwave-assisted pyrolysis reactors. Examples include, but are not limited to:

[0508] In some embodiments where an auger is used, sand or another heat carrier is optionally used. For example, the feedstock and sand can be fed at one end of the screw. The screw mixes the feedstock and conveys them through the reactor. This provides good control and does not dilute the pyrolysis products with carrier or fluidizing gas. It can be reheated in the container.

[0509] In some embodiments where an ablative process is used, the feedstock is heated to a high temperature The ablation of any carbon that occurs on the surface is a highly heat-conducting process. Such a device can prevent dilution of the product. The feed particles are suspended in a carrier gas and directed at high velocity through a cyclone with heated walls. can be inserted.

[0510] In some embodiments where a fluidized bed reactor is used, the feedstock is typically recycled. The product gas may be introduced into a hot sand bed fluidized by the gas. References to "sand" in this document include glass particles, recovered ash particles, and similar substantially inert materials. The high thermal conductivity of fluidized sand results in rapid heating of the feedstock. There may be some abrasion due to friction with sand particles. Heat is usually generated by high temperature combustion. It is provided by heat exchanger tubes through which the gas flows.

[0511] A circulating fluidized bed reactor may be used in which the gas, sand, and feedstock move together. The transport gases include recycled product gases and combustion gases. The high thermal conductivity of sand allows This ensures rapid heating of the feedstock and ablation is faster than conventional fluidized bed ablation. Separators are used to separate the product gas from the sand and charcoal particles. The sand particles can be reheated in a fluidized burner vessel and recycled to the reactor.

[0512] In some embodiments, the BPU has separate control over the feedstock inlet, temperature, and a plurality of spatially separated zones configured to mix within each zone; and a continuous reactor with a solids outlet, one of the zones being substantially inert to the BPU; The first gas inlet may be configured for introducing a gas, and one of the zones may be configured for a first gas outlet. It may comprise a mouth.

[0513] In some embodiments, the reactor comprises at least two, three, four, or more The above zones are electrical heat conduction, steam heat conduction, hot oil heat conduction, and phase change heat conduction, respectively. , waste heat conduction, and combinations thereof. In some embodiments, at least one of the zones is in communication with a heating means. The zone is heated with the effluent stream from the process gas heater, if present.

[0514] The BPU must be configured to provide at least 2 The gas phase composition and gas phase residence time of the two zones can be adjusted separately.

[0515] The BPU may be equipped with a second gas inlet and / or a second gas outlet. In an embodiment, the BPU may be configured with gas inlets in each zone. In other embodiments, the BPU may be configured with gas outlets in each zone. can be a co-current or counter-current reactor.

[0516] In some embodiments, the material feed system includes a screw or auger feed mechanism. In some embodiments, the carbonaceous solids outlet may include a screw or auger output mechanism. Prepare.

[0517] Some embodiments utilize a rotary calciner with a screw material feed system. In some embodiments, some or all of the BPUs are axially rotatable, i.e. The rotational speed determines the solid flow pattern and the heat and mass transport. Each zone consists of flights arranged on the inner wall, which affect the solids agitation. The flights may be separately adjustable within each band.

[0518] Other means of agitating the solids may be used, such as an auger, screw, or paddle conveyor. In some embodiments, the BPUs are single BPUs distributed across each band. In another embodiment, the reactors are arranged throughout each zone. It includes a twin screw positioned on the

[0519] Some systems, especially those that maintain the approximate size of the feed material throughout the process, the ability to destroy or significantly damage the structure of a biomaterial. In some embodiments, the pyrolysis zone is designed with the capacity to process mass feedstock. , augers, screws, or other separators that tend to significantly reduce the size of the feed material being pyrolyzed. Does not include rake.

[0520] In some embodiments of the present disclosure, the system is disposed in operative communication with the outlet. and a process gas heater in which condensable vapors and non-condensable gases are removed. Process gas heaters accept separate fuels (such as natural gas) and oxidants (such as air). and into a combustion chamber suitable for combustion of at least a portion of the fuel and condensable vapors. Certain non-condensable gases, such as CO or CH4, can also be oxidized to CO2.

[0521] If a process gas heater is used, the system must generate at least the heat of combustion from the dryer. a heat exchanger disposed between the process gas heater and the dryer, the heat exchanger being configured to utilize a portion of the This embodiment can contribute significantly to the overall energy efficiency of the process. do.

[0522] In some embodiments, the system comprises a condensate in at least a partially condensed form. a material disposed in operable communication with the condenser configured to combine the reactive vapor with the solid. The material enrichment unit further comprises a biomass enrichment unit. The material enrichment unit is configured to enrich the biomass enriched from the carbon recovery unit. The carbon content of the original activated carbon may be increased.

[0523] The system further pyrolyzes the biogenic activated carbon to increase its carbon content. The pyrolysis zone may further comprise a separate pyrolysis zone adapted thereto. The separate pyrolysis zone may comprise a tank, a barrel, or the like. Relatively simple containers, units, such as boxes, bins, drums, totes, cloth bags, or roll-offs Or it may be a device.

[0524] The entire system can be in a fixed location or can be made portable. The system can be built using modules, which can be used to This system can be easily replicated for scale-up. It can also be constructed using the economic principles of

[0525] Some embodiments of the present disclosure relating to carbon enrichment of solids will now be further described. In some embodiments, the process for producing biogenic activated carbon comprises:

[0526] (a) providing a carbon-containing feedstock comprising biomass;

[0527] (b) optionally drying the feedstock to remove at least a portion of the moisture contained within the feedstock; Removal and

[0528] (c) optionally degassing the feedstock to remove any grit contained within the feedstock, if any; removing at least a portion of the interatomic oxygen;

[0529] (d) in a pyrolysis zone, in the presence of a substantially inert gas, Hot pyrolysis is carried out at a pyrolysis temperature selected from 700°C to about 700°C for at least 10 minutes. generating solids, condensable vapors, and non-condensable gases;

[0530] (e) removing at least a portion of the condensable vapors and at least a portion of the non-condensable gases from the hot pyrolysis solids; and to separate a part of it.

[0531] (f) in a cooling zone, in the presence of a substantially inert gas, the hot pyrolysis solid is cooled to about 1000 K. Cool below the decomposition temperature for at least 5 minutes to generate warm pyrolysis solids. And,

[0532] (g) Optionally cooling the warm pyrolysis solid in the cooler to produce a cold pyrolysis solid. And,

[0533] (h) subsequently scanning the hot and / or cold pyrolysis solids; At least a portion of the condensable vapor and / or at least a portion of the non-condensable gas from step (e) forming a concentrated pyrolysis solid having an increased carbon content through a further portion thereof;

[0534] (i) A biomass containing at least a portion of the concentrated pyrolysis solids in a carbon recovery unit. and recovering the source of activated carbon.

[0535] In some embodiments, step (h) comprises scouring the warm pyrolysis solid. and removing at least a portion of the condensable vapor from step (e) in vapor and / or condensed form. The process involves producing concentrated pyrolysis solids with increased carbon content. In an embodiment, step (h) comprises the step of (e) over the warm pyrolysis solid. and enriching the non-condensable gases from the pyrolysis process with an increased carbon content through at least a portion of the non-condensable gases from the pyrolysis process. This includes producing a solid.

[0536] In various embodiments, carbon enrichment is achieved by measuring carbon content, energy content, and mass yield. It should be understood that this increases the rate.

[0537] Alternatively, or in addition, the vapor or gas may be contacted with cold pyrolysis solids. In some embodiments, step (h) comprises the step ( e) passing at least a portion of the condensable vapor from the mixture in vapor and / or condensed form; In some embodiments, the method further comprises producing a concentrated pyrolysis solid having an increased carbon content. In step (h), the non-pyrolyzed solid from step (e) is dispersed throughout the cold pyrolysis solid. Passing at least a portion of the condensable gas through the pyrolysis process produces a concentrated pyrolysis solid having an increased carbon content. This includes achieving

[0538] In certain embodiments, step (h) comprises scouring the cooled pyrolysis solids. and (e) removing substantially all of the condensable vapor from step (e) in vapor and / or condensed form. The process involves producing concentrated pyrolysis solids having an increased carbon content. In an embodiment, step (h) comprises the step of (e) over the cold pyrolysis solid. Concentrated pyrolysis with increased carbon content through substantially all of the non-condensable gases from This includes producing a solid.

[0539] This process involves the step of separating the steam or gas prior to using the steam or gas for carbon enrichment. For example, the condensate obtained from step (e) may be treated or separated in various ways. an intermediate feed stream comprising at least a portion of the condensable vapor and at least a portion of the non-condensable gas; a separation unit configured to generate at least first and second output streams; In certain embodiments, the intermediate feed stream may comprise all of the condensable vapors, non-condensable vapors, and gases, or both.

[0540] Separation techniques include distillation columns, flash vessels, centrifuges, cyclones, membranes, filters, and packing machines. Separation may involve or use packed beds, capillary columns, etc. Separation may be carried out, for example, primarily by distillation, It can be based on absorption, adsorption, or diffusion and can be determined by vapor pressure, activity, molecular weight, density, viscosity, etc., for the stationary phase. utilizing differences in degree, polarity, chemical functionality, affinity, and any combination thereof. can be done.

[0541] In some embodiments, the first and second output streams are separated by an intermediate ratio based on their relative volatility. For example, the separation unit may be a distillation column, a flash tank, or It may be a condenser.

[0542] Thus, in some embodiments, the first output stream comprises condensable vapor and the second output stream comprises condensable vapor. The output stream of the process comprises non-condensable gases. Condensable vapors include terpenes, alcohols, acids, aldehydes, etc. The carbon-containing compound may include at least one selected from the group consisting of aldehydes, ketones, and methyl methyl ketones. These vapors contain aromatic compounds such as benzene, toluene, ethylbenzene, and xylene. Heavier aromatic compounds such as refractory tars may be present in the vapor. The gas is at least one selected from the group consisting of carbon monoxide, carbon dioxide, and methane. The carbon-containing molecule may include:

[0543] In some embodiments, the first and second output streams are separated based on their relative polarities. For example, the separation unit may be a stripping column, a packed bed, a chromatographic column, or a The substrate may be a lithography column, or a membrane.

[0544] Thus, in some embodiments, the first output stream comprises polar compounds and the second output stream comprises polar compounds. The output stream contains non-polar compounds. The polar compounds are methanol, furfural, and acetic acid. The non-polar compound may comprise at least one carbon-containing molecule selected from the group consisting of: , carbon monoxide, carbon dioxide, methane, terpene, and terpene derivatives. The compound may include at least one carbon-containing molecule selected from the group consisting of:

[0545] Step (h) is a step in which the biomass of the plant is reduced compared to an otherwise identical process. The total carbon content of the activated carbon may be increased. The degree of carbon content increase may vary in various embodiments. For example, the concentration may be about 1%, 2%, 5%, 10%, 15%, 25%, or even It is highly likely that

[0546] In some embodiments, step (h) comprises determining the fixed carbon content of the biogenic activated carbon. In these or other embodiments, step (h) increases the activity of the biogenic Increase the volatile carbon content of the charcoal. The volatile carbon content is due to volatile substances in the reagent. Volatile matter is carbon that contains aliphatic or aromatic compounds (e.g., terpenes). hydrogen hydrides; oxygenates, including alcohols, aldehydes, or ketones; and various tars Volatile carbons typically form solids under ambient conditions, but are not limited to these. When heated, the fixed carbon is either oxidized or gasified. , or otherwise released before being released as vapor.

[0547] Depending on the conditions associated with step (h), some amount of volatile carbon becomes fixed carbon (e.g. For example, by Boudouard carbon formation from CO. Typically, volatile materials is expected to enter the micropores of fixed carbon and exist as condensed / adsorbed species, but still relatively This residual volatility is a concern for product applications requiring high surface area and porosity. It may be comparatively more advantageous for fuel applications.

[0548] Step (h) determines the energy content (i.e., energy density) of the biogenic activated carbon. The increase in energy content can be attributed to the total carbon, fixed carbon, volatile carbon, or The degree of energy content increase may also be due to an increase in hydrogen. For example, the concentration may be about 1%, 2%, 5%, 10%, 15%, 25%, or even It is highly likely that

[0549] Further separation may be used to separate one or more non-agglomerated compounds for use in a process or further treatment. Condensable gases or vapors can be recovered, e.g., by further processing. This allows for the production of purified CO or synthesis gas.

[0550] As another example, separation of acetic acid followed by reduction of acetic acid to ethanol can be performed. The reduction may be accomplished at least in part using hydrogen derived from the non-condensable gases produced. do.

[0551] Condensable steam is either used for energy in the process (e.g., by thermal oxidation) or are either used in carbon enrichment to increase the carbon content of biogenic activated carbon Certain non-condensable gases, such as CO or CH4, can be added to the process. part of the substantially inert gas for the pyrolysis step A combination of any of the above is also possible. be.

[0552] A potential benefit of including step (h) is that the gas stream is scrubbed and the resulting gas The gas stream is enriched with CO and CO2. The resulting gas stream is - can be utilized for recovery, recycled for carbon enrichment of solids, and / or inert in the reactor Similarly, by separating non-condensable gases from condensable vapors, , the CO / CO2 stream may be, for example, an inert gas in the reactor system or the cooling system. It is prepared for use as a

[0553] Another variation of the present disclosure is that the principle of the carbon enrichment step can be applied to any feed where the addition of carbon is desired. It is assumed that the above can be applied to raw materials.

[0554] In some embodiments, a batch or continuous process for producing biogenic activated carbon is used. Process is

[0555] (a) providing a solids stream comprising a carbon-containing material;

[0556] (b) Condensable carbon-containing vapors, non-condensable carbon-containing gases, or condensable carbon-containing vapors and non-condensable carbon-containing gases. providing a gas stream comprising a mixture of condensable carbon-containing gases;

[0557] (c) passing a gas stream over a solid stream under favorable conditions to produce a carbon-containing material and forming a carbon-containing product having an increased carbon content.

[0558] In some embodiments, the starting carbon-containing material is pyrolyzed biomass or torrefied biomass. The gas stream may be obtained during an integrated process to provide a carbon-containing material; or The gas stream may be obtained from another process of the carbon-containing material. The gas stream, or a portion thereof, may be obtained from an external source. (e.g., ovens in sawmills). Mixtures of gas streams, as well as various A mixture of carbon-containing materials from sources is possible.

[0559] In some embodiments, the process involves re-opening the gas flow to repeat the process. Recycle or reuse it to recover the carbon and / or energy content of the carbon-containing product. In some embodiments, the process further comprises further increasing the ghee content. The process involves recirculating or reusing the gas stream to carry out this process. Increasing the carbon and / or energy content of a feedstock different from the carbon-containing material It further includes:

[0560] In some embodiments, the process generates at least a first and a second output stream. and further comprising introducing the gas stream into a separation unit configured to: The first and second output streams include a mixture of condensable carbon-containing vapor and non-condensable carbon-containing gas. may be separated based on relative volatility, relative polarity, or any other property. It may be obtained from another processing of the carbon-containing material.

[0561] In some embodiments, the process involves re-opening the gas flow to repeat the process. Recycle or reuse it to further increase the carbon content of the carbon-containing product. In some embodiments, the process further comprises: The gas stream is recycled or reused to reduce the carbon content of another feedstock. and increasing the

[0562] The carbon-containing product may have an increased total carbon content, higher solids, or the like compared to the starting carbon-containing material. Constant carbon content, higher volatile carbon content, higher energy content, or any of these It may have any combination.

[0563] In a related variation, the biogenic activated carbon production system comprises:

[0564] (a) a material feed system configured to introduce a carbon-containing feedstock;

[0565] (b) a material feed system configured to remove moisture contained within the carbon-containing feedstock; an optional dryer disposed in operable communication with the stem;

[0566] (c) a BPU disposed in operable communication with the dryer (wherein the BPU is spatially separated from the dryer); at least one pyrolysis zone disposed in operative communication with a cooling zone; U may comprise an outlet for removing condensable vapors and non-condensable gases from the solids),

[0567] (d) a cooler disposed in operable communication with the BPU;

[0568] (e) throughout the solid to form a concentrated solid with increased carbon content operatively associated with the cooler, configured to pass condensable vapors and / or non-condensable gases; a material concentration unit disposed therethrough;

[0569] (f) a carbon recovery unit disposed in operable communication with the material concentration unit; do.

[0570] The system may further include a preheating zone disposed in operative communication with the pyrolysis zone. In some embodiments, the dryer is configured as a drying zone within the BPU. Each can be installed in a single BPU or in separate BPUs. It may be placed within.

[0571] In some embodiments, the cooling zone is configured with a gas inlet and the pyrolysis zone is configured with a gas inlet. an outlet configured to generate a gas phase flowing substantially countercurrently to the solid phase; In these or other embodiments, the preheating zone and / or drying zone (or drying The reactor is configured with a gas outlet to generate a gas phase that flows substantially countercurrently to the solid phase. It is possible.

[0572] In certain embodiments, the system comprises:

[0573] (i) a housing having an upper and lower portion;

[0574] (ii) a bottom inlet at the bottom of the enclosure;

[0575] an inlet configured to carry a condensable vapor and a non-condensable gas;

[0576] (iii) a top outlet at the top of the enclosure;

[0577] an outlet configured to carry a concentrated gas stream derived from the condensable vapor and the non-condensable gas;

[0578] (iv) a passageway defined between the upper and lower portions of the enclosure;

[0579]

[0580] (v) a material transport system following the passageway, configured to transport solids; The body contains at least a portion of the condensable vapor and / or at least a portion of the non-condensable gas. Incorporates a material concentration unit with a material concentration unit (shaped to adsorb a portion of the material).

[0581] The present disclosure describes various compositions useful as biogenic activated carbons, as well as methods incorporating these agents. In some variations, the biogenic activated carbon can produce products including: Produced by any process disclosed herein, such as a process comprising the steps of:

[0582] (a) providing a carbon-containing feedstock comprising biomass;

[0583] (b) optionally drying the feedstock to remove at least a portion of the moisture contained within the feedstock; removing the

[0584] (c) optionally degassing the feedstock to remove any grit contained within the feedstock, if any; removing at least a portion of the interatomic oxygen;

[0585] (d) in a pyrolysis zone, in the presence of a substantially inert gas, Hot pyrolysis is carried out at a pyrolysis temperature selected from 700°C to about 700°C for at least 10 minutes. generating solids, condensable vapors, and non-condensable gases;

[0586] (e) removing at least a portion of the condensable vapors and at least a portion of the non-condensable gases from the hot pyrolysis solids; and separating a portion of the mixture.

[0587] (f) in a cooling zone, in the presence of a substantially inert gas, the hot pyrolysis solid is cooled to about 1000 K. Cool below the decomposition temperature for at least 5 minutes to generate a warm pyrolysis solid. Tep and

[0588] (g) cooling the warm pyrolysis solid to generate a cold pyrolysis solid;

[0589] (h) recovering the biogenic activated carbon containing at least a portion of the cold pyrolysis solids; Pu.

[0590] In some embodiments, the process for producing biogenic activated carbon comprises warm Pyrolysis solids or cold pyrolysis solids are sized (e.g., sorted, screened, classified, etc.) ) to form a sized pyrolyzed solid. The resulting pyrolysis solids are suitable for applications requiring activated carbon products with certain particle size characteristics. It can be used as follows.

[0591] In some embodiments, the biogenic activated carbon has a dry basis of at least about 55 % by weight, for example, at least 55% by weight, at least 60% by weight, at least 65% by weight , at least 70% by weight, at least 75% by weight, at least 80% by weight, at least 8 5% by weight, at least 90% by weight, at least 95% by weight, at least 96% by weight, at least 97%, at least 98%, or at least 99% by weight of total carbon Total carbon includes at least fixed carbon and may further include carbon from volatile materials. In some embodiments, the carbon from volatile matter is the total carbon present in the biogenic activated carbon. Approximately at least 5%, at least 10%, at least 25%, or at least 5% of the For example, fixed carbon can be measured using ASTM D3172, while volatile carbon is Decomposable carbon can be estimated using ASTM D3175.

[0592] Biogenic activated carbon according to the present disclosure may contain from about 0% to about 8% hydrogen by weight. In some embodiments, the biogenic activated carbon contains more than about 0.5% hydrogen by weight, e.g., about 0.6% by weight, approximately 0.7% by weight, approximately 0.8% by weight, approximately 0.9% by weight, approximately 1% by weight, approximately 1. 2% by weight, approximately 1.4% by weight, approximately 1.6% by weight, approximately 1.8% by weight, approximately 2% by weight, approximately 2.2% by weight Amount%, approx. 2.4 wt%, approx. 2.6 wt%, approx. 2.8 wt%, approx. 3 wt%, approx. 3.2 wt% , about 3.4 wt%, about 3.6 wt%, about 3.8 wt%, about 4 wt%, or about 4 wt% The hydrogen content of the biogenic activated carbon may be any suitable amount known in the art. It can be determined by methods such as the combustion analysis procedures outlined in ASTM D5373. In some embodiments, the biogenic activated carbon is derived from a fossil fuel source. It has a hydrogen content that exceeds that of activated carbon, typically fossil fuel-based activated carbon. The product has about 1% by weight or less hydrogen, for example, about 0.6% by weight hydrogen. In embodiments, the properties of the activated carbon product are determined by measuring the amount of fossil fuel-based activated carbon product (including i.e., those with very low hydrogen content) compared with the hydrogen content of fossil fuel-based activated carbon products. and blending with a suitable amount of a biogenic activated carbon product having a hydrogen content exceeding the and

[0593] The biogenic activated carbon may contain, on a dry basis, about 10% by weight or less of water, e.g., about 5% by weight or less. The biogenic activated carbon product may contain about 1% by weight or less, e.g., about Biogenic activated carbon products may contain up to 0.5% by weight of nitrogen, on a dry basis, approximately 0. It may contain 5% by weight or less, for example, about 0.2% by weight or less, of phosphorus. may contain about 0.2% by weight or less, e.g., about 0.1% by weight or less, sulfur on a dry basis. .

[0594] In certain embodiments, the biogenic activated carbon contains up to 20% by weight of oxygen, e.g., Approximately 0.2% by weight, approximately 0.5% by weight, approximately 1% by weight, approximately 2% by weight, approximately 3% by weight, approximately 4% by weight, Approximately 5% by weight, approximately 6% by weight, approximately 7% by weight, approximately 7.5% by weight, approximately 8% by weight, approximately 9% by weight, approximately 1 0% by weight, approximately 11% by weight, approximately 12% by weight, approximately 13% by weight, approximately 14% by weight, approximately 15% by weight, about 16%, about 17%, about 18%, about 19%, or about 20% by weight of oxygen The presence of oxygen in activated carbon is particularly related to the presence of halogens (such as chlorine or bromine). Together, they may be beneficial for certain applications, such as mercury capture. Biogenic activated carbon has an oxygen content that exceeds that of activated carbon derived from fossil fuel sources. Typically, fossil fuel-based activated carbon products contain less than about 10% by weight of oxygen, e.g. , about 7% oxygen by weight, or about 0.3% oxygen by weight. The properties of the activated carbon product are determined by the amount of fossil fuel-based activated carbon product (i.e., very low (which has a low oxygen content) with an oxygen content exceeding that of fossil fuel-based activated carbon products Optimized by blending with a suitable amount of biogenic activated carbon product with a suitable amount of hydroxybenzoate. It can be done.

[0595] Carbon, hydrogen, and nitrogen are measured, for example, using ASTM D5373 for ultimate analysis. Oxygen can be estimated, for example, using ASTM D3176. Sulfur can be measured using For example, it can be measured using ASTM D3177.

[0596] Certain embodiments may contain hydrogen (other than any moisture that may be present), nitrogen, phosphorus, or sulfur. To provide a reagent having little or essentially no yellow color, and substantially carbon and Any ash and moisture present. Therefore, some embodiments may be dry / ash-free. (DAF) based materials with up to (and including) 100% carbon.

[0597] Generally speaking, feedstocks such as biomass contain silica and other carbon-containing compounds that are not readily released during pyrolysis. It goes without saying that ash-free feedstocks contain non-volatile species, including iron and various metals. It is possible to use pyrolysis solids containing ash, in which case there should not be a significant amount of ash in the pyrolysis solids. Ash can be measured, for example, using ASTM D3174.

[0598] Varying amounts of non-combustible material such as ash may be present. Biogenic activated carbon has a dry base of approximately 1 0% by weight or less, for example, about 5% by weight, about 2% by weight, about 1% by weight, or about 1% by weight or less In certain embodiments, the reagent contains little or no ash. or contains essentially no ash or other non-combustible material. This embodiment provides essentially pure carbon containing 100% carbon on a dry basis.

[0599] Varying amounts of moisture can be present. On a total mass basis, biogenic activated carbon contains at least 1% %, at least 2% by weight, at least 5% by weight, at least 10% by weight, at least 1 5% by weight, at least 25% by weight, at least 35% by weight, at least 50% by weight, or may contain 50% or more by weight of water. As intended herein, "moisture" refers to absorbed water. in biogenic activated carbon products, including water molecules, adsorbed water molecules, chemical hydrates, and physical hydrates. The equilibrium water content should be interpreted as including any form of water present in the The moisture content may also change depending on the local environment, such as relative humidity. Moisture content varies during transportation and other logistics processes. The amount of ATP that can be measured may be determined by any suitable method known in the art, including by any suitable method known in the art.

[0600] For this purpose, biogenic activated carbon is used to achieve the higher heat value associated with the total combustion of bone-dry reagents. They may have different "energy contents," which means energy densities based on the The original activated carbon should be approximately at least 11,000 Btu / lb, at least 12,000 Btu / lb, at least 13,000Btu / lb, at least 14,000Btu / lb, or at least 15,000 Btu / lb. In certain embodiments, the energy content is about 14,000-15,000 Btu / The energy content is measured using methods known in the art, including, for example, ASTM D5865. It may be measured by any suitable method known in the art.

[0601] The biogenic activated carbon may be formed into a powder, such as a coarse or fine powder. For example, the reagent may be In some embodiments, about 200 mesh, about 100 mesh, about 50 mesh, Average mesh size: about 10 mesh, about 6 mesh, about 4 mesh, or about 2 mesh In some embodiments, the biogenic activated carbon can be formed into a powder having a maximum Approximately 500μm, for example, approximately 10μm or less, approximately 10μm, approximately 25μm, approximately 50μm, approximately 7 5 μm, about 100 μm, about 200 μm, about 300 μm, about 400 μm, or about 500 μm It has an average particle size of m.

[0602] Biogenic activated carbon generally has a size predominantly of about 0.21 mm (70 mesh) or less. Biogenic activated carbon can be produced as powdered activated carbon containing particles ranging in size from 0.2 mm to It can be produced as granular activated carbon, comprising irregularly shaped particles having sizes in the 5 mm range. Biogenic activated carbon is generally available in extruded and cylindrical shapes with diameters between 0.8 mm and 5 mm. The activated carbon may be produced as a pelletized activated carbon containing the material.

[0603] In some embodiments, the biogenic activated carbon is in the form of pressed particles, bound particles, or agglomerates. The starting material for forming these objects is a particle-reducing material. These bodies may be in powder form, such as the intermediates obtained by or by other means of agglomerating the particles, may be formed by mechanical pressure or other forces. do.

[0604] After formation from pyrolysis, the biogenic activated carbon may be pulverized to form a powder. "Micronization" in this context means any sizing, milling, pulverization, or other process to reduce the average particle size. It is intended to include grinding, crushing, extrusion, or other primarily mechanical processes. Micronization can be performed in batch, continuous, or continuous mode, and can be assisted by chemical or electrical forces, if desired. It may be a continuous or semi-continuous process, and in some embodiments, the pyrolysis solids are formed at a rate of 1000 kJ / min. The process may be performed at a different location than the one in which the process is performed.

[0605] In some embodiments, the biogenic activated carbon is produced in the form of a structured object, The structure is substantially derived from the feedstock. For example, feedstock chips are a type of biogenic activated carbon. Alternatively, the feedstock cylinder may produce a biogenic activated carbon cylinder. , which may be slightly smaller than the starting material, but otherwise have the same basic structure and and can maintain its shape.

[0606] The biogenic activated carbon according to the present disclosure has a thickness of at least about 1 cm, 2 cm, 3 cm, 4 cm, 5 cm, cm, 6cm, 7cm, 8cm, 9cm, 10cm or more It may be generated as an object or formed into such an object. , the minimum or maximum dimension may be a length, width, or diameter.

[0607] Other variations of the present disclosure involve the incorporation of additives into the process, the product, or both. In some embodiments, biogenic activated carbon is incorporated into the process. In these or other embodiments, the activated carbon comprises at least one process additive. , including at least one product additive that is introduced into the activated carbon after this process.

[0608] Other variations of the present disclosure involve the incorporation of additives into the process, the product, or both. In some embodiments, biogenic activated carbon is incorporated into the process. In these or other embodiments, the reagent comprises at least one process additive. and at least one product additive introduced into the reagent after this process.

[0609] In some embodiments, the biogenic activated carbon has, on a dry basis:

[0610] 55% by weight or more total carbon;

[0611] not more than 5% by weight of hydrogen,

[0612] not more than 1% by weight of nitrogen;

[0613] optionally 0.5% to 10% by weight of oxygen;

[0614] not more than 0.5% by weight of phosphorus;

[0615] not more than 0.2% by weight of sulfur, and

[0616] from metals, metal oxides, metal hydroxides, metal halides, or combinations thereof Contains selected additives.

[0617] Additives include iron chloride, iron bromide, magnesium, manganese, aluminum, nickel, and chromium. Calcium, silicon, magnesium oxide, dolomite, dolomitic lime, fluorite, fluoro Selected from spar, bentonite, calcium oxide, lime, or a combination thereof However, it is by no means limited to these.

[0618] In some embodiments, the biogenic activated carbon has, on a dry basis:

[0619] 55% by weight or more total carbon;

[0620] not more than 5% by weight of hydrogen,

[0621] not more than 1% by weight of nitrogen;

[0622] optionally 0.5% to 10% by weight of oxygen;

[0623] not more than 0.5% by weight of phosphorus;

[0624] not more than 0.2% by weight of sulfur, and

[0625] It includes an additive selected from an acid, a base, or a salt thereof.

[0626] Additives include sodium hydroxide, potassium hydroxide, magnesium oxide, hydrogen bromide, and chloride water. sodium silicate, potassium permanganate, organic acids (e.g., citric acid), or The combination may be selected from, but is in no way limited to, these.

[0627] In certain embodiments, the biogenic activated carbon comprises, on a dry basis:

[0628] 55% by weight or more total carbon;

[0629] not more than 5% by weight of hydrogen,

[0630] not more than 1% by weight of nitrogen;

[0631] optionally 0.5% to 10% by weight of oxygen;

[0632] not more than 0.5% by weight of phosphorus;

[0633] not more than 0.2% by weight of sulfur;

[0634] from metals, metal oxides, metal hydroxides, metal halides, or combinations thereof a selected first additive, and

[0635] a second additive selected from an acid, a base, or a salt thereof;

[0636] The first additive is different from the second additive.

[0637] The first additive is iron chloride, iron bromide, magnesium, manganese, aluminum, nickel , chromium, silicon, magnesium oxide, dolomite, dolomitic lime, fluorite, Select from Fluorospar, bentonite, calcium oxide, lime, or a combination of these. The second additive may be independently selected from sodium hydroxide, potassium hydroxide, and ammonium hydroxide. Magnesium, hydrogen bromide, hydrogen chloride, sodium silicate, potassium permanganate, organic acids (e.g., citric acid), or combinations thereof.

[0638] Certain biogenic activated carbons contain, on a dry basis, carbon, hydrogen, nitrogen, oxygen, phosphorus, and sulfur. , non-combustible materials, as well as iron chloride, iron bromide, magnesium, manganese, aluminum, nickel Kel, chromium, silicon, magnesium oxide, dolomite, dolomitic lime, fluorite , Fluorospar, Bentonite, Calcium Oxide, Lime, and combinations thereof The composition consists essentially of an additive selected from the group consisting of:

[0639] Certain biogenic activated carbons contain, on a dry basis, carbon, hydrogen, nitrogen, oxygen, phosphorus, and sulfur. , non-flammable materials, as well as sodium hydroxide, potassium hydroxide, magnesium oxide, and aqueous bromide The compound is selected from the group consisting of hydrogen chloride, hydrogen chloride, sodium silicate, and combinations thereof. Consisting essentially of additives.

[0640] The amount of additive (or total additives) may be, for example, about 0.1% by weight, about 1% by weight, or less on a dry basis. about 0.01% by weight to about 25% by weight, including about 5% by weight, about 10% by weight, or about 20% by weight The amount of additive may vary greatly. When incorporated into the diet, the energy content calculated on the basis of the total activated carbon weight (including additives) is reduced. It is understood that the additive(s) may be reduced. Biogenic activated carbon having a % or less of hydroxybenzoic acid, based on the total weight of the biogenic activated carbon (including additive(s)). If based on approximately at least 11,000 Btu / lb, at least 12,000 Btu / lb, at least 13,000 Btu / lb, at least 14,000 Btu / lb, Or it may have an energy content of at least 15,000 Btu / lb.

[0641] The above discussion regarding product morphology also applies to embodiments incorporating additives. Certain embodiments may be used as binders or to enhance final properties for specific applications. Other additives are incorporated as modifiers.

[0642] In some embodiments, the majority of the carbon in the biogenic activated carbon is renewable. In some embodiments, substantially all of the carbon is Certain market mechanisms (e.g., renewable identification numbers, tax credits, etc.) exist. The value stems from the renewable carbon content in biogenic activated carbon. In embodiments, the additive itself is derived from a biogenic source or is otherwise renewable. Some organic acids, such as citric acid, are derived from renewable carbon sources. Thus, in some embodiments, the bioactive The carbon content of the charcoal consists of, consists essentially of, or consists substantially of renewable carbon. For example, the fully biogenic activated carbon formed by the methods disclosed herein can be: (a) recycled; (b) pyrolysis solids derived exclusively from biomass from renewable carbon sources, and (c) renewable carbon Consisting of, consisting essentially of, or consisting substantially of one or more additives derived exclusively from the source .

[0643] The biogenic activated carbon produced as described herein can be used to produce a wide variety of carbonaceous products. In some variations, the product obtained by the process of the present disclosure is useful for or a biogenic activated carbon as described in the compositions described herein, or any portion, combination, or derivative of any of the following:

[0644] Generally speaking, biogenic activated carbon can be burned to produce energy (including electricity and heat). or partially oxidized or steam reformed to produce synthesis gas, or their adsorption or utilized for its absorption properties, or in metal refining (reduction of metal oxides, etc.) or other industrial applications. Utilized for their reactive properties during processing or for carbon steel and various other metals They can be utilized for their material properties in alloys. Essentially, biogenic activated carbons are: For any market application of carbon-based articles or advanced materials, including special applications that may be developed It can be used.

[0645] Biogenic activated carbon prepared according to the processes disclosed herein is a biomass fuel that can be used in a variety of applications, including: In some embodiments, the activated carbon has the same or better properties than conventional activated carbon. In this study, biogenic activated carbons matched or exceeded the surface area associated with fossil-fuel-based activated carbons. In some embodiments, the surface area of ​​the Biogenic activated carbons are known to remove contaminants as well as or better than conventional activated carbon products. In some embodiments, the biogenic activated carbon can be used in a variety of ways, including: Comparable or equivalent to the level of inert material (e.g., ash) associated with activated carbon products. have a level of inert material (e.g., ash) that is at or about below In embodiments, the biogenic activated carbon has particle size and / or particle size associated with conventional activated carbon products. or particle size distribution comparable to, equal to, greater than, or approximately less than In some embodiments, the bioactive The carbon product is comparable to or substantially similar to the particle shape associated with conventional activated carbon products. In some embodiments, the biological The original activated carbon product has particle shapes that differ substantially from those associated with conventional activated carbon products. In some embodiments, the biogenic activated carbon product has a shape similar to that of conventional activated carbon. Pore ​​volume comparable to, equal to, or exceeding the pore volume associated with the product In some embodiments, the biogenic activated carbon product has a volume. Comparable to, substantially similar to, or the pore size associated with the product In some embodiments, the biobased activation product has the same pore size. Comparable to or substantially similar to particle friction resistance values ​​associated with conventional activated carbon products. In some embodiments, the frictional resistance of the particles is equal to or the same as that of the particles. The bio-derived activated carbon products are comparable to or have comparable hardness values ​​to those associated with conventional activated carbon products. In some embodiments, the hardness value is qualitatively similar to or identical to that of the hardness value ... Therefore, biogenic activated carbon products are comparable to or exceed hardness values ​​associated with conventional activated carbon products. Qualitatively, the hardness value is about equal to or less than the hardness value of ... In this state, biogenic activated carbon products have bulk density values ​​associated with conventional activated carbon products. Having a bulk density value that is comparable to, substantially similar to, or identical to In some embodiments, the biogenic activated carbon product is a biodegradable activated carbon product, which is generally related to conventional activated carbon products. comparable to, substantially below, or nearly below the bulk density value In some embodiments, the biogenic activated carbon product has a bulk density value that is comparable to or substantially similar to the absorption capacity associated with activated carbon products of has the same absorption capacity.

[0646] Prior to suitability or actual use in any product application, the biogenic activated carbon of the present disclosure must be , can be analyzed, measured, and optionally modified (eg, by additives) in a variety of ways. Some potentially interesting properties besides chemical composition and energy content include density, Particle size, surface area, microporosity, absorption, adsorption, binding capacity, reactivity, desulfurization activity, basicity, hardness , and iodine value.

[0647] Some variations of the present disclosure provide various activated carbon products. Activated carbon is used in a variety of applications, including water treatment, air purification, and Gas refining, solvent vapor recovery, food and beverage processing, sugar refining and sweetener refining, automotive applications, It is used in a wide variety of liquid and gas phase applications, including pharmaceuticals. Important product characteristics include particle size, shape, and composition; surface area, pore volume, and pore size; distribution, carbon surface and internal chemistry, particle abrasion resistance, hardness, bulk density, and Adsorption capacity may be included.

[0648] The surface area of ​​biogenic activated carbon can vary widely. An exemplary surface area is about 500 m 2 / g , 600m 2 / g, 800m2 / g, 1000m 2 / g, 1200m 2 / g, 1400m 2 / g, 1600m 2 / g, or 1800m 2 / g etc. approx. 400m 2 / g~approx. 2000 m 2 / g or greater. Surface area generally correlates with adsorption capacity.

[0649] The iodine number is a parameter used to characterize the performance of activated carbon. is the result of measuring the degree of carbon activation and the content of micropores (e.g., 0-20 Å). This is an important measurement for liquid phase applications. Other pore-related measurements include mesopores. methylene blue to measure the pore size (e.g., 20–500 Å), and macropore content ( For example, the Molasses Number, which measures the molasses content (>500 Å), is included. Pore ​​size distribution and pore volume are important in determining ultimate performance. Biogenic activated carbon Typical bulk densities of are about 400-500 g / liter, such as about 450 g / liter. do.

[0650] Hardness or Abrasion Number is a measure of the abrasion resistance of activated carbon. This is due to the ability of activated carbon to withstand frictional forces and mechanical stress during handling and use. It is a measure of physical integrity. A certain amount of hardness is desirable, but too much hardness can lead to over-hardening of the device. Excessive wear may occur. Exemplary wear values ​​measured according to ASTM D3802 are approximately 1%. Approximately 5%, approximately 10%, approximately 15%, approximately 20%, approximately 25%, approximately 30%, approximately 35%, approximately 40%, approximately 45%, approx. 50%, approx. 55%, 60%, approx. 65%, approx. 70%, approx. 75%, approx. 80%, approx. 8 5%, approximately 90%, approximately 95%, approximately 96%, approximately 97%, approximately 98%, approximately 99%, or approximately 99% The range of super-equivalents is from about 1% to over about 99%.

[0651] In some embodiments, the biogenic activated carbon is subjected to friction in the main activated carbon processing facility. An optimum range of hardness can be achieved that is reasonably resistant to wear but does not cause abrasion and abrasion. This optimum condition is determined in some embodiments of the present disclosure by the feedstock as well as the processing conditions. This is possible by selecting the items.

[0652] For example, coconut shells tend to achieve abrasion values ​​of over 99%. It is known that this is a suboptimal feedstock for achieving optimal hardness. In some embodiments where the process of the present disclosure can address high hardness requirements, By operating it, you can increase or maximize the hardness by about 75%, about 80%, about 8 5%, approximately 90%, approximately 95%, approximately 96%, approximately 97%, approximately 98%, approximately 99%, or approximately 99% In accordance with the present invention, a biogenic activated carbon product can be produced having an abrasion value of greater than 0.05%.

[0653] The biogenic activated carbon provided by the present disclosure has a wide range of commercial applications. Without limitation, biogenic activated carbon is widely used in emission control, water purification, groundwater treatment, wastewater treatment, air scrubbing, and Par applications, PCB removal applications, deodorization applications, soil vapor extraction, city gas plants, industrial water filtration , industrial fumigation, tank and process vents, pumps, blowers, filters, pre-filters in mist filters, piping, piping modules, adsorbers, absorbers, and columns It can be used.

[0654] Some variations have, on a dry basis, about 55% or more by weight total carbon, about 15% or less by weight A biogenic activated carbon composition is provided that contains hydrogen and about 1% by weight or less of nitrogen, and the activated carbon composition The article is characterized by an iodine number greater than about 500, and at least a portion of the carbon is a graphene. It exists in the form

[0655] In some embodiments, the composition is responsive to an externally applied magnetic field or The magnetic field contains additives that respond to an externally applied magnetic field. Such additives are iron or iron-containing. Graphene itself (without additives) can be induced by an externally applied magnetic field. Can respond.

[0656] Some variations have, on a dry basis, about 55% or more by weight total carbon, about 15% or less by weight Organisms containing hydrogen, less than about 1% by weight of nitrogen, and about 0.0001% to about 1% by weight of iron and a method for producing activated carbon compositions comprising the steps of: providing a first activated carbon composition having a first carbon atom and a second carbon atom; The carbonaceous composition is characterized by an iodine value greater than about 500, and the composition is resistant to externally applied Responds to magnetic fields.

[0657] Some variations have, on a dry basis, about 55% or more by weight total carbon, about 15% or less by weight Biogenic, containing hydrogen, less than about 1% by weight of nitrogen, and about 0.1% to about 1% by weight of iron An activated carbon composition is provided, the activated carbon composition being characterized by an iodine value greater than about 500, The object responds to an externally applied magnetic field.

[0658] Some variations have, on a dry basis, about 55% or more by weight total carbon, about 15% or less by weight A biogenic activated carbon composition is provided that contains hydrogen and about 1% by weight or less of nitrogen, and the activated carbon composition The article is characterized by an iodine number greater than about 500, and at least a portion of the carbon is a graphene. It exists in the form

[0659] The present disclosure provides a biogenic graphene-containing product characterized by an iodine value greater than about 500. Also provided.

[0660] Some variations of the present disclosure use biogenic activated carbon compositions to reduce emissions. A method is provided, the method comprising:

[0661] (a) providing activated carbon particles comprising a biogenic activated carbon composition;

[0662] (b) providing a gas-phase exhaust stream containing at least one selected contaminant;

[0663] (c) Additives selected to assist in the removal of selected contaminants from the gas-phase effluent stream. Providing things and

[0664] (d) introducing activated carbon particles and additives into the gas phase exhaust stream to reduce the concentration of selected contaminants; adsorbing at least a portion of the contaminant onto activated carbon particles, thereby forming contaminant-adsorbed carbon particles in the gas-phase effluent stream; To produce offspring,

[0665] (e) separating at least a portion of the contaminant-adsorbed carbon particles from the gas-phase effluent stream to determine whether the contaminants are present in the contaminant-adsorbed carbon particles; and producing a reduced gas phase exhaust stream.

[0666] The additive in the biogenic activated carbon composition is provided as part of the activated carbon particles; or Alternatively or additionally, the additive may be introduced directly into the gas phase exhaust stream, fuel bed, or combustion zone. Those skilled in the art will recognize that additives can be added directly or indirectly to the gas phase exhaust stream to remove selected contaminants. Other methods of direct or indirect introduction are also feasible.

[0667] The selected contaminants (in gas phase effluent streams) were mercury, boron, selenium, arsenic, and The metal may be a metal such as a metal selected from the group consisting of any of the compounds, salts, and mixtures thereof. The pollutants selected may be, for example, hazardous air pollutants, organic compounds (e.g., VOCs), or may be a non-condensable gas. In some embodiments, the biogenic activated carbon product comprises: Adsorbs and absorbs higher amounts of selected contaminants than comparable amounts of non-biogenic activated carbon products. In some such embodiments, the selected The contaminants include metals, hazardous air pollutants, organic compounds (e.g., VOCs), non-condensable gases, and is any combination thereof. In some embodiments, the selected contaminant is In some embodiments, the selected contaminants include one or more VOCs. In some embodiments, the biogenic activated carbon contains at least about 1% by weight of hydrogen. and / or contains at least about 10% by weight oxygen.

[0668] Harmful air pollutants can cause cancer or other serious health effects, such as reproductive or causes or may cause birth defects or adverse environmental and ecological effects Section 112 of the Clean Air Act, as amended is incorporated herein by reference in its entirety. Pursuant to Section 112 of the Clean Air Act, U.S. Environmental Protection Agency: The EPA is mandated to control 189 harmful air pollutants. Any current or future compound classified as a hazardous air pollutant is a possible Included among selected potential contaminants.

[0669] Volatile organic compounds (some of which are also harmful air pollutants) are usually These are organic chemicals that have high vapor pressures at room temperature. Examples include short-chain alkanes, olefins, and Many volatile organic compounds include phenols, alcohols, ketones, and aldehydes. are dangerous to human health or harmful to the environment. The EPA Regulating Volatile Organic Compounds in Land. The EPA's definition of Volatile Organic Compounds is found in 40 Federal Regulations. and is set forth in CFR 51.100, which is incorporated herein by reference in its entirety. be absorbed.

[0670] Non-condensable gases are gases that do not condense under normal room temperature conditions. Non-condensable gases include nitrogen. Oxides, carbon monoxide, carbon dioxide, hydrogen sulfide, sulfur dioxide, sulfur trioxide, methane, ethane ethylene, ozone, ammonia, or a combination thereof, Not limited.

[0671] Multiple contaminants can be removed by activated carbon particles. The dye-adsorbed carbon particles may be capable of adsorbing at least two contaminants, at least three contaminants, or more The biogenic activated carbon disclosed herein is useful for the control of multiple contaminants, including: and may allow for the control of certain targeted contaminants (e.g., selenium).

[0672] In certain embodiments, the contaminant-adsorbing carbon particles may be contaminant-adsorbing particles that are contaminant-adsorbing. and at least one, at least two, or at least three of sulfur dioxide, or Includes all of the above (in any combination).

[0673] The separation in step (e) can be carried out, for example, by filtration (e.g., a woven fabric filter) or electrostatic Woven fabric filters, also known as baghouses, can be used in e.g. Measured woven filter tubes, envelopes, or cartridges may be utilized. Shaker style and reverse-air systems There are several types of baghouses, including: It may also include a wash.

[0674] Electrostatic precipitators or electrostatic air cleaners use the force of induced electrostatic charges to remove particles from flowing gases. Electrostatic precipitators are particle collection devices that minimize the flow of gas through the device. Highly efficient, with minimal obstruction, that can easily remove particulate matter from the airflow Electrostatic precipitators are filtering devices that apply energy only to the particulate matter they collect. No additional heat is added and therefore it is very efficient in terms of energy (electricity) consumption.

[0675] Electrostatic precipitators can be dry or wet. Wet electrostatic precipitators operate with a saturated gas flow. Wet electrostatic precipitators are used to remove liquid droplets such as sulfuric acid mist from industrial process gas streams. , the gas has a high moisture content, the gas contains flammable particles, or the gas is viscous in nature. This can be useful when having adhesive particles.

[0676] In some embodiments, the contaminant-adsorbed carbon particles are treated to regenerate the activated carbon particles. In some embodiments, the method includes thermally oxidizing the contaminant-adsorbed carbon particles. The contaminant-adsorbed carbon particles or a regenerated form thereof can be burned to provide energy. This can be done.

[0677] In some embodiments, the additive is an acid, a base, a salt, a metal, a metal oxide, a metal hydroxide The metal may be selected from a metal hydride, a metal halide, or a combination thereof. In this embodiment, the additives are magnesium, manganese, aluminum, nickel, iron, chromium , silicon, boron, cerium, molybdenum, phosphorus, tungsten, vanadium, iron chloride, Iron bromide, magnesium oxide, dolomite, dolomitic lime, fluorite, fluorospa -, bentonite, calcium oxide, lime, sodium hydroxide, potassium hydroxide, bromide water Acid, hydrogen chloride, sodium silicate, potassium permanganate, organic acids (e.g., citric acid) and combinations thereof.

[0678] In some embodiments, the gas phase exhaust stream is a mixture of a fuel containing a biogenic activated carbon composition. It comes from combustion.

[0679] In some embodiments, particularly those related to mercury removal, biogenic activated carbon compositions are used. Ways to reduce mercury emissions include:

[0680] (a) providing activated carbon particles comprising a biogenic activated carbon composition that includes iron or an iron-containing compound; To do,

[0681] (b) providing a gas phase effluent stream containing mercury;

[0682] (c) introducing activated carbon particles into the gas phase effluent stream to deposit at least a portion of the mercury onto the activated carbon particles; thereby generating mercury-adsorbed carbon particles in the gas phase exhaust stream;

[0683] (d) Removal of at least mercury-adsorbed carbon particles from gas-phase emissions using electrostatic precipitation or filtration. and separating a portion of the mercury-reduced gas phase effluent stream.

[0684] In some embodiments, biogenic activated carbon compositions are used to treat emissions (e.g., mercury) The method for reducing the carbon footprint further includes using biogenic activated carbon as a fuel source. In such embodiments, potential contaminants are adsorbed, absorbed, and / or chemisorbed. In addition to the ability of biogenic activated carbon products to reduce emissions by Thus, in an exemplary embodiment, a biogenic activated carbon product can be utilized. When used as a fuel source and mercury control product, For example, about 70%, about 75%, about 80%, about 85%, about 90%, about 95%, about 96%, Approximately 97%, approximately 98%, 98.5%, approximately 99%, approximately 99.1%, approximately 99.2%, approximately 99.3 %, approx. 99.4%, approx. 99.5%, approx. 99.6%, approx. 99.7%, approx. 99.8%, approx. 99 .9%, or approximately 99.9% or more, from being emitted by the powerplant.

[0685] In an exemplary embodiment, the biogenic activated carbon may be used in a filter such as an electrostatic precipitator or a woven fabric filter. It can be injected (e.g., into a pipe) upstream of a particulate matter control device. In some cases, flue gas desulfurization The system (dry or wet) can be downstream of the activated carbon injection point. The activated carbon is The injection location is typically within the current plant layout (not the new location). If so, this will determine whether further downstream particu...

Claims

1. 1. A biogenic activated carbon composition, the composition comprising, on a dry basis: at least 90% by weight fixed carbon; Maximum 8% by weight of volatile substances; up to 2 wt. % hydrogen, including hydrogen contained in said volatile materials; a maximum of 0.3 wt. % nitrogen, including nitrogen contained in said volatile materials; maximum 0.1 wt. % sulfur, including sulfur contained in said volatile materials; up to 7.5 wt. % oxygen, including oxygen contained in the volatile materials; and Contains a heat value of at least 15,000 BTU / lb; The biogenic activated carbon composition, wherein the fixed carbon is biogenic carbon derived from biomass rather than from coal.

2. A blended composition comprising biogenic activated carbon and metallurgical coke, The biogenic activated carbon comprises, on a dry basis: at least 90% by weight fixed carbon; Maximum 8% by weight of volatile substances; up to 2 wt. % hydrogen, including hydrogen contained in said volatile materials; a maximum of 0.3 wt. % nitrogen, including nitrogen contained in said volatile materials; maximum 0.1 wt. % sulfur, including sulfur contained in said volatile materials; up to 7.5 wt. % oxygen, including oxygen contained in the volatile materials; and Contains a heat value of at least 15,000 BTU / lb; The blended composition, wherein the fixed carbon is biogenic carbon derived from biomass rather than from coal.

3. 3. The composition of claim 2, wherein the blend composition comprises at least 2% and at most 5% by weight of the biogenic activated carbon.

4. 4. The composition of claim 2 or 3, wherein the blend composition comprises a CRI of up to 26%.

5. The composition of any one of claims 2 to 4, wherein the blend composition comprises at least 62% CSR.

6. The composition of any one of claims 1 to 5, wherein the biogenic activated carbon comprises at least 65% CSR.

7. The composition of any one of claims 2 to 6, wherein the blend composition further comprises a product additive.

8. The composition of any one of claims 1 to 7, wherein the biogenic activated carbon further comprises a product additive.

9. 9. The composition of claim 7 or 8, wherein the product additive is selected from iron chloride, iron bromide, magnesium, manganese, aluminum, nickel, chromium, silicon, magnesium oxide, dolomite, dolomitic lime, fluorite, fluorospar, bentonite, calcium oxide, lime, or combinations thereof.

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