Biogenic activated carbon and methods of making and using the same

Abstract

To provide a process for producing biogenic activated carbon.SOLUTION: A continuous process for producing biogenic activated carbon comprises countercurrently contacting, by mechanical means, a feedstock with a vapor stream comprising an activation agent including water and / or carbon dioxide; removing vapor from the reaction zone; recycling at least some of the separated vapor stream, or a thermally treated form thereof, to an inlet of the reaction zone(s) and / or to the feedstock; and recovering solids from the reaction zone(s) as biogenic activated carbon. Biogenic activated carbon compositions comprise at least 55 wt% carbon, some of which may be present as graphene, and have high surface areas and high iodine numbers. Some embodiments provide biogenic activated carbon that is responsive to a magnetic field. Methods of using the biogenic activated carbon are disclosed.SELECTED DRAWING: Figure 21

Description

[Technical field]

[0001] Claiming priority 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. This application claims the benefit of priority from U.S. Provisional Patent Application No. 61 / 737,514, filed December 14, 2012. No. 6,399,413, 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. , biogenic activated carbon, and uses of biogenic activated carbon, including emissions control. [Background technology]

[0003] Activated carbon was first produced commercially in the early 20th century, initially to decolorize sugars, and later to It was used to remove taste and odor from water. Granular activated carbon was first used for gas masks. was 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 feedstocks, followed by the activation of the pyrolysis solids. Pyrolysis typically requires 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 composition 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 composition comprising 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. The present invention provides a biogenic activated carbon composition having a hydrogen content of about 1% or less by weight and a nitrogen content of about 1% or less by weight. The activated carbon composition is characterized by an iodine value of greater than about 500. At least a portion of the is present in the form of graphene.

[0006] In another embodiment, the present disclosure provides a composition comprising 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. % 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 methacrylate. and the activated carbon composition is characterized by an iodine value of greater than about 500. The composition is responsive to an externally applied magnetic field.

[0007] In another embodiment, the present disclosure provides a composition comprising 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. % 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 having an iodine content greater than about 500. The composition is characterized by a magnetic field having a specific magnetic field strength and is responsive to an externally applied magnetic field.

[0008] In another embodiment, the present disclosure provides a composition comprising 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. The present invention provides a biogenic activated carbon composition having a hydrogen content of about 1% or less by weight and a nitrogen content of about 1% or less by weight. The activated carbon composition is characterized by an iodine value of greater than about 500, and at least one of the carbon Some of them exist in the form of graphene.

[0009] In another embodiment, the present disclosure provides a bioavailable iodine extract 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 cellulose, on a dry basis, has a total carbon content of about 55% by weight or more, hydrogen content of about 15% by weight or less, and % 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 further comprises: (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. (c) removing said feed in one or more indirectly heated reaction zones; The feedstock is separated into a substantially inert gas stream and at least one of water or carbon dioxide. The solids, condensable vapors, and non-condensable vapors are separated by mechanical countercurrent contact with an activator containing the other. (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 version of said separated steam stream; and / or by adding at least a portion of the resulting mixture to said feedstock prior to step (c). (f) recycling the biogenic activated carbon to the gas inlet of said reaction zone(s); and recovering at least a portion of said solids from said reaction zone(s) by means of a catalytic converter.

[0012] In another embodiment, the present disclosure provides a continuous process for producing biogenic activated carbon. The process further comprises: (a) providing a carbon-containing starting feedstock comprising biomass; and (b) optionally drying said carbon-containing feedstock to remove at least a portion 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 activating agent comprising a solid, The generation of 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 gas from an external source to generate a separated vapor stream; a liquid or vapor stream is added 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. The process further comprises: (a) subjecting a carbon-containing starting feed comprising biomass to a continuous process for producing a carbon-containing starting feed comprising: (b) optionally drying said carbon-containing feedstock to produce said carbon-containing feedstock. (c) removing at least a portion of the moisture from the feedstock; and (b) applying one or more indirectly reacting The feedstock is mechanically conveyed through the heated reaction zone to substantially a vapor stream containing an essentially inert gas and at least one of water or carbon dioxide By countercurrently contacting the activated carbon with the activated carbon, a solid, a condensable vapor, and a non-condensable gas are generated. (said condensable vapor and said noncondensable gas enter said vapor stream); (d) said removing at least a portion of said vapor stream from the 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 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, the solid being 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. The process further comprises: (a) subjecting a carbon-containing starting feed comprising biomass to a continuous process for producing a carbon-containing starting feed comprising: (b) optionally drying said carbon-containing feedstock to produce said feedstock. (c) removing at least a portion of the moisture from the feedstock; and In the reaction zone, the feedstock is mechanically conveyed and the feedstock is substantially inert. a vapor stream containing a reactive gas and an activating agent containing at least one of water or carbon dioxide and (iii) contacting the mixture in a countercurrent manner with the mixture to generate a solid, a condensable vapor, and a non-condensable gas (previously referred to as "solid") said condensable vapor and said noncondensable gas enter said vapor stream; (d) said reaction zone; removing at least a portion of said vapor stream from the steam generating region to generate a separated vapor stream; (e) removing at least a portion of the separated vapor stream or a thermally treated form thereof; to said feedstock and / or to the gas of said reaction zone(s) prior to step (c). (f) recycling the solid carbon to the inlet to increase the surface area of ​​the carbon in said solid; and 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, At least a portion of the graphene is present in the form of the biogenic activated carbon composition, 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 affected by an externally applied magnetic field. 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. The present invention provides a method for removing or contaminating a contaminant, the method comprising: (a) removing at least one contaminant from a sample; (b) providing a gas phase exhaust stream comprising an additive and a biogenic active ingredient; and (c) contacting the activated carbon composition with activated carbon particles to generate contaminant adsorbent particles; Separating at least a portion of said contaminant-adsorbed particles from said gas phase exhaust 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 present invention provides a method for treating mercury comprising the steps of: (a) providing a gas phase effluent stream comprising mercury; b) converting the gas phase exhaust stream into an activated carbon composition comprising a biogenic activated carbon composition that contains iron or an iron-containing compound; (c) contacting the mercury-adsorbed carbon particles with the mercury-adsorbed carbon particles; and Separating at least a portion of said mercury-adsorbed carbon particles from said gas phase exhaust 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) producing said carbon. and oxidizing a nitrogen-containing feedstock to produce a gas phase exhaust comprising energy and at least one pollutant. and generating a stream, said biogenic activated carbon composition being capable of detecting at least one contaminant. At least a portion 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 contaminants comprising the steps of: (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 present invention provides a method for treating a sulfur contaminant comprising the steps of: (a) providing a liquid containing sulfur contaminants; and (b) 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 includes: (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 includes: (a) providing a gas-phase effluent stream that includes at least one sulfur contaminant; and (b) mixing 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 that contains one or more contaminants, the method comprising: (a) removing a gas that contains one or more contaminants; (b) providing a gas or liquid stream having a dry content of about 55% or more by weight total carbon, about 15% or less by weight hydrogen, and about 1% or less by weight 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 that contains one or more contaminants, the method comprising: (a) removing a gas that contains one or more contaminants; (b) providing a gas or liquid stream having a dry content of about 55% or more by weight total carbon, about 15% or less by weight hydrogen, and about 1% or less by weight nitrogen; and contacting the activated carbon composition with a biogenic activated carbon composition having an iodine value of at least about 500. At least a portion of the 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 black, the method comprising: (a) removing, on a dry basis, at least about 55% by weight of total carbon black; %, about 15% by weight or less of hydrogen, and about 1% by weight or less of nitrogen. (b) obtaining any of the carbons, at least a portion of which is present in the form of graphene; (c) isolating said graphene from said biogenic activated carbon composition; and The liquid or gas may be in a separated form or as part of the biogenic activated carbon composition described above. 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, from the aforementioned biogenic activated carbon composition; (c) separating the graphene from the adhesive, sealant, coating, paint, ink, 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 transporting electrons or ions, 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 includes, in part, using graphene as described above. [Brief description of the drawings]

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

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

[0028] [Diagram 3] 1 illustrates one embodiment of a zero oxygen continuous supply 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] [Diagram 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 shows an embodiment of a pyrolysis reactor system of the present disclosure, optionally with a dryer and a 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 multiple reactor system of the present disclosure, optionally with a dryer and degasifier, and an inert gas inlet.

[0036] [Figure 11] 1 shows an embodiment of a multiple 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 multiple reactor system of the present disclosure, optionally with a dryer, degasifier, cooler, and inert gas inlet.

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

[0039] [Figure 14] 1 shows a 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 plugs 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 dual-reactor biomass processing unit of the present disclosure for producing biogenic activated carbon.

[0048] [Diagram 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] [Diagram 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] FIG. 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 lower center is a reduced version of Figure 28. The lighter colored areas contain small graphene crystallites.

[0055] [Diagram 30] A transmission electron micrograph of activated carbon with an iodine number of 716. The small dark rectangular object at center left is the graphite fragment of Figures 28 and 29. The lighter areas represent small graphene crystallites.

[0056] [Diagram 31] This is 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 curvilinear segments are graphene crystallites. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0057] The detailed description is provided to enable any person skilled in the art to make and use the disclosure. In this specification, several embodiments, applications, variations, alternatives, and uses of the present disclosure are described. These and other embodiments, features, and advantages are set forth in the following detailed 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.

[0058] As used in this specification and the appended claims, the singular forms "a," "an," and " and "the" include plural referents unless the content clearly indicates 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 the term "common name."

[0059] Unless otherwise indicated, the reaction conditions, stoichiometries, etc. used in the specification and claims are All numbers expressing concentrations of ingredients, etc. are expressly assumed to be preceded by the term "about" in all instances. Therefore, unless otherwise indicated, the following The numerical parameters set forth in the specification and attached claims are approximations and should be understood as including, but not limited to, the following: At a minimum, this may vary depending on the particular analytical technique.

[0060] For this purpose, “biogenic” refers to renewable resources on time scales of months, years, or decades. means any material (whether a feedstock, product, or intermediate) that contains elements such as carbon that can be Non-biological materials may be non-renewable or may last for centuries or May be renewable over geological timescales of thousands, millions, or even longer. It is noted that biogenic materials may include a mixture of biogenic and non-biogenic sources. I want to.

[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 rheological properties of a 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) for use in chemical analysis or physical testing. , typically carbon purity).

[0062] Graphene is a single layer of carbon atoms densely packed into a two-dimensional honeycomb lattice and is different from other Graphene is the basic building block of three-dimensional graphite-like materials. They can be folded into zero-dimensional fullerenes, rolled into one-dimensional nanotubes, or stacked. It can be combined with other materials to form three-dimensional graphite. That is, 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 is a related sp 2 Among its forms, including graphitic allotropes In one embodiment, graphene refers to any of the graphenes 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 planar sheet of bonded carbon atoms one atom thick. In another embodiment, graphene is a carbon-carbon nanotube having a length of about 0.142 nm. Unless the context indicates otherwise, all references to graphene include monolayer and It contains precisely multiple layers of carbon atoms. Also, all references to graphene should be read as "biogenic graphene." should be considered synonymous with "laphene."

[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 compared to that of the 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 is 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 be used interchangeably with In various embodiments, the materials that may be produced by the processes and systems of the present disclosure include The term "carbon content," or any other concentration limit, is used throughout this specification 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 process disclosed may be attributable only to The starting material has a relatively low initial carbon content, but the resulting product is highly enriched in carbon compared to the starting material. (high carbon yield), but nevertheless 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, about 10% or less of the oxygen required to complete combustion, about 5% or less, about 1 %, about 0.5%, about 0.1%, or about 0.01%. In some embodiments, there is less oxygen present 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) from the heat source (ii) heat transfer from the feedstock increases the temperature within the feedstock; (ii) primary pyrolysis at this higher temperature The onset of the reaction releases volatiles and forms char; (iii) heat against 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 may produce tars; (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, and is a function of the pressure profile.

[0067] Pyrolysis can at least partially dehydrate the feedstock. The solution is more than about 50% of the water from the feedstock, more than about 75% of the water, more than about 90% of the water from the feedstock, more than about 95% of the water from the feedstock, more than about 9 ... , or more than 99%.

[0068] As mentioned above, some variations of the present disclosure involve multiple reactors or multiple zones within a single reactor. Optimize carbon yield and product quality by pyrolysis while modifying and modifying feedstocks. and be capable of being designed and operated in a manner that maintains flexibility and adaptability to the requirements of the product. It is premised, at least in part, on discoveries 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 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 walls are mechanically Utilizing equipment that does not break down or otherwise convert biomass particles into smaller particles Various reactor configurations are discussed below after the process description.

[0070] Additionally, the feedstock may be 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. The 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 preserve 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. Measures are taken to provide greater strength to the structure. In some embodiments, the feedstock is heated for an extended period of time, such as 1 hour or more, about 2 hours or more, about 3 hours or more. , approx. 4 hours or more, approx. 5 hours or more, approx. 6 hours or more, approx. 7 hours or more, approx. 8 hours or more, approx. 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 or more, about 15 hours or more, about 16 hours or more, about 17 hours or more, about 18 hours or more, about 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 4 hours and maintaining the feedstock 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 rate of temperature increase 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 / min 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 occurs primarily or entirely in the 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. The temperature rise rate is determined based on the temperature during preheating, prepyrolysis, and / or carbonization or pyrolysis. At least a small amount of carbonization or pyrolysis is performed during at least a portion of the thermal, prepyrolysis, 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 the present invention, prior to pyrolysis, the dried feedstock is subjected to a process to crush the wood and reduce its strength. It is more accurate in determining 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 an embodiment, 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 substantially uniform in shape; For example and without limitation, biomass can be processed to produce pellets of substantially uniform particle size (e.g., mesh size). Alternatively, biomass can be processed to produce sawdust of substantially Chips having uniform dimensions (e.g., about 1 inch by about 1 / 2 inch by about 1 / 8 inch cross section) In another embodiment, the feedstock can be milled from biomass to produce a pulp. and preparing a length of material having substantially uniform width and depth dimensions or diameters. (e.g., a wooden stick, a wooden board, or a wooden dowel). , by 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 by 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. A bioreactor prepared from a feedstock consisting of fragments of substantially uniform shape and size. The original activated carbon product is made 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 be a separate reactor or, alternatively, within a single reactor, the BPU may contain multiple zones. These figures each show different alternative embodiments. However, all other considerations in this disclosure are to be construed as being in accordance with the illustrated embodiment and the illustrated It should be understood that the above-mentioned teachings may be applied to each of the embodiments described above.

[0074] Referring now generally to FIG. 1, a block flow diagram of a multi-reactor embodiment of the present disclosure is illustrated. This embodiment may utilize two or more different reactors. Three reactors are shown. Although shown in the solution embodiment, any different number of reactors may be used. In each reactor, at least one material is transported 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, a raw material 109, such as biomass, is optionally dried and The dimensions are determined outside the system and the material is then optionally fed into the feed system 108 in a low oxygen atmosphere. The mixture is introduced into a reactor 100 at 100° C. As will be 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 at about 3% or less. The raw material 109 is sealed 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 material is transported. The steam and off-gas from the reactor are then sent directly to preheat the biomass. or sent to a process gas heater and / or heat exchanger before The gas is either sent to and used for preheating or pyrolysis of gas.

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

[0077] As will be discussed in more detail below, in one embodiment, the first reactor 112 is 132 and is adapted to be connected to any other reactor in the system to recover waste heat 132 and Energy is stored via a waste heat recovery system. In one embodiment, the first reactor 1 The waste heat released in the drying system 12 is used to dry the raw material 109 either in-system or outside the system. Activating a steam bin or another suitable heating mechanism configured to heat the mixture. In the process, other by-products of the waste heat, such as substantially heated inert gas, are pumped 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 range 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 below, 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 off-gas 120 from the exhaust gas 123. In the embodiment, the off-gas 120 is extracted for optional later use. Thus, the heating sources used for the various zones within BPU 102 can be electric or gas. In some configurations, the heat sources used for the various reactors of the BPU 102 are different from those of the other units 102. In various embodiments, the heat is indirect. do.

[0079] After preheating the first reactor 112, the material transport unit 304 transports the preheated material 123 through The reaction mixture is filtered into 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 then transports the material through a high temperature steam containment system (e.g., an airlock). 2 reactor 114, which prevents gas from escaping and at the same time 04 through the second reactor. 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 gas 122 released from the material 123. In one embodiment, the gas 122 is discharged to a In one illustrated embodiment, the off-gas 120 from the first reactor 112 is extracted for 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 again is a 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 biomass126 does not spontaneously combust when exposed to oxygenated air, It should be understood that cooling may also be performed within the third reactor 116. In one such embodiment, The third reactor 116 then reduces the temperature of the carbonized biomass to less than 200° C. In an embodiment, the third reactor is a reactor for stirring and uniformly cooling the carbonized biomass. Cooling may be provided by direct or indirect means using water or other liquids. Cooling can occur by air or other cooled gases either directly or indirectly. 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 the above-mentioned structure can 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, water or other liquid, either directly or It may be cooled either directly or indirectly by other gases, or it may be cooled either directly or indirectly by other gases. or a combination of the above, such as a screw, an auger, a conveyor (specifically, in one embodiment, (conveyor belt), drum, screen, pan, countercurrent bed, vertical tower, jacket In various embodiments, the cooling device may be a paddle with a cooling screw, a cooling screw, or a combination thereof. Cooling may be by water spray, a stream of cooled inert gas, liquid nitrogen, or ambient air (if below ignition temperature). It may include a water spray to capture flash steam or to introduce 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 a first reactor 1 and a plurality of outputs. At least one input is connected to the first reactor 1 of the BPU 102. 12 and the exhaust port of the second reactor 114. One of the multiple outputs is a carbon capture unit 104, and another of the multiple 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 one embodiment, the gas phase separator separates the ozone 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 certain embodiments, the condensables are used for energy recovery (134) (e.g., a dryer, a reactor, in gas turbines or process gas heaters) or other carbon enrichment. In various embodiments, the non-condensables (e.g., CO) can be used for energy recovery ( 34) (e.g., in dryers, reactors, or process gas heaters) As an inert gas in processes (e.g., degassing units, reactors, BPUs, or In the cooler discussed in more detail below), or for carbon enrichment.

[0083] In various embodiments, the condensate 128 may be a mixture of acetic acid, methanol, furfural, etc. In another embodiment, the concentrated volatile organic compound produced by the gas-phase separator 200 includes 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 the distillation / treatment unit 138.

[0084] In various embodiments, as discussed in more detail below, the carbon capture 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 in which 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, as illustrated in more detail in FIG. , 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 capture unit. The final high-carbon biomass produced was then directed toward the charcoal-derived biomass126. In various embodiments, the activated carbon product is added with additional carbon. 126 is the carbonized biomass with reduced temperature. The carbon-enriched gas from the timber processing facility may be installed near the facility, as well as gas from an external source. It can be used in the following manner.

[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 raw material is then introduced into the reactor 200 under a low oxygen atmosphere using the material supply system 108 described above. As will be discussed in more detail below, the material supply system 108 may be configured to The oxygen level in the surrounding air is reduced to about 3% or less. The raw material 209 is After that, it 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 biomass. do.

[0087] In the illustrated embodiment, the raw materials are first transported to a material supply on a material transport unit 304. From the system 108, the BPU 202 moves to an optional drying zone 210. In one embodiment, An optional drying zone 210 heats the raw material to remove water and other impurities before it is passed 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 200° C. The water 238 or other The moisture may be removed, for example, from optional drying zone 210. In another embodiment, the moisture may be removed from optional drying zone 210. The drying zone is adapted to extract steam and vapor. The steam and vapor from the optional drying zone may be extracted for any subsequent use. As shown, the steam or vapor extracted from any drying zone may be fed through the material feed system. In one embodiment, the material feed system may be used in a suitable waste heat recovery system having 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 will be discussed in more detail below, in one embodiment, the optional drying zone 210 comprises: 2. The cooling zone 216 is adapted to recover waste heat 232 and to implement a suitable waste heat recovery system. In one embodiment, the energy released in the cooling zone 216 is stored via the and configured to dry raw material 209 in an optional drying zone 210 using the waste heat generated by the drying process. The heating mechanism is turned on. After drying for the desired time, the dried biomass 221 is It exits the drying zone 210 and enters the preheat zone 212 .

[0089] In the illustrated embodiment, dried biomass 221 is introduced into the first (preheating) zone 21. 2, where the temperature is changed from a range of about ambient temperature to about 150° C. to a range of 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, dry biscuits may be It should be understood that the mass 221 may be misprocessed before entering the second band 214. As will be discussed in more detail below, the preheat zone 212 simultaneously preheats and dries the vapor. An output mechanism for capturing and discharging off-gas 220 from the biomass 221 may be included. In some embodiments, the off-gas 220 is extracted for any subsequent use. In an embodiment, the heat sources used for the various zones within the BPU 202 are electric or gas. In one embodiment, the heat sources used for the various zones of the BPU 202 are units 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 is Passing through the second / pyrolysis zone via a steam containment 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, the gas 222 is In one illustrated embodiment, the off-gas 220 from the preheat 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 The temperature is reduced or cooled in zone 216 .

[0091] In one embodiment, as the carbonized biomass 225 enters the cooling zone 216, the carbonized biomass The mass 225 is cooled to a prescribed temperature range of about 20° C. to 25° C. (about room temperature) as described above. The BPU 20 is then cooled to produce a carbonized biomass 226 having a reduced temperature. 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 in a single stream. One or more of these 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 includes: At the discharge ports of the first / preheat 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). One of the multiple outputs is connected to a collection device or an oxyhydrogen 206 or further processing equipment such as a distillation column. In the present invention, the gas phase separator is a gas phase separator for separating the first / preheating zone 212 and the second / pyrolysis zone 214 from the The off-gases 220 , 222 are processed to produce a condensate 228 and a concentrated gas 204 . In one embodiment, the condensate 228 comprises polar amines such as acetic acid, methanol, and furfural. In one embodiment, the enriched gas 2 produced by the gas phase separator 200 includes 04 includes at least a non-polar gas. In one embodiment, the gas phase separator comprises a fractionation column. In one embodiment, acetic acid is delivered to optional acid hydrogenation unit 2 via line 228. In another embodiment, the methanol and / or furfural are optionally via optional further line(s) 236 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. As illustrated in more detail in and discussed above, the carbon capture unit 500 is a gas-phase The separator 200 also includes an input 524. 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, the activated carbon from an external source is added to produce a raw biogenic activated carbon product 136. The concentrated 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 withdrawn from the carbon recovery unit 500 at reference 234 is then fed to an energy recovery system and / or optionally 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 timber 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. and 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 reduce oxygen levels. to about 3% or less, about 2% or less, about 1% or less, or about 0.5% or less. 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 the inert gas that has been preheated and then pumping 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. to a further reactor where heated inert gas is introduced to obtain 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 is extracted from the BPU. The gas is heated through a heat exchanger which extracts heat from the gas that is discharged and combusted in the process gas heater. I feel heated.

[0096] As seen in FIG. 3, the closed material supply system 108 includes a raw material supply hopper 3 00, a material transport unit 304, and an 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 dried / cooked biomass 109 / 209. The raw material supply hopper 300 is a discharge vessel or an air-closed vessel. 4, which in one embodiment is a screw that is operatively 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 fed by a feeding system. 4 is made such 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 an embodiment, the material delivery system may be a screw, an auger, a conveyor, a drum, a screen, or the like. chute, drop chamber, air conveying device (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 purging 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 adjacent 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 The oxygen purge manifold 30 has one gas outlet line 314. In various embodiments, the oxygen purge manifold 30 has one gas outlet line 314. At least one gas inlet line 312 of the second gas inlet port 310a, 310b, b, 310c. Similarly, in various embodiments, At least one gas outlet line 314 of the oxygen purge manifold 302 includes a plurality of gas outlet ports. In one embodiment, the casing 308 is in operative communication with each of the ports 308a, 308b, and 308c. In the gas inlet port 310a, 310b, 311b, 312, the gas inlet line 312 supplies the inert gas to the gas inlet ports 310a, 310b, 311b, 311c, 311d, 311e, 311f, 311g, 311h, 311i, 311j ... It should be understood that the device is configured to pump 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 During operation, the inert gas 312 is pumped through one embodiment of the system. 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%; about 1% or less; Desired levels of 0.5% oxygen or less, or about 0.2% oxygen or less are not achieved It should be understood that in some cases, the encapsulated system may be In order to purge the necessary amount of oxygen from the air surrounding the raw material 109 in the system, an inert gas 3 An additional injection of 12 should be performed. In one embodiment, the 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 drawing more of the remaining oxygen from the sealed 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 injects of inert gas, the gas injector A third injection of inert gas 312 at port 310c is then introduced into the enclosed system at gas outlet 308c. 3. Purge remaining undesirable amounts of oxygen 314 from the chamber. If desired, further inlet / outlet In various embodiments, the oxygen level is controlled throughout the material delivery system. The inert gas injection is monitored throughout to allow for calibration of the amount and location of the inert gas injection.

[0101] In an alternative embodiment, the heat, steam, and gas recovered from the reactor are fed back to the feed system. The feedstock is then directed into the feed tube where they are enclosed within a jacket to isolate them 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 The feed system is directed into the feed system where they are enclosed in a jacket and in direct contact with the feed material. The catalyst is separated from the feedstock, but the feedstock 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 a vertical arrangement through the material transport unit 304. It should be understood that the halves are slightly offset from one another relative to the halves of the plane. 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 roughly 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 the 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). Thus, the material transport units that carry this material are different at different stages of the process. In the present invention, 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 304. The material transport unit 304 may be configured to move through the are appropriately calibrated and calculated by the controller and processor associated with

[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 sensed gas (e.g. , any FTIR derived), measured parameters, thermometers, or reactor processes 3. The speed of the material transport unit 304 may be adjusted based on other suitable variations. In various embodiments, any suitable water supply in operative communication with the controller and processor. A chemical sensor, a temperature sensor or a gas sensor is installed in the zone / reactor or in each zone / reactor. It can be integrated at any suitable location between the reactors or along the material transport unit 304. In one embodiment, the controller and processor may receive the following from the sensor or gauge: This information is used to optimize the speed and efficiency of the BPU 100 / 200. In the embodiment, 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 the reactor 102 or multiple reactors (112 / 114 / 116) , the concentration of gas within 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 speed, gas input to the material transport unit, and material in the material transport unit The device is 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 U202 corresponds substantially to BPU202 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. As can be seen in FIG. 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 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 exhausted air may 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 It is 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 BPU 202 then introduces the raw material 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 includes a drying zone 420a. The biomass is then heated to remove water or other moisture from the raw material 209. zone or preheat 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℃, about 270℃, about 280℃, about 290℃, about 300℃, about 310℃, about 320℃, about 330℃, about 340℃, about 350℃, about 360℃, about 370℃, about 380℃, about 390℃ , about 400°C, 410°C, about 420°C, about 430°C, about 440°C, about 450°C, about 460°C ℃, about 470℃, about 480℃, about 490℃, about 500℃, about 510℃, about 520℃, about 5 30°C, about 540°C, about 550°C, about 560°C, about 570°C, about 580°C, about 590°C, About 600℃, about 610℃, about 620℃, about 630℃, about 640℃, about 650℃, about 660℃ ℃, about 670 ℃, about 680 ℃, about 690 ℃, or about 700 ℃. In this configuration, the carbonization zone of the reactor 421 is adapted to extract the gases produced during carbonization. In another embodiment, the gas generated during carbonization is optionally In one embodiment, the carbonization temperature is 100° C. Minimize or eliminate carbon dioxide production and maximize the carbon content of carbonized biomass. It is selected so that

[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 be actively cooled. In the form, the carbonized biomass solids are heated to a temperature of room temperature ±10, 20, 30, or 40°C. The mixture is cooled to .

[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, as well as a plurality of gas extraction probes 400, In various embodiments, each of the gas introduction One of the inlet probes and one of each of the gas extraction probes 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 inlet probes and two or more gas extraction probes may be used. It should also be understood that the term "gas introduction probe" 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 for use in a heat or energy recovery system. It should be understood that the ion exchange resin is reused in the stem.

[0112] In the illustrated embodiment, the preheat zone 212 includes a gas inlet 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 preheat zone 212, and the gas extraction probe 400 extracts the gas from the preheat 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 includes carbon-enriched off-gas. As described above, the gases extracted from the preheat zone 212 and pyrolysis zone 214 may be, for example, It should be understood that the carbon dioxide emitted is then reintroduced into the material later in the process in a carbon recovery unit. In one embodiment, the gas extracted from any of the reactor zones is trimmed. Energy recovery in a dryer or process gas heater for further pyrolysis in the reactor The wastewater is either used for biogas harvesting or 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 a gas extraction probe 404. The nitrogen is introduced into the pyrolysis zone 214, and the gas extraction probe 404 is connected to 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 introduced into the gas supply passage 4. Thus, the gas extracted by the gas extraction probe 404 includes carbon-enriched off-gas. In the process, the carbon enriched gas extracted from the pyrolysis zone 214 is used as described above. 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 preheat 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 an 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 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 the gas extraction probe of the various embodiments described above are and a plurality of sensors to measure the gases introduced into each zone and the respective It will be 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 the 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 spaced apart within each zone. It extends over a long distance.

[0117] In one embodiment, the gas introduction probes are arranged to guide the gas through each of the zones to one of the BPUs 202. In one such embodiment, the four gas introduction probes each extend from one side of the , extending from one side of the BPU to each respective zone. A gaseous catalyst is added to enrich the oxygen levels. A plurality of openings for each of the gas introduction probes are associated with that particular gas introduction probe. It should be understood that the 1000 MHz to 1000 MHz bands may only be placed within each of the bands designated.

[0118] For example, referring to FIG. 4, the gas introduction probes are arranged in a direction from the left of the drying zone to the Each of the four gas introduction probes extends into one of the four zones, and all four gas introduction probes move through the drying zone. 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 inlet probe terminates within the preheat zone. The remaining two gas introduction probes move through the pyrolysis zone and are The probe terminates in the pyrolysis zone. The cooling zone gas inlet 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 constructed 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 examples above. In order to save space, the assemblies 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 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 positioned 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, the preferred connector is four gas leads external to the BPU 102. Each of the four gas inlet probes is fitted with a gas injection probe. The air entering each room is individually controlled.

[0120] In one such embodiment, similar to the example above, the dry zone gas introduction probe is 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 Each of the zones is exposed before being bonded. The individual zone gas introductions are effectively controlled independently of each other while being controlled as one continuous gas introduction. Only the gas introduction probe line is required. It should be appreciated that the configuration of FIG. 1 is preferably used in a gas extraction probe in one embodiment.

[0121] In one embodiment, each zone or reactor is an individual zone or reactor. In another embodiment, the apparatus is adapted to extract and collect off-gas from one or more of the The off-gas from each zone / reactor is then stored for disposal, analysis, and / or later use. In various embodiments, each reactor / zone is separated from the other. It 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 discarded, analyzed, and / or or for later use, and in various embodiments, from one or more zones / reactors. The off-gas from the process gas heater is fed 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 of the 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 tower 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 concentrated gas from the gas phase separator may be optionally 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, the 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 separated into a gas-phase separator. One or more of these determines whether and how much gas is introduced into the combined stream. The device is configured to control how much of the mixed 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. Gas 124 / 224 is gas extracted from the second / pyrolysis zone / reactor 114 / 214. 122 / 222 or the first / preheating zone / reactor 1 coupled with only any gas flow 12 / 212. The off-gas 124 / 224 is a gas phase separator. At 200, off-gas 124 / 224 is polar compounds 128 / 228 / 136 / 23 6 and non-polar compounds 204, such as non-polar gases. The 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 fed into the carbon capture 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 should be understood to be introduced into a separate carbon capture unit. In the present embodiment, material enrichment occurs in a carbon recovery unit 500. In various embodiments, the gas-phase separator 200 includes multiple outputs. 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 of the mixture is directed to a scrubber 500 and another portion is directed to a scrubber or other suitable purification device, as desired. In various embodiments, the undesirable gas is sent to a carbon recovery unit and then purified and discarded. The off-gas that is not exhausted 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 capture unit may be used in Off-gas from the , as an inert gas (e.g., in degassing units, reactors, BPUs, or coolers) ), 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 reused. For example, in one embodiment, the output water is reused 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 are regenerated. It should also be understood that the water may be sent to storage tanks for utilization, resale, distillation, or purification.

[0125] As seen in FIG. 5, one embodiment of a 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, In the present invention, the material concentration 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 first portion 502a and a second portion 502b, configured to carry reactor off-gas. The inlet 524 is located at the bottom of the lower portion of the 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, the housing comprising: 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 objects with their bases attached to each other. cone, two regular tetrahedrons attached at their bases, and two rectangular pyramids attached at their bases , or shaped substantially like two isosceles triangular prisms attached at their bases.

[0127] In one embodiment, the upper portion 502a and the lower portion 502b of the housing 502 are semi-ellipsoidal, semi-elliptical, Rectangular prism, semi-ellipsoid, semi-spheroid, cone, regular tetrahedron, rectangular pyramid, isosceles triangle The duct transitions are made from rectangular prisms and circular to rectangular ducts. 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 02a 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 is substantially rectangular, circular, or elliptical. The width between the top of the housing 502a and the bottom of the upper part 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 inlet opening 506, and an outlet opening 508. In one embodiment, the inlet opening The portion and the exit opening are configured to receive the 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 10 mm to reduce gas leakage. The outlet opening 508 includes an outlet opening sealer 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 capture unit housing has a narrow circular bottom. It has 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 portion 502b of the housing of the carbon recovery unit 500 is , substantially rectangular and substantially wider than the width of the narrow circular bottom connection opening. In this embodiment, the lower portion 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 mouth is wider than the top opening of the lower portion. The width of the opening is approximately 6.5 feet (along the direction of the conveyor system). In this embodiment, the upper portion passes through the carbon capture unit 500 that is not adsorbed by the activated material. The gas trap is configured to capture any gas passing through the trap.

[0132] In various embodiments, the configuration of the lower portion of the carbon recovery unit is such that the biogenic activated carbon product 126 / 226 to retard and disperse the gas 204 over a larger surface area of ​​the conveyor. It should be understood that the present invention is directed to providing a carbon capture unit 500 having a lower portion. The exact shape of 502b and upper portion 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 when injected, the catheter naturally tends to expand. 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 creases 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 the BPU 102 / 2 02 or external to the BPU. The output of the reactor / band 116 / 216 is the active material of biogenic substances processed by BPU102 / 202. In one embodiment, the biogenic activated carbon product 126 / 226 is preferably In various embodiments, 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 must be properly sealed with airlocks or another suitable sealing mechanism. The conveyor opening is sealed to prevent gas from escaping 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 cooler. ,Offgas from the carbon capture 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 The refrigerant may be used either in a centralized recovery unit (usually in a chiller) or in a secondary recovery unit.

[0134] In various embodiments, the process includes cooling reactor / zone 116 / 216. First, the biogenic activated carbon product 126 / 226 was cooled in the cooling zone 116 / 21 using a discharge mechanism. 6 to the transport system. The activated carbon product 126 / 216 is spread across the width of the conveying system to prevent material from being stacked or It minimizes focusing and maximizes surface area for gas absorption. Once the composition 126 / 216 has been deposited and properly spread into the delivery system, various embodiments In the above, the transport system is defined between the lower part and the uppermost part of the carbon capture unit 1. Transport the biogenic activated carbon product 126 / 216 through the opening in the 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. The biogenic activated carbon product is enriched with non-polar gases, and then 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 charcoal product is the end product of the process disclosed herein and is treated in a 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 fed to 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 system. may be utilized in any reusable capacity in the system, including for 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 capture unit may be used in either the 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 amounts of carbon, which is then converted to non-polar gases. It should be appreciated that the enriched gas stream 204 strongly favors the adsorption of terpenes, carbon monoxide, It should also be understood that this includes primarily non-polar gases such as carbon dioxide and methane. In the embodiment, when the concentrated gas is directed from the gas phase separator to the carbon recovery unit, the gas flow The amount 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 compounds are dissolved during carbonization of the biomass and are then extracted from the gas phase separator 200 to a carbon recovery unit. 104。 In various embodiments, the enriched gas 204 is at least a portion of the enriched gas 204. The enriched gas 204 may be further processed before being introduced into a carbon recovery unit or a 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 some cases, the biogenic activated carbon product is passed two or more times through one or more carbon capture 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 split 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. Various embodiments and alternatives discussed below with respect to FIGS. 6-13 are illustrative of the implementation of FIGS. 1-5 above. It should be understood that this 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. However, 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 atmosphere and temperature conditions.

[0140] In one embodiment specifically illustrated in FIG. 6, the system 600 includes a material delivery system. 602, a BPU 606 including a pyrolysis zone 608 and a cooling zone 610, a 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. 6, the BPU 606 includes a pyrolysis zone 608 and a cooling zone 610. The BPU 606 is configured to transport a material, including at least condensable vapors and non-condensable gases 612, through 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 FIG. 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, and a cooler 71. 4, and a carbon recovery unit 716. In the system 700, an optional feed system 702 and a preheater 706 are provided. 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 of the output 712 is The material includes 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 an embodiment, the system 700 includes 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 820. 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 06 is removed during the drying process. FIG. and an optional chiller 816 prior to the material concentration unit 818. As shown, the material enrichment unit 818 is in communication with the gas outlet 814 of the BPU 808. , 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 discussed 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 the carbon recovery unit 820 does not further concentrate the material.

[0144] In various embodiments, an optional process gas heater 824 is disposed in the system. , it should be understood that the BPU 808 may be attached to the BPU 808. Steam or other off-gas from 808 may be any of the following: 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 the zones 904, 910, 914; In various embodiments, the at least one gas inlet 906 is in communication with the As shown, 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 one embodiment, one of the zones may be an outlet for outputting enhanced carbon from the system 900. Also includes.

[0146] Although FIG. 9 shows a gas inlet 906 connected to a preheat zone 904, various embodiments may It should be understood that the term "gas inlet" includes any combination of these three zones. Although the outlet 912 originates from the pyrolysis zone 910, various embodiments may be used in 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., The outlet of the solution zone 910 is then the input to the preheat zone 904. In the BPU, the reactors 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 “shocks” the biomass. 9. 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 steam and gas. In an embodiment, the preheat zone 904 may be considered a soft 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 a function 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, the chemical reactions and mass transport are complex. In various embodiments, secondary reactions occur in the cooling zone 914. The carbon-containing components that are present may decompose to form additional fixed carbon and / or may adsorb carbon. It should be understood that the advanced carbon 916 may therefore be simply a processing step. Rather than being a solid devolatilized residue of the top, organic vapors that can form carbon (e.g., This includes additional carbon deposited from the gas phase, such as by the decomposition of 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 10, and a carbon recovery unit 1022. As discussed further below, the 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 embodiment, the carbon recovery unit 1022 is an output unit for outputting activated carbon from the system 1000. Includes mouth 1024.

[0151] In at least the various embodiments illustrated in FIGS. 10-13, the illustrated system It should be understood that this includes an optional deaerator and an optional dryer. As seen in FIG. For example, as represented by the dashed line, an optional deaerator 1004 may be connected to the material feed system 1002. The pyrolysis reactor 1002 is connected to the system 1000. Similarly, the dryer 1006 is connected to the system 1000 between the material supply system 1002 and the pyrolysis reactor 1012. In various embodiments, the material from the material supply system is It can flow in 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 the method, 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 disclosed. 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; A removing step;

[0154] (c) Optionally degas the feedstock to remove any granules, if any, contained within the feedstock. removing at least a portion of the interatomic oxygen;

[0155] (d) subjecting the feedstock to a temperature of about 250° C. to about 700° C. in the presence of a substantially inert gas phase; Pyrolyze for at least 10 minutes at at least one temperature selected from the following: hot pyrolysis solids, condensation 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 noncondensable gases from the hot pyrolysis solids; and isolating 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 multiple reactor system 1100 is illustrated. Similar to the embodiment discussed and illustrated in FIG. 10, this embodiment uses a material supply system. The pyrolysis reactor 1102, the pyrolysis reactor 1112, the cooling reactor 1118, and the carbon recovery unit 11 24. In the illustrated embodiment of FIG. 11, the cooler 1120 is optional and The concentrating unit 1122 is disposed 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 concentrated or not. It should be understood that in various embodiments, the optional deaerator 1104 and the optional dryer 1106 may be used. The vessel 1106 is disposed between the material supply system 1102 and the pyrolysis reactor 1112 . In the illustrated embodiment, the pyrolysis reactor 1112 is a reactor for the pyrolysis of condensable vapors and non-condensable gases. and sending the removed material to a material enrichment unit 1122. Also includes exit 1114.

[0160] Various embodiments provide for subjecting cooled carbon containing carbon-containing species to an environment to produce a final product. By including a separate material enrichment unit 818, 1122 that enriches the carbon content of , expanding the concept of further carbon formation. If the temperature of this unit is below the pyrolysis temperature It is expected that the additional carbon will be 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 feed and separation conditions. Zone or reactor specific input and output flows are used for FTIR sampling and dynamic probing. Allows for better process monitoring and control through process adjustments etc.

[0162] The present disclosure is different from fast pyrolysis and different from conventional slow pyrolysis. The high quality carbon materials of the present disclosure, including compositions having the following properties, can be used in the processes and systems of the present disclosure. can be obtained from

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

[0164] Biomass includes, for example, plants and plant-derived materials, vegetation, agricultural waste, forestry waste, 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, silver grass, 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, plastics The feedstock may include one or more materials selected from the group consisting of woven fabric, woven fabric, and textile 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). Any mixture of carbon-containing feedstocks, not biomass, or biomass and fossil fuels (e.g. 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, petroleum coke, etc. The materials may include 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 transported by 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 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 shape of the material in large pieces such as chips, or other shapes of wood (e.g. round, cylindrical, square, etc.) In some embodiments, the feed materials may be held together, such as with a binder. pellets or other aggregate 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., from the product rather than the feedstock. By reducing the particle size, the process can become more energy efficient. 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. In particular, in some embodiments, large fragments are supplied, produced, and sold. As discussed above, some commercial applications of activated carbon products are based on actually large dimensions (e.g., on the order of 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 sized activated carbon products and / or 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 biogenic carbonaceous activated carbon product 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 objective 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 the strength of the product. This control also avoids the pelletizing problems of 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 so that Further drying prior to pyrolysis is not necessary. Typically, biomass that normally contains moisture is Biomass is extracted from commercial sources and passes through a drying step prior to introduction into the pyrolysis reactor. However, in some embodiments, it may be desirable to provide a dry supply. A feedstock is used. In various embodiments, any biomass works well, but the material how it was grown, harvested, irrigated, the choice of material species, 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 growth, Metal construction 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 in the final product. It should be appreciated that this results in more fixed carbon.

[0173] A relatively low oxygen environment (e.g., about 10%, 5%, 3%, or It is advisable to provide 1% O2 at the earliest possible time. First, uncontrolled combustion is a safety hazard. 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 benzene, 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 some embodiments In the step (a), the reactor(s) or the BPU is substantially free of molecular oxygen in the gas phase. Ensure that there is little or no oxygen in the reactor(s) or BPU. To remove air 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 is 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 with small amounts of oxygen can be used. Steam may be present in the degassed gas, but adding significant amounts of moisture back to 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 either recovered or recycled.

[0176] In principle, the effluent from the degassing unit (or a part of it) 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 fed to 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 the soluble oxygen from any moisture present. In certain embodiments, the drying and degassing steps are performed in a single unit. Combined 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, The feedstock may be fed using any known means, including a screw material feed system or a 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 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 (such as in FIG. 6, 8, or 9). ), physically separate units (e.g., those in Figures 7 and 10-13), or The BPU should be broadly interpreted to include spatial domains in any combination. The distinction of zones within the BPU is based on the structure, e.g., the presence of flights within the BPU or the ability to separate heat Alternatively or additionally, the heating elements may be associated with distinct heating elements for providing heating to the zones. In various embodiments, the distinction between zones within the BPU is at least one distinct temperature It is related to functions such as fluid flow patterns, solid flow patterns, and extent 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 preheat zone and the pyrolysis zone is somewhat arbitrary and may include a certain amount of heat. The decomposition may occur in part in the preheat zone, and a certain amount of "preheat" 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 include preheating and / or gentle heating, as seen, for example, in FIG. A preheat zone 304 operating under pyrolysis conditions is used. In various embodiments, the preheat zone 3 The temperature of the step 04 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 gas. The temperature is not high enough to shock the biomass material to initiate rapid decomposition of the solid phase of the biomass. or 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. Temperature that may be applied to the body, or gas phase, or reactor or BPU wall (process side) In each zone, the temperature gradient is in both the axial and radial directions. It is understood that the function exists both in time and in time (i.e., upon activation or transiently) Therefore, references to zone temperatures are to average temperatures that may affect actual dynamics. or other effective temperature. The temperature may be measured by a thermocouple or other temperature probe. The amount of the active ingredient may be measured directly by the enzyme 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 or 650°C. The extracted biomass undergoes pyrolysis chemical reactions that release gases and condensable vapors, resulting in high carbon reactions. Leaves a significant amount of solid material as an intermediate. Biomass components (mainly cellulose, hemicellulose, etc.) The cellulose, cellulose, and lignin penetrate the pores or create new pores. The temperature should be at least as long as the residence time in the pyrolysis zone and It depends on the identity of the feedstock and the product properties.

[0185] The cooling zones operate to cool the high carbon reaction intermediates to various 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 is sufficiently Reactions that may remain elevated and 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). It is.

[0187] The residence time in the zones can vary. For the desired amount of pyrolysis, higher temperatures are recommended for the duration of the reaction. 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 this context In each zone, the residence times (and residence time distributions) of both the solid and vapor phases are 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 the vapor residence time are decoupled.

[0189] The residence time of the solids in the preheat zone depends on the temperature and the time required to reach the preheat temperature. Depending on the circumstances, the time period may 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 the This dictates the minimum residence time required to achieve

[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 may be selected from 100 to 120 minutes. There should be sufficient time for the carbonization chemical reaction to occur. For times less than about 10 minutes In order to remove a large amount of non-carbon elements, the temperature is very high, e.g., above 700°C. This temperature is required to produce the vapors and gases that come from fast pyrolysis and the carbon itself. It promotes gas evolution, but should be avoided if the product of interest is solid carbon. be.

[0191] In the static systems of various embodiments, an equilibrium transformation is reached at a certain point in time. In one embodiment, the vapor is continuously passed over the solids while continuously removing the volatiles. As it flows, 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 times of the vapor phases can be separately selected and controlled. 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 may be any combination or variation of the above. 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 discharging the gas from a batch vessel. This involves simulated countercurrent flow of vapor by removing a 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, as it involves multiple phases within the fluid. Typically, solids flow 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 independent and ranges from about 1 kPa to about 3000 kPa, such as about 101.3 kPa (standard atmospheric pressure). A true gas extractor for withdrawing 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 The inputs 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 compactness to improved safety. In an embodiment, the pyrolysis zone is at about 90 kPa, 95 kPa, 100 kPa, 101 kPa a, 102 kPa, 105 kPa, or 110 kPa pressure (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 higher pressure (e.g. 100-1000 kPa) can be useful. Elevated pressure can also promote 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 above can be carried out within the reactor itself or using a distinct separation unit. 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 heating source, may possibly be 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. The sweep gas is simply a given The ability to remove volatiles at a rate greater 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 more moderate temperature. The reason that the sweep gas improves volatile removal is that Liquid / vapor phase solution in which 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 limitation of volatilization, but also reduces the thermodynamic limitation, making it more efficient. Many volatile species can be vaporized to achieve thermodynamic equilibrium.

[0202] To produce a product with high fixed carbon, volatile organic carbon is removed from subsequent processing steps. It is important to remove the charged gas. Without removal, the volatile carbon will dissolve into 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 obtain the desired state. It is also speculated that the porosity of the pyrolysis solids is increased by the addition of activated carbon. In embodiments, higher porosity is desirable.

[0203] In one particular embodiment, the sweep gas is provided at 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 countercurrent 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 patterns generally approach perfectly 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 preheat zone. In these or other embodiments, the sweep gas is introduced into the preheat zone and extracted from the pyrolysis zone. In an embodiment, a sweep gas is introduced into each of the preheating zone, the pyrolysis zone, and the 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 located between the pyrolysis zone and the cooling zone.

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

[0208] The volatiles-containing sweep gas may exit from one or more zones and may be combined if obtained from multiple zones. 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 provided to control air 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 to cause 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 is also recovered by heat exchange with another stream (e.g. sweep gas). The energy content can be calculated by dividing the energy content by the units elsewhere in the process, such as dryers or reactors. It can be utilized by directly or indirectly providing or assisting in the heating of 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 Instead, other fuels may be used.

[0210] The yield of carbonaceous materials will vary 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 the additive prior to the pyrolysis step depends on the process conditions. The same process is used 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: (i) not adding any time, or (ii) After pyrolysis, but added by an otherwise identical process, biogenic activated carbon 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 For example, in some embodiments, the carbonaceous material may be a starting Contains about 40% to about 70% of the carbon contained in the feedstock. The remaining carbon is made up of various In terms of degree, methane, carbon monoxide, carbon dioxide, light hydrocarbons, aromatics, tar, terpenes, This results in the formation of alcohols, acids, aldehydes, or ketones.

[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 The cooled water is then partially condensed and the resulting cooled water 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 solids are collected and simply cooled at a slow rate. If the material 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 should be broadly interpreted to include any part of a tank, a pipe, or any part thereof. It is understood that in configuration, a cooler is distinct 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 a cooler. The cooler first cools the warm pyrolysis solids with steam to reach the first cooler temperature, and then , and operates to cool the air to reach a second cooler temperature, the second cooler temperature being Reduced ignition hazard of warm pyrolysis solids in the presence of air below 1 condenser temperature is related to.

[0215] After cooling to ambient conditions, the carbonaceous solids are collected, stored, and transported to another operating site. may be transferred to another location or otherwise disposed of, traded or sold. The solids can be fed into a unit 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. A portion of the material (e.g., large chunks) may be returned to the grinding unit. Small and Large Particles The cooled effluent may be recovered for separate downstream use. The pyrolysis solids are milled into fine powders such as pulverized carbon or activated carbon products, or are subjected to abrasive 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 the efficiency and achieve the desired carbon purity, and bio-origin The activated carbon of the source or the reagents incorporated are selected to improve one or more properties of the downstream product. Certain additives can be broadly classified into 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] The additives may be added at any suitable point during the entire 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 milling step; before, during or after the sizing step and / or may be added before, during, or after the packaging step. Additives are used in feedstock supply facilities, transport trucks, unloading equipment, storage bins, conveyors ( (including open or closed conveyors), dryers, process heaters, or any other units 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. Additives can be added after carbonization or Or even after micronization it may 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 provided. The hopper 2104 receives the feedstock 210 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 transported to the biomass The steam flow 2114 is introduced into the reactor 2112 in a countercurrent manner to the passages. 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 exhaust gas stream 2158 with the The gas flow 2158 may include nitrogen and / or carbon dioxide. Gas stream 2158, or a portion thereof, is passed through passage 2160 to reactor 2112, 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 illustrates 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. A first multizone reactor unit 2212A is substantially similarly configured. In this embodiment, the biogenic activated carbon 222 produced by the reactor 2212A At least a portion of 6A passes through passage 2202 into hopper 2204 and then into a second reaction 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 20 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 additionally, the second reactor 2212B is indirectly heated by the 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 may 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. This process provides a follow-up process: (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, A feedstock is mechanically conveyed, said feedstock being mixed with a vapor stream comprising a substantially inert gas and and an activating agent comprising at least one of water and carbon dioxide in a countercurrent manner. generating solids, condensable vapors, and non-condensable gases (including the aforementioned condensable vapors and of non-condensable gas enters the aforementioned vapor stream), (d) removing at least a portion of said vapor stream from said reaction zone. generating a separated vapor stream; and (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 from said reaction zone(s) as biogenic activated carbon; and recovering at least a portion of said solids.

[0222] In some embodiments, at least a portion of the moisture contained within the feedstock is removed. For example, the feedstock may contain about 8% by weight or about 4% by weight of The dried product may contain less than about 12% moisture by weight, such as less than about 12% moisture by weight. In an embodiment, no further water is added to the feedstock. The activator is added to the feedstock from the beginning. It may contain water derived from the moisture contained in the material.

[0223] In some embodiments, the activating agent comprises both water and carbon dioxide. The ratio of carbon dioxide 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 The reaction zone is maintained at a reaction temperature selected from 1000 to 900° C. All of the indirectly heated reaction zones are In some embodiments, the maximum reaction temperature is maintained at 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. The method includes removing all of the vapor stream from the steam exhaust area.

[0226] In some embodiments, step (e) comprises adding to the gas inlet of the reaction zone and / or and introducing at least a portion of the separated vapor stream into the feedstock prior to step (c). In some embodiments, step (e) comprises adding 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). Including the incorporation of some thermally treated 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 adding 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%, 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%, 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%, About 58%, about 59%, about 60%, about 61%, about 62%, about 63%, about 64%, about 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%, About 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%, approx. 26%, approx. 27%, approx. 28%, approx. 29%, approx. 30%, approx. 31%, approx. 32%, approx. 33%, approx. 34%, approx. 35%, approx. 36%, approx. 37%, approx. 38%, approx. 39%, approx. 40%, approx. 41%, approx. 42%, approx. 43%, approx. 44%, approx. 45%, approx. 46%, approx. 47%, approx. 48%, approx. 49%, approx. 50%, approx. 51%, approx. 52%, approx. 53%, approx. 54%, approx. 55%, approx. 56%, approx. 57%, approx. 58%, approx. 59%, approx. 60%, approx. 61%, approx. 62%, approx. 63%, approx. 64%, approx. 65%, approx. 66%, approx. 67%, approx. 68%, approx. 69%, approx. 70%, approx. 71%, approx. 72%, approx. 73%, approx. 74%, approx. 75%, approx. 76%, approx. 77%, approx. 78%, approx. 79%, approx. 80%, approx. 81%, approx. 82%, approx. 83%, approx. 84%, approx. 85%, approx. 86%, approx. 87%, approx. 88%, approx. 89%, approx. 90%, approx. 91%, approx. 92%, approx. 93%, approx. 94%, approx. 95%, approx. 96%, approx. It contains 97%, about 98%, about 99%, or about 100% carbon dioxide.

[0230] In some embodiments, the adjusted gas composition may be between 0% and 100% nitrogen, e.g. ,About 0%,About 1%,About 2%,About 3%,About 4%,About 5%,About 6%,About 7%,About 8%,About 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% , approx. 26%, approx. 27%, approx. 28%, approx. 29%, approx. 30%, approx. 31%, approx. 32%, approx. 33% , approx. 34%, approx. 35%, approx. 36%, approx. 37%, approx. 38%, approx. 39%, approx. 40%, approx. 41% , 42%, 43%, 44%, 45%, 46%, 47%, 48%, 49% , approx. 50%, approx. 51%, approx. 52%, approx. 53%, approx. 54%, approx. 55%, approx. 56%, approx. 57% , 58%, 59%, 60%, 61%, 62%, 63%, 64%, 65% , approx. 66%, approx. 67%, approx. 68%, approx. 69%, approx. 70%, approx. 71%, approx. 72%, approx. 73% , approx. 74%, approx. 75%, approx. 76%, approx. 77%, approx. 78%, approx. 79%, approx. 80%, approx. 81% , approx. 82%, approx. 83%, approx. 84%, approx. 85%, approx. 86%, approx. 87%, approx. 88%, approx. 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. ,About 0%,About 1%,About 2%,About 3%,About 4%,About 5%,About 6%,About 7%,About 8%,About 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% , approx. 26%, approx. 27%, approx. 28%, approx. 29%, approx. 30%, approx. 31%, approx. 32%, approx. 33% , approx. 34%, approx. 35%, approx. 36%, approx. 37%, approx. 38%, approx. 39%, approx. 40%, approx. 41% , 42%, 43%, 44%, 45%, 46%, 47%, 48%, 49% , approx. 50%, approx. 51%, approx. 52%, approx. 53%, approx. 54%, approx. 55%, approx. 56%, approx. 57% , 58%, 59%, 60%, 61%, 62%, 63%, 64%, 65% , approx. 66%, approx. 67%, approx. 68%, approx. 69%, approx. 70%, approx. 71%, approx. 72%, approx. 73% , approx. 74%, approx. 75%, approx. 76%, approx. 77%, approx. 78%, approx. 79%, approx. 80%, approx. 81% , approx. 82%, approx. 83%, approx. 84%, approx. 85%, approx. 86%, approx. 87%, approx. 88%, approx. 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 less than 8%, less than about 6%, less than about 4%, or less 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 be adjusted to include, in some embodiments, at least At least about 70% by weight of nitrogen, at least about 75% by weight of nitrogen, at least about 80% by weight of 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 deliver a feedstock to an 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 a thermally treated form thereof. Step (e) determines the yield of carbon in the solid. Further, step (e) preferably increases the surface area and iodine value of the solid. In some embodiments, step (f) may include using a biogenic activated carbon. This involves recovering all of the solids from the reaction zone by means of a distillation process.

[0235] Additives may be optionally introduced before, during, or after one or more of steps (a) to (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, dopant Lomite, dolomitic lime, fluorite, fluorospar, bentonite, calcium oxide Alkaline, lime, sodium hydroxide, potassium hydroxide, hydrogen bromide, hydrogen chloride, sodium silicate , 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 uranium 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 flux is generated by the presence of a magnetic metal, such as iron, or a compound thereof. The carbonaceous coal is composed of 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 is responsive 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-magnetic material that itself 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 comprises depositing graphene on a substrate in two or three dimensions. In order 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 are CO, CO2 , CH4, light hydrocarbons, tars, etc. An exemplary liquid stream may include 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. It can also be a liquid / vapor stream. External sources and gases recycled within the system, i.e., separated steam streams or their thermally Combinations, including mixtures in processed forms, are also possible.

[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, A feedstock is mechanically conveyed, said feedstock being mixed with a vapor stream comprising a substantially inert gas and and an activating agent comprising at least one of water and carbon dioxide in a countercurrent manner. generating solids, condensable vapors, and non-condensable gases (including the aforementioned condensable vapors and of non-condensable gas enters the aforementioned vapor stream),

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

[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 said solid from said 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 Graphene-containing biogenic activated carbon is a material that is For example, the graphene fraction in biogenic activated carbon may vary significantly compared to that 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 may be .8, about 0.9, about 0.95, or even more.

[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 carbon-containing vapors passing through a pyrolyzed or pyrolyzed feedstock. It is believed that graphene may reside primarily at or near the surface of the resulting solid. In another embodiment, sufficient heat and mass transport into the solid can be used to form graphene. Formation can occur essentially throughout the solid.

[0250] The process further separates graphene from the graphene-containing biogenic activated carbon. Separation can be accomplished by mechanical means such as a centrifuge, a magnetic separator, or an electrostatic precipitator, respectively. This can be accomplished 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 provides carbon 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 is provided. 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, said feedstock being mechanically conveyed and passing said feedstock through 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 (said non-condensable gases enter said vapor stream);

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

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

[0258] (f) removing at least said solids from said reaction zone(s). and recovering at least a portion of the solid, the solid comprising a 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, said feedstock being mechanically conveyed and passing said feedstock through 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 (said non-condensable gases enter said vapor stream);

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

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

[0265] (f) removing at least said solids from said reaction zone(s). and recovering at least a portion of the solid, the solid comprising a 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 further comprises: forming a substrate or device using at least a portion of the solid recovered in step (f). The method further includes fabricating graphene on the chair.

[0267] In some embodiments, graphene or graphene-containing biogenic activated carbon is , responsive to an externally applied magnetic field. In some embodiments, the graphene or Graphene-containing biogenic activated carbons have electrical conductivity values ​​and / or electrical conductivity 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 the preparation of a fluororesin 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 transporting said feedstock in one or more indirectly heated reaction zones; and mixing the feedstock with a steam stream containing a substantially inert gas and water or carbon dioxide. and reacting the solid, condensable vapor, and (The aforementioned condensable vapor and the aforementioned non-condensable gas are the aforementioned into the steam stream),

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

[0273] (e) removing at least a portion of said separated vapor stream or a thermally treated form thereof; to said feedstock and / or to the gas of said reaction zone(s) prior to step (c). recirculating the carbon in said solid to an 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 about 55% by weight of the activated carbon on a dry basis. or more total carbon, about 15% or less hydrogen, and about 1% or less nitrogen, At least a portion of the bio-based activated carbon is in the form of graphene, and the bio-based activated carbon is The charcoal composition is characterized by an iodine value greater than about 500, and the biogenic activated charcoal described above is Responds to a magnetic field applied 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, in the presence of a substantially inert gas, step (a'), (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. pyrolyzing the mixture to produce 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 noncondensable gases from the hot pyrolysis solids; and to separate a part of it.

[0282] (f) In a cooling zone, the hot pyrolysis solids are cooled to about 100° C. 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 biological origin, containing at least a portion of warm pyrolytic or cold pyrolytic solids; recovering the activated carbon product; and

[0285] (i) micronizing said biogenic activated carbon composition to produce said 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 produce 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 solids; 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; and

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

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

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

[0297] In some embodiments, the process further comprises adding an additive prior to the pyrolysis step. In such an embodiment, the resulting biogenic activated carbon comprises the additive were produced without or with additives added during or after the pyrolysis step, Can be produced in higher mass yields than biogenic activated carbon produced in an otherwise identical manner 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 prior to the pyrolysis step. In some embodiments, the results are The resulting biogenic activated carbon is free of additives (or may be added during or after the pyrolysis step). (with additives added) but produced by an otherwise identical process It has a higher fixed carbon content compared to biogenic activated carbon. In the experiment, the additives were added during or after the pyrolysis step, in the same manner except that the additives were added during or after the pyrolysis step. Overall, biogenic activated carbons have a higher solubility than process-produced biogenic activated carbons. In some embodiments, the bioavailable bioavailable is more completely and / or evenly distributed. The activated carbons were otherwise identical except that the additive was added either before or after the pyrolysis step. Compared with the biogenic activated carbon produced by the single process, the When combined, less additive is required to obtain the desired performance characteristics.

[0298] In some embodiments, the additive is a metal, a metal oxide, a metal hydroxide, or the like. For example, the additive may be magnesium, manganese, aluminum, or a combination of these. nium, 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), may be selected from these combinations, but is in no way limited to these.

[0300] In some embodiments, the additive is selected from a metal halide. Genides are compounds formed between metals and halogens (fluorine, chlorine, bromine, iodine, and astatine). The 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 Typically, this is achieved by neutralization. In some embodiments, the additive is an iron halide. ferric 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] 1% by weight or less of nitrogen;

[0305] not more than 0.5% by weight 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 are iodide ion, hydrogen iodide, , iodide salts, metallic iodides, ammonium iodide, iodine oxide, triiodide ion, triiodide Iodide salts, metal triiodides, ammonium triiodide, iodate ion, iodate salts, boron Iodide, iodoform, iodic acid, methyl iodide, iodine-containing hydrocarbons, periodic acid, o Periodic acid, metaperiodic acid, and combinations thereof, salts, acids, bases, or derivatives 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; A removing step;

[0313] (c) Optionally degas the feedstock to remove any granules, if any, contained within the feedstock. removing at least a portion of the interatomic oxygen;

[0314] (d) in a pyrolysis zone, in the presence of a substantially inert gas, ℃ to about 700 ℃ for at least 10 minutes, hot pyrolysis 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 noncondensable gases from the hot pyrolysis solids; and isolating a portion of the mixture.

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

[0317] (g) Cooling the warm pyrolysis solids in a cooling unit separate from the cooling zone to produce cold 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 includes:

[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 degas the feedstock to remove any granules, if any, contained within the feedstock. removing at least a portion of the interatomic oxygen;

[0324] (d) in a pyrolysis zone, in the presence of a substantially inert gas, ℃ to about 700 ℃ for at least 10 minutes, hot pyrolysis 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 noncondensable 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 solids are cooled to about Cool below the decomposition temperature for at least 5 minutes to generate warm pyrolysis solids. And,

[0327] (g) Cooling the warm pyrolysis solids in a cooling unit separate from the cooling zone to produce cold generating a pyrolysis solid that is

[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 is 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. Iodine or 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 not used. Alcohols such as methanol or ethanol may 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 yolk and lysine, and is preferably added to the biogenic activated carbon composition for incorporation. It involves iodine introduced as a solid that sublimes to iodine vapor. At room temperature, iodine is a solid. Upon heating, iodine sublimes into steam. Thus, 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 sublime and the I2 vapor penetrates the carbon particles, Thus, iodine may 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. The present invention provides 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 exhaust 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 exhaust 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 exhaust 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 nitriles, metal halides, iodine, iodine compounds, and combinations thereof. In some embodiments, the additive is selected from magnesium, manganese, arsenic, Aluminum, nickel, iron, chromium, silicon, boron, cerium, molybdenum, phosphorus, tantalum ngsten, 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 contaminant is a hazardous air pollutant. 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

[0338] In some embodiments, the contaminant-adsorbed carbon particles are contaminant-adsorbing particles that are capable of detecting contaminants such as carbon dioxide, nitrogen oxides, mercury, and 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 one 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') combusting said contaminant-adsorbed carbon particles. and 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 comprising mercury;

[0345] (b) separating the gas phase exhaust stream from a biogenic activated carbon composition comprising 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 Enhances the aforementioned electrostatic precipitation during step (c), thereby improving mercury control.

[0348] In some embodiments, the method further comprises: (d) disposing the other electrostatic 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; and generating a gas phase exhaust stream containing the dye, the biogenic activated carbon composition comprising at least Each of the two particles adsorbs at least a portion of the contaminant.

[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 biogenic activated carbon composition described above. 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 The pollutants are 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 includes additives such as acids, bases, salts, metals, metal oxides, metal hydroxides, metal halides, and iodides. 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 ferric chloride, ferric 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 A heat value of 5,000 BTU / lb, e.g., about 5,000, at least about 6,000, 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 10,000 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 locations where fuel may be present during injection, such as in fuel yards, storage bins, on conveyors, in mixers, Alternatively, or in addition, biologically derived Activated carbon is burned either in admixture with or independent of other fuel source(s). By way of example and not of 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 at or before the charcoal The oxygen-containing feedstock may be 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 generating 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 is 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, Cr, iron, chromium, silicon, boron, cerium, molybdenum, phosphorus, tungsten, vanadium ferric chloride, ferric 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, iodine 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 a metal salt, a compound thereof, a salt thereof, and a mixture thereof. In some embodiments, the at least one contaminant comprises an organic compound. In some embodiments, the at least one contaminant comprises a halogen. In some embodiments, the at least one contaminant comprises hydrogen sulfide. At least one of the contaminants comprises a chlorinated by-product. 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 aforementioned activated carbon. In some embodiments, the method further comprises regenerating the particles. It further includes combusting the elementary 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 further comprising:

[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, the sulfur contaminants are 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 sulfides, 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, iodine compounds, and combinations thereof. In this embodiment, the additives are magnesium, manganese, aluminum, nickel, iron, chromium, , silicon, boron, cerium, molybdenum, phosphorus, tungsten, vanadium, ferric chloride, Iron bromide, magnesium oxide, dolomite, dolomitic lime, fluorite, fluorospar -, bentonite, calcium oxide, lime, sodium hydroxide, potassium hydroxide, water bromide 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) includes filtering and / or permeating said liquid. In the 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 includes administering the activated carbon particles directly to the body. (c) further comprising sedimenting 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 engine In some embodiments, the process is selected from the group consisting of ethanol production. In some embodiments, the liquid is a naturally occurring 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, prior to step (a), the water has a concentration of greater than about 50 mg / L. of 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 field, wastewater streams are used in metal mining, acid mine drainage, mineral processing, municipal wastewater 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, the additives are magnesium, manganese, aluminum, nickel, iron, chromium, potassium, etc. 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 comprising at least one sulfur contaminant;

[0371] (b) contacting the gas phase exhaust 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 exhaust stream; and separating the portions.

[0373] In some embodiments, the sulfur-containing contaminants are elemental sulfur, sulfuric acid, sulfurous acid, sulfur dioxide, Yellow, sulfur trioxide, sulfate anion, bisulfate anion, sulfite anion, bisulfite anion Anions, thiols, sulfides, disulfides, polysulfides, thioethers, thioesters, thioa 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, their salts, their derivatives, and combinations thereof. The phase exhaust stream is derived from or is generated from the combustion of a fuel that includes 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; and In some embodiments, the additive is an acid, a base, a salt, a gold metal oxides, metal hydroxides, metal halides, iodine, iodine compounds, and the like In some embodiments, the additive is selected from the group consisting of malic acid, ethyl acetate ... 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) comprises filtering the mixture. 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, comprising:

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

[0376] (b) subjecting said gas or liquid stream to a process for producing, on a dry basis, a mixture of about 55% by weight or more total carbon, about 1 5% by weight or less hydrogen, and about 1% by weight or less nitrogen, and at least about 500% by weight iodine. and contacting said composition with a biogenic activated carbon composition comprising an exogenous cation. 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, comprising:

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

[0379] (b) subjecting said gas or liquid stream to a process for producing, on a dry basis, a mixture of about 55% by weight or more total carbon, about 1 5% by weight or less hydrogen, and about 1% by weight or less nitrogen, and at least about 500% by weight iodine. and contacting said carbon with a biogenic activated carbon composition comprising a prime 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 present invention provides a method for removing a fluorine-containing compound, the method comprising 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 about 1% by weight or less of nitrogen (at least one of the aforementioned carbons) Some of these 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 in the form of a biogenic activated carbon composition as described above. 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 % 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, sinks for static electricity dissipation, materials for electron or ion transport, Band communication system components, infrared sensor components, chemical sensor components, biological sensor components a graphene aerospace 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 about 1% by weight or less of nitrogen (at least one of the aforementioned carbons) Some of these exist in the form of graphene.

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

[0389] (c) providing said graphene in isolated form or in said biogenic activated carbon composition; This includes use as part of a product in an adhesive, sealant, coating, paint, or ink. 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 about 1% by weight or less of nitrogen (at least one of the aforementioned carbons) Some of these exist in the form of graphene.

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

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

[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 about 1% by weight or less of nitrogen (at least one of the aforementioned carbons) Some of these exist in the form of graphene.

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

[0397] (c) providing said graphene in isolated form or in said biogenic activated carbon composition; As part of an article, it can be used 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 about 1% by weight or less of nitrogen (at least one of the aforementioned carbons) Some of these exist in the form of graphene.

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

[0401] (c) providing said graphene in isolated form or in said biogenic activated carbon composition; and use in a graphene-based circuit or memory system 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 about 1% by weight or less of nitrogen (at least one of the aforementioned carbons) Some of these exist in the form of graphene.

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

[0405] (c) providing said graphene in isolated form or in said biogenic activated carbon composition; As part of an article, 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 about 1% by weight or less of nitrogen (at least one of the aforementioned carbons) Some of these exist in the form of graphene.

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

[0409] (c) providing said graphene in isolated form or in said biogenic activated carbon composition; As part of a fuel delivery system, it can be used as 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 about 1% by weight or less of nitrogen (at least one of the aforementioned carbons) Some of these exist in the form of graphene.

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

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

[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 about 1% by weight or less of nitrogen (at least one of the aforementioned carbons) Some of these exist in the form of graphene.

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

[0417] (c) providing said graphene in isolated form or in said biogenic activated carbon composition; As part of the present invention, 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 about 1% by weight or less of nitrogen (at least one of the aforementioned carbons) Some of these exist in the form of graphene.

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

[0421] (c) providing said graphene in isolated form or in said biogenic activated carbon composition; as part of an article or 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 about 1% by weight or less of nitrogen (at least one of the aforementioned carbons) Some of these exist in the form of graphene.

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

[0425] (c) providing 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 about 1% by weight or less of nitrogen (at least one of the aforementioned carbons) Some of these exist in the form of graphene.

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

[0429] (c) providing 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 about 1% by weight or less of nitrogen (at least one of the aforementioned carbons) Some of these exist in the form of graphene.

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

[0433] (c) providing said graphene in isolated form or in said biogenic activated carbon composition; and using the resulting mixture 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) an additive selected to assist in the removal of a selected contaminant from the gas-phase exhaust 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 the activated carbon particles, thereby providing the contaminant-adsorbed carbon particles in the gas phase exhaust stream. and

[0439] (e) separating at least a portion of the contaminant-adsorbed carbon particles from the gas-phase exhaust stream to determine whether the contaminants are present. 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 the activated carbon particles. Alternatively, the additive may be introduced directly into the gas phase exhaust stream.

[0441] Additives (to aid in the removal of selected contaminants from the gas phase exhaust stream) include acids, Bases, salts, metals, metal oxides, metal hydroxides, metal halides, iodine, iodine compounds or a combination thereof. In some embodiments, the additive is iodine or an iodine compound, or iodine and one or more iodine compounds, optionally dissolved in a solvent. Contains a combination of uranyl 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 condensable gas.

[0443] In some embodiments, the contaminant-adsorbed carbon particles are in an adsorbed or 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 pulmonary circulation comprising the steps of:

[0444] In some embodiments, the gas phase exhaust stream is a mixture of a fuel and 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 separation in step (e) comprises filtration, e.g., A woven fabric filter may be utilized. In some embodiments, in step (e), Separation methods include electrostatic precipitation. Scrub cleaning (including wet or dry scrubbing) may also be 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 adsorbed, either catalytically or non-catalytically. The contaminant-adsorbed carbon particles, or a regenerated form of them, are then 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 contains iodine or an iodine-containing compound; providing activated carbon particles comprising:

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

[0449] (c) introducing activated carbon particles into the gas phase exhaust 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 from the exhaust gas to produce a mercury-reduced gas phase exhaust stream.

[0451] In some variations, a process for producing energy is provided, the process comprising: The 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 the biogenic activated carbon composition in the carbon-containing feedstock may result in the formation of oxidative by-products. for adsorbing at least one contaminant derived from or derived from a carbon-containing feedstock. effective, thereby reducing pollutant emissions,

[0455] The biogenic activated carbon composition may be used to treat a variety of conditions, including but not limited to acids, bases, salts, metals, metal oxides, metal hydroxides, metal Additives selected from halides, iodine, iodine compounds, or combinations 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 generated as a by-product of the oxidation. The feedstock may, in various embodiments, 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; 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, a 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 a selected contaminant from the liquid; To do,

[0462] (d) contacting the liquid with the activated carbon particles and the additive to produce at least one selected At least a portion of the contaminants is adsorbed onto the activated carbon particles, thereby forming 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 0.05% 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. , an iodine compound, or a combination 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 I, II, III, IV, or a combination of these 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 triiodide, iodate ion, iodate salts, polyiodides, Iodoform, iodic acid, methyl iodide, iodine-containing hydrocarbons, periodic acid, orthoperiodine periodic 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] The additive results in a final product with a higher energy content (energy density). The increase in energy content can be attributed to 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 additive 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. Chemically modify biomass to reduce cell wall rupture for greater strength / integrity. In some embodiments, the additive increases 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 mechanical properties such as shear modulus. Additives are not used simply 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 improved by using biogenic activated carbon containing additives. This can occur within parts of the composition, thereby improving the final strength.

[0470] Chemical additives can be applied to wet or dry biomass feedstock. The additive 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 into another container.

[0471] In certain embodiments, a soaking pretreatment is used, and the solid feedstock is pretreated batch by batch with: 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 provides the energy required for pyrolysis. These or other methods may reduce the amount of ghee and / or increase the yield of carbonaceous products. In embodiments, the additives applied to the feedstock are further described below with respect to composition. In this manner, the carbonaceous product can be provided with the functionality desired for its intended use.

[0473] In some embodiments, the process for producing biogenic activated carbon comprises warm Dimensioning (e.g., sorting, screening, classifying, etc.) of pyrolysis solids or cold pyrolysis solids ) to form a sized pyrolyzed solid. The pyrolysis solids obtained are suitable for use in applications requiring activated carbon products with certain particle size characteristics. It can be used in the following manner.

[0474] Throughput, or process capacity, can range from small laboratory-scale units to any These vary widely from batch, demonstration, or semi-industrial scale to full industrial scale biorefineries. 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 tons / day, 1 00 tons / day, 500 tons / day, 1000 tons / day, 2000 tons / day or more It is.

[0475] In some embodiments, a portion of the produced solids is present at the front end of the process, i.e. , may be recycled to a drying or degassing unit, or may be used in 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 recirculated independently, carried forward to a subsequent step, or or may be removed / purged from the process at any time.

[0476] In some embodiments, the pyrolysis materials are recovered and then subjected to further pyrolysis. to separate reactors to create a product with higher carbon purity. In an embodiment, the secondary process may take place in a simple container such as a steel drum, where the heating An inert gas (such as heated N2) is passed through it. Other vessels useful for this purpose include Includes process tanks, barrels, bins, totes, cloth bags, and roll-offs. This secondary sweep gas with the product may be sent, for example, to a process gas heater or may be fed to the main To cool the final product, for example, an inert gas tank at ambient temperature may be used. A separate flow 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. The process is carried out in a furnace 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 operative communication with the stem;

[0480] (c) a biomass processing unit including a plurality of zones disposed in operative 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 pyrolysis zone. outlets for removing condensable vapors and non-condensable gases from the

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

[0482] (e) a carbon recovery unit disposed in operative 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 operative communication with the stem;

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

[0487] (d) a thermal decomposition reactor configured to decompose 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 cooling device disposed in the cooling device;

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

[0490] The system comprises at least one separator 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 feed 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, the cooling zone, and the 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 as described above). (may be integrated with a cooling zone).

[0494] The system may include a purging means for removing oxygen from the system. The means for introducing a substantially inert gas into the system includes one or more inlets for introducing a substantially inert gas into the system. and one or more outlets for removing substantially inert gas and displaced oxygen from the In some embodiments, the purge means is in operative communication between the dryer and the BPU. The deaerator is arranged in such a manner that the

[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 disposed 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 be comprised 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 connected to the various stages of the process, through 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 when

[0498] In some embodiments (see generally FIG. 4), the reactive gas probe is Such a reaction gas probe is disposed in operative 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 For example, feed rate, inert gas sweep rate, temperature (in one or more zones), The reaction can be controlled or adjusted by adjusting the pressure (in the reaction zone), additives, etc.

[0499] As intended herein, "monitoring and controlling" via a reactive gas probe refers to monitoring and controlling a reactive gas. Any one or more samplings via a gas probe are included, and are necessary or desirable. When considered as such, well-known principles of process control (feedback, feedforward, Proportional integral induction logic, etc.) can be used to adjust the manufacturing process or equipment based on the measurement results. should be construed to include.

[0500] The reactive gas probe can be configured to extract a gas sample in a number of ways. For example, the sampling line is designed so that when the sampling line is opened, a certain amount of gas is released through pyrolysis. 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 reaction gas probe has one gas output or a portion of it (e.g., a gas output radiator). It is associated with the line that branches off from the inn.

[0501] In some embodiments, the gas input and gas output are both inert gases in the zone. Periodically introduce gas and withdraw inert gas from the gas output with a process sample (see “Sample”). Such an arrangement can be used as a reactive gas probe by detecting the It can be used in zones that do not have separate gas inlets / outlets for substantially inert gases. or the reaction gas probe has a separate gas inlet / outlet in addition to the process inlet and outlet. Sampling inactive specimens that are periodically introduced and extracted 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 be different 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 concentration of the sample. This can then be analyzed by a suitable technique (gas chromatography (GC), Mass spectrometry (MS), GC-MS, or Fourier transform infrared spectroscopy (FTIR) The CO and / or CO2 concentrations in the gas phase are 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 pyrolysis 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 comprising an additional 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 the thermocouples placed in the cooling zone). The measured results 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 for determining, for example, the presence or absence of any It may be useful to determine the extent of mild pyrolysis.

[0506] In one particular embodiment, the cooling zone is configured with a gas inlet and the pyrolysis zone is configured with a gas inlet. an outlet for generating a gas phase in substantially countercurrent flow relative to the solid phase; Alternatively, or in addition, the preheat zone (if present) may comprise a gas outlet for discharging 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 reactor 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, Auger, Rotating Cone, Rotary Ram Kiln, Calciner, Roaster, Moving Bed Reactor, Transport Bed These include 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. It provides good control and does not dilute the pyrolysis products with carrier or fluidizing gas. Sand is a separate It may be reheated in the vessel.

[0509] In some embodiments where an ablative process is used, the feedstock is The ablation of any charcoal on the surface is a highly thermally conductive 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 whose walls are heated. can be inserted.

[0510] In some embodiments where a fluidized bed reactor is used, the feedstock is typically recycled. The hot sand bed may be fluidized by the gas that is the product gas. References to "sand" in this specification include similar substantially inert materials such as glass particles, recovered ash particles, etc. 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. This 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. Transport gases include recycled product gases and combustion gases. The high thermal conductivity of sand allows It ensures rapid heating of the feedstock and ablation is faster than conventional fluidized bed ablation. A separator is used to separate the product gas from the sand and coal 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 of the feedstock inlet, temperature, and a plurality of spatially separated zones configured for mixing within each zone; and a continuous reactor having a solids outlet, one of the zones being substantially inert to the BPU; The first gas inlet may be configured with a first gas inlet for introducing gas, and one of the zones may be configured with a first gas outlet. It may consist of 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 a process gas heater, if present.

[0514] The BPU must be at least 2 GHz and up to all bands present in the BPU (including all bands). The gas phase composition and gas phase residence time of the two zones can be separately adjusted.

[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 having a screw material feed system. In some embodiments, some or all of the BPUs are axially rotatable, i.e. The rotational speed determines the solids flow patterns and the heat and mass transport. Each zone consists of flights arranged on the inner wall to agitate the solids. 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 chips arranged across each band. In another embodiment, the reactors are arranged throughout each zone. The axially extending twin screw is included.

[0519] Some systems maintain the approximate size of the feed material throughout the process, Ability to transform a biofilm, i.e., to destroy or significantly damage its structure. In some embodiments, the pyrolysis zone is designed with the capacity to process mass feedstock. , Auger, screw, or Does not include rake.

[0520] In some embodiments of the present disclosure, the system is disposed in operative communication with the outlet. The process gas heater further comprises 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 vapor. 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 use at least some of the heat of combustion in 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 condensation system in at least a partially condensed form. a material disposed in operative communication with the cooler configured to combine the reactive vapor with the solid. The material enrichment unit further comprises a biomass enrichment unit. The material enrichment unit is a biomass enrichment unit that enriches the biomass obtained from the carbon recovery unit. The carbon content of the original activated carbon may be increased.

[0523] The system is designed to further pyrolyze the biogenic activated carbon to increase its carbon content. The separate pyrolysis zone may further comprise a separate pyrolysis zone adapted for pyrolysis. The separate pyrolysis zone may be a tank, barrel, or the like. Relatively simple containers, units, such as 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, a process for producing biogenic activated carbon includes:

[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 degas the feedstock to remove any granules, if any, contained within the feedstock. removing at least a portion of the interatomic oxygen;

[0529] (d) in a pyrolysis zone, in the presence of a substantially inert gas, ℃ to about 700 ℃ for at least 10 minutes, hot pyrolysis 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 noncondensable 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 solids are cooled to about 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 across the warm pyrolysis solid and / or the cold pyrolysis solid; 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 second portion of the pyrolysis product; and

[0534] (i) A bioreactor 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. Removing at least a portion of the condensable vapor from step (e) in vapor and / or condensed form. The process includes producing concentrated pyrolysis solids having increased carbon content through the decomposition of the solids. In an embodiment, step (h) comprises the step of (e) over the warm pyrolysis solid. A concentrated pyrolysis process having an increased carbon content through at least a portion of the non-condensable gas 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 the cold pyrolysis solids. In some embodiments, step (h) comprises the step ( e) passing at least a portion of the condensable vapor from the In some embodiments, the method further comprises the steps of: In step (h), the non-pyrolyzed solid from step (e) is dissolved in water 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 creating

[0538] In certain embodiments, step (h) comprises scanning across the cold pyrolysis solid. Removing substantially all of the condensable vapor from step (e) in vapor and / or condensed form. The method includes the steps of: producing a concentrated pyrolysis solid having an increased carbon content through the pyrolysis of the carbon dioxide gas; 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] The process comprises the steps of: 1) preparing a mixture of steam or gas prior to using the steam or gas for carbon enrichment; For example, the condensate obtained from step (e) may include various methods of treating or separating the condensate. 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 a first and a second output stream. In certain embodiments, the intermediate feed stream may be composed of 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. The separation may include or use packed beds, capillary columns, etc. Separation may be, for example, primarily by distillation, It can be based on absorption, adsorption, or diffusion and can be determined by the vapor pressure, activity, molecular weight, density, viscosity, etc., of 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 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 includes non-condensable gases. The 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 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 tower, a packed bed, a chromate The substrate may be a lithography column, or a membrane.

[0544] Thus, in some embodiments, the first output stream comprises a polar compound and the second output stream comprises a polar compound. The output stream contains non-polar compounds. The polar compounds are methanol, furfural, and acetic acid. The non-polar compound may include at least one carbon-containing molecule selected from the group consisting of acids. , 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 aryl, aryl, phenyl ...

[0545] Step (h) is a step that reduces the amount of biogenic The amount of carbon content increase can vary in various embodiments. For example, the amount may be about 1%, 2%, 5%, 10%, 15%, 25%, or more. It is highly likely.

[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 biogenic activity. 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 are typically carbon that forms solids under ambient conditions. 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), a certain 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 pores 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. In comparison, it may be 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 increase total carbon, fixed carbon, volatile carbon, or The degree of energy content increase may further be attributed to an increase in hydrogen. For example, the amount may be about 1%, 2%, 5%, 10%, 15%, 25%, or more. It is highly likely.

[0549] Further separation may be used to extract one or more unagglomerated products 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 syngas.

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

[0551] The 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, may be added to the process. Part of the gas that is utilized for energy in the pyrolysis step or is substantially inert 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 deactivated in the reactor. Similarly, by separating the non-condensable gases from the condensable vapors, The CO / CO2 stream may be, for example, an inert gas in the reactor system or the cooling system. The composition 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 feedstock where the addition of carbon is desired. This is based on the understanding that it can be applied to raw materials.

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

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

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

[0557] (c) passing a gas stream over the solids stream under favorable conditions to reduce the amount of 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 that provides 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 derived 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-circulating the gas flow to repeat the process. Recycle or reuse the carbon and / or energy of carbon-containing products In some embodiments, the process further comprises further increasing the ghee content. The process involves recirculating or reusing the gas stream to carry out the process. Increasing the carbon and / or energy content of a feedstock different from the carbon-containing material The present invention further includes:

[0560] In some embodiments, the process produces 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. The gas streams may be separated based on their relative volatility, relative polarity, or any other property. It may result from another processing of the carbon-containing material.

[0561] In some embodiments, the process involves re-circulating 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: Recycle or reuse the gas stream to reduce the carbon content of another feedstock. Further comprising increasing

[0562] The carbon-containing product has an increased total carbon content, higher solids content, and / or higher yields 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 operative communication with the stem;

[0566] (c) a BPU disposed in operative communication with the dryer (the BPU being 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 chiller disposed in operative communication with the BPU;

[0568] (e) throughout the solid to form a concentrated solid having an increased carbon content. A cooling device in operative communication with the cooling device, the cooling device being configured to pass condensable vapors and / or non-condensable gases therethrough. a material concentration unit disposed through the

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

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

[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 for generating a gas phase in substantially countercurrent flow relative to the solid phase; In these or other embodiments, the preheat zone and / or drying zone (or drying The gas phase is substantially countercurrent to the solid phase and is configured with a gas outlet. It is possible.

[0572] In certain embodiments, the system comprises:

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

[0574] (ii) a bottom inlet at the lower portion of the housing;

[0575] an inlet configured to convey 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 housing; and

[0579]

[0580] (v) a material transport system following the passageway and configured to transport solids; The body is at least a portion of the condensable vapor and / or at least a portion of the non-condensable gas. The material is concentrated in a material concentration unit having a pore size of 10 mm or less.

[0581] The present disclosure describes various compositions useful as biogenic activated carbon, 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; A removing step;

[0584] (c) Optionally degas the feedstock to remove any granules, if any, contained within the feedstock. removing at least a portion of the interatomic oxygen;

[0585] (d) in a pyrolysis zone, in the presence of a substantially inert gas, ℃ to about 700 ℃ for at least 10 minutes, hot pyrolysis 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 noncondensable gases from the hot pyrolysis solids; and isolating a portion of the mixture.

[0587] (f) in a cooling zone, in the presence of a substantially inert gas, the hot pyrolysis solids are cooled to about Cool below the decomposition temperature for at least 5 minutes to generate warm pyrolysis solids. 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. P.S.

[0590] In some embodiments, the process for producing biogenic activated carbon comprises warm Dimensioning (e.g., sorting, screening, classifying, etc.) of pyrolysis solids or cold pyrolysis solids ) to form a sized pyrolyzed solid. The pyrolysis solids obtained are suitable for use in applications requiring activated carbon products with certain particle size characteristics. It can be used in the following manner.

[0591] In some embodiments, the biogenic activated carbon has a molecular weight 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, Contains 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 the 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 can be measured using Evolutive 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 has greater than about 0.5% hydrogen by weight, e.g., greater than 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%, about 3.6%, about 3.8%, about 4%, or about 4% by weight The hydrogen content of the biogenic activated carbon may be any suitable amount known in the art. It may 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 an embodiment, the properties of the activated carbon product are determined by measuring the amount of the fossil fuel-based activated carbon product (such as i.e., those with very low hydrogen content) to hydrogen from fossil-fuel-based activated carbon products. and blending the activated carbon product with a suitable amount of a biogenic activated carbon product having a hydrogen content greater than the hydrogen content of the activated carbon product. and

[0593] The biogenic activated carbon has, 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 It may contain up to 0.5% nitrogen by weight. The biogenic activated carbon product may contain, on a dry basis, about 0. The biogenic activated carbon product may contain up to 5% by weight phosphorus, for example up to about 0.2% by weight 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 can be up to 20% by weight 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 sensitive 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 oxygen, e.g. , about 7% oxygen by weight, or about 0.3% oxygen by weight. The properties of the activated carbon product are similar to those of a certain amount of fossil fuel-based activated carbon product (i.e., very low (which has an oxygen content in excess of that of fossil-fuel based activated carbon products) Optimized by blending with a suitable amount of biogenic activated carbon product with 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 be modified to include hydrogen (other than any moisture that may be present), nitrogen, phosphorus, or sulfur. The present invention provides a reagent having little or essentially no yellow color and substantially no carbon and Any ash and moisture present. Thus, some embodiments may be dry / ash-free. The Company provides materials having up to and including 100% carbon on a DAF basis.

[0597] Generally speaking, feedstocks such as biomass contain silica and other ferrocene that are not easily released during pyrolysis. and various metals. It is possible to use pyrolysis solids without significant 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 basis 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 to no ash. or contains essentially no ash or other non-combustible material. This embodiment provides essentially pure carbon that contains 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% water. %, 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, 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 moisture content should be interpreted as including any form of water present in the The moisture content may also vary depending on the local environment, such as relative humidity. Moisture changes during transportation, transportation, and other logistics. The amount of protein that can be measured may be determined by any suitable method known in the art, including by any method known in the art.

[0600] Biogenic activated carbon is used for this purpose due to the higher heat value associated with the total combustion of bone-dry reagents. The term "energy content" refers to the energy density based on the The source activated carbon is approximately at least 11,000 Btu / lb and 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 to 15,000 Btu / The energy content is measured using methods known in the art, including, for example, ASTM D5865. The amount of the ion exchange reaction 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 of 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 with particles ranging from 0.2 mm to 1.5 mm in diameter. It can be produced as granular activated carbon, containing irregularly shaped particles having sizes in the range of 5 mm. 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 pelletized activated carbon containing the particles.

[0603] In some embodiments, the biogenic activated carbon is in the form of pressed particles, bound particles, or agglomerates. The starting materials for forming these objects are formed into structured objects containing grains. These bodies may be in the form of powders of reagents such as 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 the present specification means any sizing, milling, pulverization, or pulverization to reduce the average particle size. It is intended to include grinding, crushing, extrusion, or other primary mechanical processing. Micronization can be performed by batch, continuous, or continuous processes. It may be a continuous or semi-continuous process, and in some embodiments, the pyrolysis may be carried out at a temperature where the pyrolysis solids are formed. The processing may be performed at a different location than the processing at which the

[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, the feedstock chips are a mixture 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 has the same basic structure and structure as the starting material. and can maintain their 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 in minimum dimension The object may be generated as an object or may be formed into such an object. , the minimum or maximum dimension may be a length, width, or diameter.

[0607] Other variations of the present disclosure include incorporating additives into the process, 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 the process.

[0608] Other variations of the present disclosure include incorporating additives into the process, 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. The process includes at least one product additive that is introduced into the reagent after the process.

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

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

[0611] 5% by weight or less of hydrogen,

[0612] 1% by weight or less of nitrogen;

[0613] Optionally 0.5% to 10% by weight of oxygen,

[0614] not more than 0.5% by weight 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. , silicon, magnesium oxide, dolomite, dolomitic lime, fluorite, fluoro Selected from spar, bentonite, calcium oxide, lime, or combinations thereof. However, it is by no means limited to these.

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

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

[0620] 5% by weight or less of hydrogen,

[0621] 1% by weight or less of nitrogen;

[0622] Optionally 0.5% to 10% by weight of oxygen,

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

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

[0625] The additive is selected from an acid, a base, or a salt thereof.

[0626] Additives include sodium hydroxide, potassium hydroxide, magnesium oxide, hydrogen bromide, and water chloride. 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 has, on a dry basis,

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

[0629] 5% by weight or less of hydrogen,

[0630] 1% by weight or less of nitrogen;

[0631] Optionally 0.5% to 10% by weight of oxygen,

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

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

[0634] From metals, metal oxides, metal hydroxides, metal halides, or combinations thereof a first additive selected, 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 ferric chloride, ferric bromide, magnesium, manganese, aluminum, nickel , chromium, silicon, magnesium oxide, dolomite, dolomitic lime, fluorite, Choose from Fluorospar, bentonite, calcium oxide, lime, or a combination of these. The second additive may be independently selected from sodium hydroxide, potassium hydroxide, and oxide. 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 ferric chloride, ferric bromide, magnesium, manganese, aluminum, nickel Kel, Chromium, Silicon, Magnesium Oxide, Dolomite, Dolomite 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, water bromide chlorine, hydrogen chloride, sodium silicate, and combinations thereof. Consisting essentially of additives.

[0640] The amount of additive (or total additive) may be, for example, about 0.1% by weight, about 1% by weight, or less on a dry basis. %, about 5% by weight, about 10% by weight, or about 20% by weight. The amount of additive may vary widely from about 1% by weight. Reduce the energy content calculated on a total activated carbon weight basis (including additives) when added. It is understood that the additive(s) may be reduced in various embodiments. The biogenic activated carbon having a total weight of 1000 mg / kg or more (including additive(s)) of the biogenic activated carbon is In cases where the minimum is approximately 11,000 Btu / lb, the minimum is approximately 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 include additives to enhance the binder or final properties for a particular application. Additives are incorporated as other conditioning agents.

[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 classified as renewable. There are certain market mechanisms (e.g., renewable identification numbers, tax credits, etc.) that allow for the 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, can be recycled. Thus, in some embodiments, the bioactive The carbon content of the charcoal consists, consists essentially, or consists substantially of renewable carbon. For example, the fully biogenic activated carbon formed by the methods disclosed herein can be: (a) regenerated; (b) pyrolysis solids derived exclusively from biomass from renewable carbon sources; and Consisting of, consisting essentially of, or consisting essentially 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 or the biogenic activated carbon described in the compositions described herein, or Any portion, combination, or derivative of any of the above.

[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 are utilized for their absorption properties, or in metal refining (reduction of metal oxides, etc.) or other industries Utilized for their reactive properties during processing or as a catalyst 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 specialized applications that may be developed. It can be utilized.

[0645] The biogenic activated carbon prepared according to the processes disclosed herein is a biomass fuel that can be used in a wide range 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 carbon is able 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 applications, including: Comparable or equivalent to the level of inert material (e.g., ash) associated with the activated carbon product. Some have levels of inert materials (e.g., ash) that are at or below the In embodiments, the biogenic activated carbon has particle size and / or molecular weight associated with conventional activated carbon products. or particle size distribution that is comparable to, exceeds, or is approximately equal to In some embodiments, the bioactive material has a particle size and / or particle size distribution of The charcoal product has a particle shape comparable to or substantially similar to that associated with conventional activated charcoal products. In some embodiments, the biological The original activated carbon product has a particle shape that differs substantially from the particle shapes associated with conventional activated carbon products. In some embodiments, the biogenic activated carbon product has a shape similar to that of a 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 similar to the pore size associated with the product In some embodiments, the biogenic activation product has the same pore size. Comparable or substantially similar to particle friction resistance values ​​associated with conventional activated carbon products. In some embodiments, the produced particles have a friction resistance value equal to or equal to that of the particles. The bio-derived activated carbon products match or exceed hardness values ​​associated with conventional activated carbon products. Qualitatively similar or identical hardness values. In some embodiments, Therefore, biogenic activated carbon products have demonstrated hardness values ​​comparable to or superior to those associated with conventional activated carbon products. Qualitatively, the hardness value is about equal to or less than the hardness value of some embodiments. In some cases, biogenic activated carbon products have bulk density values ​​that are 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 related to conventional activated carbon products. Comparable to, substantially less than, or nearly less than the bulk density value set forth above. In some embodiments, the biogenic activated carbon product has a bulk density value that is have an absorption capacity comparable to or substantially similar to that 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 properties of potential interest beyond 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 a variety of activated carbon products. Activated carbon is used in a wide variety of applications, including water treatment, air purification, and water purification. 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. Key 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 a measurement of 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 mesopore 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) Pore ​​size distribution and pore volume are important in determining the 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 measurement of the resistance of activated carbon to friction. This is due to the ability of the 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-dissipation of the device. Excessive wear may occur. Exemplary wear values, measured according to ASTM D3802, are approximately 1%. About 5%, about 10%, about 15%, about 20%, about 25%, about 30%, about 35%, about 40%, about 45%, approx. 50%, approx. 55%, 60%, approx. 65%, approx. 70%, approx. 75%, approx. 80%, approx. 8 5%, about 90%, about 95%, about 96%, about 97%, about 98%, about 99%, or about 99% The range of ultra-high is from about 1% to about 99%.

[0651] In some embodiments, the biogenic activated carbon is subjected to friction in the main facility for processing the activated carbon. An optimum range of hardness can be achieved that is adequately resistant to wear and tear, but does not cause abrasion or wear. This optimum condition is determined in some embodiments of the present disclosure based on 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 99% or higher. is known to be a suboptimal feedstock for achieving optimal hardness. In some embodiments where the application can address high hardness, the process of the present disclosure By operating it, the hardness can be increased or maximized to about 75%, about 80%, about 8 5%, about 90%, about 95%, about 96%, about 97%, about 98%, about 99%, or about 99% In accordance with the present invention, a biogenic activated carbon product can be produced having an abrasion value of greater than 0.01%.

[0653] The biogenic activated carbon provided by the present disclosure has a wide range of commercial applications. Without limiting its usefulness, biogenic activated carbon is used in emission control, water purification, groundwater treatment, wastewater treatment, air stripping, and many other applications. 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 filters, mist filters, piping, piping modules, adsorbents, absorbers, and columns It can be utilized.

[0654] Some variations have, on a dry basis, about 55% or more 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 magnet contains additives that respond to an externally applied magnetic field. Such additives are iron or iron-containing. Graphene itself (without additives) can be subjected to an externally applied magnetic field. Can respond.

[0656] Some variations have, on a dry basis, about 55% or more total carbon, about 15% or less by weight Organisms that contain hydrogen, less than about 1% by weight of nitrogen, and between about 0.0001% by weight and about 1% by weight of iron. The present invention provides an activated carbon composition comprising an activated carbon having a carbon content of 10 ... The carbonaceous composition is characterized by an iodine value greater than about 500, and the composition is resistant to an externally applied iodine. Responds to magnetic fields.

[0657] Some variations have, on a dry basis, about 55% or more 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 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) an additive selected to assist in the removal of a selected contaminant from the gas-phase exhaust 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; and adsorbing at least a portion of the contaminant onto activated carbon particles, thereby providing the contaminant-adsorbed carbon particles in the gas phase exhaust stream. To produce offspring,

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

[0666] The additive of 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. As will be appreciated by those skilled in the art, 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 contaminants selected (in gas phase emissions) 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 comprises at least about 1% by weight 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, Pursuant to Section 112 of the Clean Air Act, United States 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 are included among selected contaminants of potential concern.

[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 hazardous to human health or harmful to the environment. EPA has Regulating Volatile Organic Compounds in Land. The EPA's definition of volatile organic compounds is 40 Federal Regulations and is set forth in CFR section 51.100, which is incorporated herein by reference in its entirety. Be absorbed.

[0670] A non-condensable gas is a gas that does 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 combinations thereof. Not limited.

[0671] Several contaminants may be removed by activated carbon particles. The dye-adsorbed carbon particles are capable of detecting 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 those listed above. and may allow for the control of certain targeted contaminants (e.g., selenium).

[0672] In certain embodiments, the contaminant-adsorbed carbon particles are capable of detecting contaminants such as carbon dioxide, nitrogen oxides, mercury, etc. and at least one, at least two, or at least three of sulfur dioxide, or All of these in any combination.

[0673] The separation in step (e) can be carried out, for example, by filtration (e.g., a woven 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. Pulse jet, Shaker style and reverse-air systems There are several types of baghouses, including the scrubber baghouse. This 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, allowing fine particulate matter to be easily removed from the air stream. 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 pollutant-adsorbed carbon particles, or a regenerated form thereof, can be combusted 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 hydride is 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, ferric chloride, Iron bromide, magnesium oxide, dolomite, dolomitic lime, fluorite, fluorospar -, bentonite, calcium oxide, lime, sodium hydroxide, potassium hydroxide, water bromide 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 comprising 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 comprising mercury;

[0682] (c) introducing activated carbon particles into the gas phase exhaust stream to deposit at least a portion of the mercury on 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 the gas-phase emission stream using electrostatic precipitation or filtration. and separating a portion of the me...

Claims

1. 1. A continuous process for producing biogenic activated carbon, the process comprising: Providing a starting carbon-containing feedstock comprising biomass; Mechanically conveying the feedstock in at least one indirectly heated reaction zone. and countercurrently contacting the feedstock with a vapor stream comprising an inert gas and an activator, thereby generating solids, condensable vapors, and non-condensable gases, wherein: The activator comprises water or carbon dioxide, and the condensable vapor and non-condensable gas are introduced into the vapor stream. said mechanically conveying; removing at least a portion of said vapor stream from said at least one indirectly heated reaction zone. and generating a separated steam stream. at least a portion of the separated vapor stream or a thermally treated form thereof, or to the at least one indirectly heated reactor prior to the step of conveying the feedstock to recirculating the gas to the gas inlet of the zone; and extracting the solid from the at least one indirectly heated reaction zone as biogenic activated carbon. and recovering at least a portion of the product.

2. Prior to the mechanical conveying step, the feedstock contains a maximum of 12% by weight moisture. The method according to claim 1.

3. Prior to the mechanical conveying step, the feedstock contains a maximum of 6% by weight moisture. The method according to item 2.

4. Prior to the mechanical conveying step, the feedstock contains a maximum of 2% by weight moisture. Item 3. The method according to item 3.

5. No water is added to the feedstock, and the activator contains water, and 2. The method of claim 1, wherein the water is derived from moisture contained in the feedstock.

6. The method of claim 1 , wherein the activating agent comprises both water and carbon dioxide.

7. The ratio of the water to the carbon dioxide is optimized, thereby increasing the activation of the solids. The method according to claim 6 .

8. At least one of the at least one indirectly heated reaction zones comprises at least 2. The method of claim 1, wherein both are maintained at a reaction temperature of from 700° C. up to 900° C.

9. All of said at least one indirectly heated reaction zones are heated to a maximum temperature of 950° C. The process of claim 1 wherein the reaction is maintained at a reaction temperature.

10. The removing step comprises removing the condensable vapor from the at least one indirectly heated reaction zone. The method of claim 1 , further comprising removing at least a portion of the gas.

11. The step of removing comprises removing said vapor stream from said at least one indirectly heated reaction zone. The method of claim 10, comprising removing all of the

12. At least a portion of the separated vapor stream is passed through the feed stream prior to the mechanical conveying step. re-adding to the feed or to the gas inlet of the at least one indirectly heated reaction zone; 10. The method of claim 1, further comprising thermally treating the recycled material prior to recycling.

13. The separated vapor stream or a thermally treated form thereof may comprise up to 1 wt. % in total of 10. The method of claim 1, including carbon monoxide and VOC content.

14. The recycling step further comprises adding water to the separated vapor stream or a thermally treated form thereof. The method of claim 1 further comprising heating.

15. The recycling step comprises the step of recycling at least one selected from the group consisting of water, carbon dioxide, nitrogen, and oxygen. said separated vapor stream or its thermally treated product by introducing at least one species The method of claim 1 further comprising adjusting the gas composition of the mixed form.

16. After the recycling step, the separated vapor stream is at least 0% and up to 100% water. , at least 0% to a maximum of 100% carbon dioxide, at least 0% to a maximum of 100% nitrogen 16. The method of claim 15, comprising:

17. After the recycling step, the separated vapor stream is 16. The method of claim 15, comprising:

18. After the recycling step, the separated vapor stream is 17. The method of claim 15 or claim 16, comprising carbon dioxide.

19. After the recycling step, the separated vapor stream is at least 5% and up to 100% acid.

17. The method of claim 15 or claim 16, comprising the steps of:

20. After the recycling step, the separated vapor stream is at least 70 wt. % nitrogen and up to 17. The method of claim 15 or claim 16, comprising 100% nitrogen.

21. at least a portion of the separated vapor stream or a thermally treated form thereof is passed through a delivery system. The method further comprises introducing the at least one indirectly-activated endothelial cell into a delivery system, the delivery system comprising: configured to mechanically feed the feedstock to a first one of the heated reaction zones. The method of claim 1 ,

22. At least a portion of the activator may be added to the separated vapor stream or a thermally treated version thereof. The method of claim 1 , wherein the morphology is derived from the

23. The carbon content of the biogenic activated carbon produced by the method of claim 1 is The method includes the steps of providing, mechanically transporting, removing, and recovering, greater than the carbon content of biogenic activated carbon produced by a process that does not include a recycle step; The method of claim 1.

24. The surface area of ​​the biogenic activated carbon produced by the method of claim 1 is The method includes the steps of:

10. The surface area of ​​biogenic activated carbon produced by a process that does not include a ring step. The method described above.

25. The iodine value of the biogenic activated carbon produced by the method of claim 1 is The method includes the steps of: providing, mechanically transporting, removing, and recovering, but the recycling step The iodine value of the biogenic activated carbon produced by a method that does not include a recycling process is exceeded. Item 1. The method according to item 1.

26. The recovering step comprises recovering the at least one indirectly heated reactor as a biogenic activated carbon.

10. The method of claim 1 including recovering all of said solids from the reaction zone.

27. Additives are introduced before, during, or after at least one of the steps of claim 1. and the additive is magnesium, manganese, aluminum, nickel , iron, chromium, silicon, boron, cerium, molybdenum, phosphorus, tungsten, vanadium iron chloride, iron bromide, magnesium oxide, dolomite, dolomitic lime, fluorite, Fluorospar, bentonite, calcium oxide, lime, sodium hydroxide, potassium hydroxide Um, hydrogen bromide, hydrogen chloride, sodium silicate, potassium permanganate, organic acids, iodine , an iodine compound, and combinations thereof. How to.

28. The biogenic activated carbon is characterized by an iodine value of at least 500 and up to 2250. The method according to claim 1 .

29. The biogenic activated carbon has a molecular weight of at least 1000 m ２ / g of surface area.

2. The method according to claim 1.

30. 10. The method of claim 1, wherein the biogenic activated carbon comprises graphene.

31. 10. The method of claim 1, wherein the biogenic activated carbon is responsive to an externally applied magnetic field. 。

32. The electrical conductivity of the biogenic activated carbon exceeds the electrical conductivity of the starting carbon-containing feedstock. The method of claim 1 .

33. the electrical capacity of the biogenic activated carbon exceeds the electrical capacity of the starting carbon-containing feedstock; The method of claim 1.

34. 1. A method for producing graphene, the method comprising: Providing a starting carbon-containing feedstock comprising biomass; Mechanically conveying the feedstock in at least one indirectly heated reaction zone. and countercurrently contacting the feedstock with a vapor stream comprising an inert gas and an activator, thereby generating solids, condensable vapors, and non-condensable gases, wherein: The activator comprises water or carbon dioxide, and the condensable vapor and non-condensable gas are introduced into the vapor stream. said mechanically conveying; removing at least a portion of said vapor stream from said at least one indirectly heated reaction zone. and generating a separated steam stream. at least a portion of the separated vapor stream or a thermally treated form thereof, or to the at least one indirectly heated reactor prior to the step of conveying the feedstock to recirculating the gas to the gas inlet of the zone; and extracting the solid from the at least one indirectly heated reaction zone as biogenic activated carbon. Recovering at least a portion of the The separated vapor streams or or introducing at least a portion of the thermally treated form thereof into a reactor. method.

35. drying the feedstock, thereby removing at least a portion of the moisture therefrom; The method of claim 1 , further comprising:

36. Additives are introduced before, during, or after at least one of the steps of claim 1. Further including: The additive may be an acid, a base, a salt, a metal, a metal oxide, a metal hydroxide, a metal halide, or an iodide. iodine, an iodine compound, or a combination thereof. The method described.

37. The graphene is subjected to the steps of providing, mechanically conveying, removing, and The amount of graphene produced by the method including the recovery step but not including the recycling step. The method of claim 30, wherein the amount is greater than

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