Patent Publication Number: US-2013232863-A1

Title: Method and system for the torrefaction of lignocellulosic material

Description:
RELATED APPLICATION 
     This application is a divisional of U.S. application Ser. No. 12/832,614, filed on Jul. 8, 2010, and claims the benefit of priority to U.S. Provisional App. No. 61/235,114, filed on Aug. 19, 2009, the entirety of each of which is incorporated by reference. 
    
    
     BACKGROUND OF THE INVENTION 
     The present invention generally relates to systems and methods relating to the torrefaction of lignocellulosic material. 
     Torrefaction refers to the thermal treatment of wood, usually in an inert atmosphere, at relatively low temperatures of 225 to 300° C. Torrefaction generally results in a fuel with increased energy density relative to the mass, by the decomposition of reactive hemicellulose content of the wood. 
     Wood generally contains hemicellulose, cellulose, and lignin. In an aspect, the goal of torrefaction is to remove moisture and low weight organic volatile components from the wood. Torrefaction may also depolymerize the long polysaccharide chains of the hemicellulose portion of the wood and produce a hydrophobic solid product with an increased energy density (on a mass basis) and improved grindability. Because of the change in the chemical structure of the wood after torrefaction, it can be suitable for use in coal fired facilities (torrefied wood or biomass has the characteristics that resemble those of low rank coals) or can be compacted into high grade pellets replacing standard wood pellets. 
     Torrefaction has developed over the last few decades as a possible method to turn wood based biomass into a viable addition to the spectrum of energy products. Although there has been much research into the compositional changes that occur in the biomass (wood) while undergoing torrefaction, commercial processes are not well developed. The torrefaction method and system put forth here has been developed to meet the commercial need for a viable torrefaction process. Other torrefaction processes are described in: U.S. Patent Pub. No. 2008/0223269, in which conduction heat is used to achieve torrefaction; U.S. Pat. No. 4,787,917, in which torrefied wood is formed into sticks of unbarked wood; and PCT Pub. No. WO 2005/056723, in which a continuous method and system produces torrefied biomass from raw material (organic material and originate from forestry or other agriculture and material of fossil nature or mixture—lignocellulose). 
     BRIEF DESCRIPTION OF THE INVENTION 
     Torrefaction of the wood material typically produces three products: a solid product of dark color which can be further processed to pellets or used directly as biomass fuel; an acidic phase comprised of condensable organics (including, but not limited to acetic acid, formic acid, acetone, furfural); and gases such as carbon monoxide or carbon dioxide. In an aspect the process may be a low temperature, low oxygen pyrolysis process where the easy to remove compounds having the lowest heat and energy values are removed. 
     In an aspect of this process, approximately 30% of the mass is burned off while losing only 10% of the energy value, that is to say the remaining solid mass (approximately 70% of the original material mass) contains 90% of the heat value originally present. Torrefaction may occur in a pressurized reactor and a temperature of 220-300° C. where there is direct contact of the raw material/biomass (lignocellulosic material), which has been previously dried to remove up to approximately 95% of the moisture initially present in the biomass, with hot gas (relatively oxygen free gas). Heating of the dried biomass in the torrefaction reactor may remove the remaining water from the biomass. 
     In an aspect, there is a system for the torrefaction of lignocellulosic material. The system may include: a dryer for drying lignocellulosic material adapted to remove at least of a portion of moisture contained within the lignocellulosic material; a torrefaction reactor adapted to operate at a pressure between 1 and 50 bar and at a temperature between 100 and 1000° C., wherein the torrefaction reactor generates torrefied biomass and a torrefaction gas from the lignocellulosic material; a first recycle loop adapted to recycle torrefaction gas back to the torrefaction reactor; a cooler adapted to cool torrefied biomass, wherein the cooler is adapted to operate in a substantially oxygen-free environment; a cyclone adapted to separate the cooled torrefied biomass from an inert gas; a second recycle loop adapted to recycle the inert gas from the cyclone to the cooler and to provide the inert gas to the torrefaction reactor; and a supply line adapted to supply inert gas for addition to the cooler. The system may be adapted to use the inert gas as a medium for transferring heat among the torrefaction reactor and the cooler. 
     In another aspect, there is a method for the torrefaction of lignocellulosic material comprising the steps of: drying lignocellulosic material to remove at least a portion of the moisture contained within the lignocellulosic material; reacting the dried lignocellulosic material at a pressure between 1 and 50 bar and at a temperature between 100 and 1000° C. in a torrefaction reactor to generate torrefied biomass and torrefaction gas; recycling at least a portion of the torrefaction gas back to the torrefaction reactor; cooling the torrefied biomass in the cooler operating in a substantially oxygen-free environment; separating the torrefied biomass and an inert gas in a cyclone; recycling a portion of the inert gas separated in the cyclone to the cooler and recycling a portion of the inert gas separated in the cyclone to the torrefaction reactor; supplying make-up inert gas to the cooler. The method may use the inert gas as a medium for transferring heat among the torrefaction reactor and the cooler. 
    
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         FIG. 1  is a schematic flowchart illustrating an embodiment of the present invention. 
     
    
    
     DETAILED DESCRIPTION OF THE INVENTION 
       FIG. 1  schematically illustrates a commercial-scale facility capable of torrefaction of biomass (lignocellulosic material). The embodiment of  FIG. 1  takes advantage of heat from the process while maintaining an oxygen-free (i.e., substantially oxygen-free) environment, which is beneficial for safe, efficient operation. 
     In the illustrated process, biomass material is fed via conduit  1  to a drying device  2 , which is any conventional or nonconventional drying device capable of removing between 85 and 98% of the moisture present in the biomass. In the illustrated drying device  2 , the moisture present in the biomass is removed by energy supplied via hot gas  23 . The dryer may remove a sufficient amount of moisture such that an absolute moisture content of the dried lignocellulosic material is less than 15% of the total weight of the lignocellulosic material. In the depicted embodiment, hot gas in conduit is the result of flue gas in conduit  9  from the combustion unit  8  after the flue gas has been cooled slightly by an indirect heat exchanger  20 . Heat exchanger  20  facilitates recycling the energy in the hot flue gas  9  back to the torrefaction reactor  5  via conduit  19  for use in heating the reactor  5 . 
     The drying gas fed to dryer  2  via conduit  23  may be at a temperature of up to 1,000° C. to allow for drying to the desired residual moisture level. The dried biomass is then fed via conduit  3  and rotary valve  4  to the inlet to a pressurized reactor  5  (also called torrefaction reactor). The torrefaction reactor  5  may operate at between  5  and  20  bar, and at an operating temperature of about 220-300° C. In other embodiments, the pressure may range from 1 to 50 bar (and all subranges therebetween), and the temperature may range between 100 and 1000° C. (and all subranges therebetween). 
     To raise the temperature of the dried biomass material (e.g., from 100 to 300° C.), heat is provided from heated reactor gas supplied via conduit  19 . The heated reactor gas is comprised of a portion of the torrefaction gas (gas produced in the torrefaction reactor  5 ) which exits torrefaction reaction  5  via conduit  6  and which is recycled to the torrefaction reactor  5  (as recycled torrefaction gas via conduit  7 ) and a portion of the cyclone nitrogen rich gas via conduit  18 . 
     The portion of the recycled torrefaction gas which is recycled to the torrefaction reactor  5  and any additional nitrogen rich gas can be heated in an indirect heat exchanger  20  by flue gas or other heating means in conduit  9  from the combustion unit  8  prior to use in the torrefaction reactor  5 . A portion of the torrefaction gas (e.g., the portion in conduit  21 ) produced in the torrefaction reactor  5  can be sent to the combustion unit where the torrefaction gas is mixed with oxygen containing gas fed via conduit  12  from the Pressure Swing Adsorption (PSA) plant  11  and/or combustion air and/or with utility fuel fed via conduit  22  (if needed) to produce combustion flue gas exiting via conduit  9  from combustion unit  8 . 
     The combustion flue gas may be used as the heat source for the indirect heat exchanger  20  to heat the reactor gas provided to the torrefaction reactor  5  via conduit  19 . The cooler combustion flue gas of stream  23  may be used in the drying unit  2  to dry the incoming biomass. The drying flue gas of conduit  24  produced from the drying process may be sent to further processing prior to disposal to the atmosphere or other acceptable disposal. 
     Torrefied biomass exiting via stream  25  from the torrefaction reactor  5  at a temperature of about 220 to 300° C. may be fed to a rotary valve  26  at the inlet to the fluidbed cooler  29  (or other direct contact cooler). The fluidbed cooler  29  may be a combination indirect cooler, using water as the cooling medium, and direct cooler, using cooled nitrogen rich stream  17  or any other inert gas from heat exchanger  16  and make-up nitrogen from the PSA (or other gas separation type equipment) plant  11  or any other inert gas to cool the torrefied biomass entering the fluidbed cooler  29  via stream  25  to about 90° C. in an oxygen free or near oxygen free environment. The cooled torrefied biomass may be discharged from the fluidbed cooler  29  via a rotary valve  30  (or similar device to assure the fluidbed cooler  29  operates in an oxygen-free, or substantially oxygen-free, environment). Cool torrefied biomass in stream  40  discharged from the fluidbed cooler  29  may be mixed with torrefied biomass solids stream  35  separated in the cyclone  32  (discharged through rotary valve  33  or other such equipment to ensure an oxygen-free or near oxygen-free environment is maintained in the cyclone  32 ) to produce a stream  37  for further processing in a pelletizing unit  38  or other product handling process for compacting or packaging the torrefied biomass solids. 
     The fluidbed cooler  29  may operate at near atmospheric pressure (e.g., the cooler may operate at a slight vacuum or slightly above atmospheric pressure) and may use indirect cooling from cooling water (noted as Cooling Water Supply (CWS)  27  and Cooling Water Return (CWR)  28 ) as well as direct cooling from the nitrogen rich gas in stream  17 . The nitrogen rich gas in stream  17  may contain a portion of cyclone nitrogen rich gas in stream  36  combined with make-up nitrogen  13 . Heat exchanger  16  can be supplied with cooling water as the indirect cooling medium or other available cooling material. 
     Fluidbed cooler gas in stream  31  from the fluidbed cooler  29  may be sent to cyclone  32  where cooled gas is separated from any entrained solids. The cooled gas in stream  34  may then be split into two or more portions. For example, cyclone nitrogen gas stream  34  may be split into two portions: (i) stream  18  which can be sent to heat exchanger  20  in the heating loop around the torrefaction reactor for mixing with stream  7  to feed the torrefaction reactor  5  and (ii) stream  36  which is fed to heat exchanger  16  to be cooled. 
     Air in conduit  10  may be provided to PSA Plant  11  where two gas streams are produced: make-up nitrogen stream  13  (a stream rich in nitrogen with little or no oxygen) and an oxygen rich stream  12  which is used together with utility fuel in the combustion unit. 
     While the description provided uses nitrogen as the gas in the heating and cooling loops where oxygen-free, or substantially oxygen-free, environments may be employed avoid explosive mixtures, any inert gas (for example argon or carbon dioxide, but nitrogen is preferred) can be used in place of nitrogen. The inert gas (e.g., nitrogen) is used in this process as a “carrier” gas, meaning the inert gas carries the heat needed in the torrefaction reactor and from the fluidbed cooler. Additionally, while the process may use a PSA Plant to separate nitrogen from air, any other method of separating nitrogen from air can also be used and is not a critical feature of this invention. It is also within the scope of the invention to use any source of nitrogen or other inert gas. 
     In the embodiment of  FIG. 1 , moreover, cooling water is described as the cooling medium in the indirect cooling services. In other embodiments, the cooling medium may be some medium other than water without impacting the important technical features of this process. That is, any fluid capable of effectively cooling may be employed. 
     In an aspect, a notable feature of this process is the ability to use nitrogen rich gas from the cyclone (which would otherwise be purged from the system) as part of the reactor gas for the torrefaction step. By using this nitrogen rich gas a balance can be established in the both the cooling loop and the heating loop with minimal addition of make-up nitrogen. This also means the torrefaction gas composition is used to set the operating conditions of the combustion unit by controlling the ratio of gas (via conduit  21 ) from the reactor going to the combustion unit versus gas (via conduit  6 ) produced by the reactor. This ratio—which may be expressed in either volumetric or molar terms—then influences the nitrogen needed for make-up as well as the quantity of utility fuel required. It is also preferable that the streams being recycled in both the heating and cooling loops remain oxygen-free or substantially oxygen-free. In an aspect, the described process of  FIG. 1  may provide optimum equipment sizing, thereby saving capital investment, as well as improves the impact on the environment of the products from the process. 
     While the invention has been described in connection with what is presently considered to be the most practical and preferred embodiment, it is to be understood that the invention is not to be limited to the disclosed embodiment, but on the contrary, is intended to cover various modifications and equivalent arrangements included within the spirit and scope of the appended claims.