• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The present invention is directed to production of granular carbon, prepared from lignin. The process comprises the steps of providing agglomerated lignin, heating the agglomerated lignin to obtain thermally stabilized lignin and subjecting the thermally stabilized agglomerated lignin to heat treatment to obtain granular carbon.
    公开号:SE2050699A1
    申请号:SE2050699
    申请日:2020-06-11
    公开日:2021-12-12
    发明作者:Dimitri Areskogh；Stephan Walter；Vilhelm Olsson
    申请人:Stora Enso Oyj；
    IPC主号:
    专利说明:

    PROCESS FOR PRODUCING CARBON FROM HEAT TREATEDLIGNIN Field of the invention The present invention is directed to production ofgranular carbon, prepared from lignin.
    Background Carbon enriched materials can be used for various end-uses, such as bio- chars, activated carbons and electrode materials. ln conventional processes of converting biomass into carbon-enrichedintermediates, powders are often avoided. Direct use of lignin, as a finepowder, is not suitable since it exhibits undesired thermoplastic behaviour.
    During thermal conversion of lignin powder into carbon-enrichedintermediates, lignin undergoes plastic deformation/melting, aggressiveswelling and foaming. Combined with the strong tendency for dust formationduring handling, this severely limits processability of lignin in industriallyrelevant scale, in terms of equipment dimensioning and process throughput as well as need of intermediate processing. lt would be desirable to use lignin as an alternative to fossil-based carbon- containing materials. Lignin, an aromatic polymer is a major constituent in e.g. wood, being the most abundant carbon source on Earth second only tocellulose. ln recent years, with development and commercialization oftechnologies to extract lignin in a highly purified, solid and particularized form from the pulp-making process, it has attracted significant attention as a possible renewable substitute to primarily aromatic chemical precursorscurrently sourced from the petrochemical industry.
    However, to use lignin as a raw material for economical production of carbonenriched materials, such as bio-chars, activated carbons and electrodematerials, it would be necessary to avoid that the lignin undergoes plastic deformation/melting, aggressive swelling and foaming upon heating.
    Summary of the invention lt has surprisingly been found that lignin which has undergone agglomerationinto macroscopic particles and been thermally stabilized can be heat treatedwith retained shape and dimension, avoiding melting/swelling deformation.Thereby, production of carbon enriched materials for various end-uses, suchas bio-chars and activated carbons, is facilitated and the process avoidsdusting. lt has been found that a previously agglomerated lignin which hasbeen thermally stabilized will continue to retain its dimensional integrity duringfurther processing into carbon-enriched products. ln addition, the obtainedgranular carbon is essentially spherical and therefore suitable for example foruse in filters and other applications in which essentially spherical granular carbon is advantageous.
    The present invention is directed to a process to produce granular carbon, said process comprising the steps of a) providing agglomerated lignin having a particle size distributionsuch that at least 80 wt-% of the agglomerates have a diameterwithin the range of from 0.2 mm to 5.0 mm; b) heating the agglomerated lignin to a temperature in the range offrom 140 to 250°C for a period of at least 1.5 hours, to obtain thermally stabilized agglomerated lignin; c) subjecting the thermally stabilized agglomerated lignin to heattreatment at one or more temperatures in the range of from 300°Cto 1500°C, wherein the heat treatment is carried out for a total time of from 30 minutes to 10 hours, to obtain granular carbon.
    Preferabiy the particle size distribution of the agglomerated lignin obtained instep b) is such that at least 80 wt-% of the agglomerates have a diameter within the range of from 0.2 mm to 5.0 mm.
    Preferably, the agglomerated lignin used in step a) is produced by i. providing lignin in the form of a powder, wherein the particle sizedistribution of the lignin in the form of a powder is such that at least80 wt-% of the particles have a diameter less than 0.2 mm and amoisture content of less than 45 wt-%; ii. compacting the lignin powder of step i);crushing the compacted lignin obtained in step ii); iv. optionally sieving the compacted lignin obtained in step iii) toremove particles having a particle diameter below 100 um, therebyobtaining the agglomerated lignin having a particle size distributionsuch that at least 80 wt-% of the particles have a diameter within the range of from 0.2 mm to 5.0 mm.
    Preferably, the product obtained in step iii is subjected to sieving inaccordance with step iv. Preferably, in step iv, the sieving is carried out suchthat the agglomerated lignin obtained has a particle size distribution such thatat least 80 wt-% of the particles have a diameter in the range of from 0.5 mm to 2.0 mm, more preferably 0.5 mm to 1.5 mm.
    The compaction may be carried out without addition of any additives to thematerial to be compacted. ln the context of the present invention, an additiveis a substance that is added to the process to improve adhesion between the lignin particles. Thus, additives are substances that are added, but that are not present in the lignin that is the starting material in step a). Thus, neithermoisture, such as water, nor other components already present in the ligninthat is the starting material in step i), are considered additives in the context of the present invention.
    Detailed description lt is intended throughout the present description that the expression "lignin"embraces any kind of lignin, e.g. lignin originated from hardwood, softwood orannular plants. Preferably the lignin is an alkaline lignin generated in e.g. theKraft process. Preferably, the lignin has been purified or isolated before beingused in the process according to the present invention. The lignin may beisolated from black liquor and optionally be further purified before being usedin the process according to the present invention. The purification is typicallysuch that the purity of the lignin is at least 90%, preferably at least 95%, morepreferably at least 98%, most preferably at least 99%, 99.5% or 99.9%. Thus,the lignin used according to the process of the present invention preferablycontains less than 10%, preferably less than 5%, more preferably less than2% impurities. The lignin may be separated from the black liquor by using theprocess disclosed in WO2006031175. ln the context of the present invention, the diameter of a particle is theequivalent spherical diameter of the particle, if the particle is not spherical.The equivalent spherical diameter is the diameter of a sphere of equivalent volume.
    Preferably, the agglomerated lignin is prepared by a process comprising the steps of i. providing lignin in the form of a powder, wherein the particle sizedistribution of the lignin in the form of a powder is such that at least 80 wt-% of the particles have a diameter less than 0.2 mm and amoisture content of less than 45 wt-%; ii. compacting the lignin powder of step i); iii. crushing the compacted lignin obtained in step ii); iv. optionally sieving the compacted lignin obtained in step iii) toremove particles having a particle diameter below 100 um, therebyobtaining the agglomerated lignin having a particle size distributionsuch that at least 80 wt-% of the particles have a diameter in therange of 0.2 mm to 5.0 mm, preferably from 0.2 mm to 2.0 mm, more preferably from 0.5 to 1.5 mm.
    Preferably, the lignin in powder form is dried before compaction. The drying ofthe lignin is carried out by methods and equipment known in the art. Thelignin in powder form used in step i) has a moisture content of less than 45wt-%. Preferably, the moisture content of the lignin before compactionaccording to the present invention is less than 25 wt-%, preferably less than10 wt-%, more preferably less than 8 wt-%. ln one embodiment, the moisturecontent of the lignin before compaction according to the present invention isat least 1 wt-%, such as at least 5 wt-%. The temperature during the drying ispreferably in the range of from 80°C to 160°C, more preferably in the range offrom 100°C to 120°C.
    The lignin powder obtained after drying has a wide particle size distributionranging from 1 um to 2 mm which is significantly skewed towards themicrometer range, meaning that a significant proportion of the particles has adiameter in the range of 1 to 200 micrometers.
    The compaction of the lignin is preferably carried out by roll compaction.
    The roll compaction of lignin can be achieved by a roller compactor toagglomerate the lignin particles. ln the compaction step, an intermediate product is generated. Here, the finelignin powder is usually fed through a hopper and conveyed by means of ahorizontal or vertical feeding screw into the compaction zone where thematerial is compacted into flakes by compaction rollers with a defined gap. Bycontrolling the feeding screw speed, the pressure development in thecompaction zone, flakes with uniform density can be obtained. The pressuredevelopment in the compaction zone can preferably be monitored andcontrolled by the rotational speed of the compaction rolls. As the powder isdragged between the rollers, it enters what is termed as the nip area wherethe density of the material is increased and the powder is converted into aflake or ribbon. The rolls used have cavities. The depth of each cavity used inthe roll compaction is from 0.1 mm to 10 mm, preferably from 1 mm to 8 mm,more preferably from 1 mm to 5 mm or from 1 mm to 3 mm. The specificpress force exerted during the compaction may vary depending on theequipment used for compaction, but may be in the range of from 1 kN/cm to100 kN/cm. Equipment suitable for carrying out the compaction are known in the art.
    After compaction, crushing is preferably carried out. ln the crushing step, the intermediate product from the compaction step issubjected to crushing or grinding, such as by means of rotary granulator,cage mill, beater mill, hammer mill or crusher mill and/or combinations thereof. During this step, a further intermediate product is generated.
    After crushing, the crushed material is preferably subjected to a sieving step,to remove fine material. ln addition, large material, such as agglomerateshaving a diameter larger than 5.0 mm, may be removed and/or recirculated back to the crushing step. ln the sieving step, the intermediate product from the crushing step isscreened by means of physical fractionation such as sieving, also referred to as screening, to obtain a product which is agglomerated lignin with a defined particle size distribution set by the porosity of the sieves or screens in thisstep. The sieve or screen is selected such that most particles having adiameter below 100 (or 500) um pass through the screen and are rejectedand preferably returned to the compaction step, whereas most particleshaving a diameter above 100 (or 500) um are retained and subjected to thesubsequent heating step of the process according to the present invention.The sieving may be carried out in more than one step, i.e. the sieving can becarried out such that the crushed material from the crushing step passes sequentially through more than one screen or sieve. ln one embodiment of the roll compaction, the rolls configuration is such thatthe first roll has an annual rim in such configuration so that the powder in the nip region is sealed in the axial direction along the roller surface. ln one embodiment, the roll configuration is such that the nip region is sealedin the axial direction along the roller surface with a static plate.By ensuring that the nip region is sealed, loss of powder at the axial ends of the rollers is minimized as compared to entirely cylindrical nip rollers. lt is particularly beneficial to carry out the compaction according to thepresent invention on a material that is essentially only lignin, i.e. in theabsence of additives, since that makes the use of the compacted producteasier, due to the absence of binders or other components that couldotherwise negatively influence the application in which the compacted, crushed and optionally sieved lignin is supposed to be used.
    The agglomerated lignin preferably has a bulk density in the range of from 0.5g/cm3 to 0.7 g/cm3, more preferably from 0.5 g/cm3 to 0.6 g/cm3. The ligninpowder, prior to agglomeration, preferably has a bulk density in the range offrom 0.3 g/cm3 to 0.4 g/cm3.
    The agglomerated lignin has a particle size distribution such that at least 80 wt-% of the particles have a diameter in the range of from 0.2 mm to 5.0 mm.
    Preferably, the particle size distribution is such that at least 90 wt-%, morepreferably at least 95 wt-%, of the particles have a diameter in the range offrom 0.2 mm to 5.0 mm. More preferably, at least 90 wt-%, more preferably atleast 95 wt-%, of the particles have a diameter in the range of from 0.5 mm to 2 mm.
    The step of heating the agglomerated lignin to produce thermally stabilizedagglomerated lignin can be carried out continuously or in batch mode. Theheating can be carried out using methods known in the art and can be carriedout in the presence of air or completely or partially under inert gas. Preferably,the heating is carried out in a rotary kiln, moving bed furnace or rotary hearth furnace.
    The heating to produce thermally stabilized agglomerated lignin is carried outat such that the agglomerated lignin is heated to a temperature in the range offrom 140 to 250°C, preferably from 180 to 230°C. The heating is carried outfor at least 1.5 hours, i.e. the residence time of the agglomerated lignin insidethe equipment used for the heating is at least 1.5 hours. Preferably, theheating is carried for less than 12 hours. The heating may be carried out atthe same temperature throughout the entire heating stage or may be carriedout at varying temperature, such as a stepwise increase of the temperature orusing a temperature gradient. More preferably, the heating is carried out suchthat the agglomerated lignin is first heated to a temperature of from 140 to175°C for a period of at least one hour and subsequently heated to a temperature of from 175 to 250°C for at least one hour.
    The colour of the thermally stabilized agglomerated lignin is different from thecolour of the agglomerated lignin prior to thermal stabilization. The colour canbe determined for example by using a spectrophotometer and reported inaccordance with the CIELAB colour space. ln the CIELAB colour space,colour can be reported as lightness (L*), green-red (a*) and blue-yellow (b*)components. Preferably, the lightness (L*) of the surface of the thermally stabilized agglomerated lignin is in the range of from 37 to 39, preferably in the range of from 37 to 38. The lightness of the surface of the agglomeratedlignin prior to thermal stabilization is above 44, such as in the range of from44 to 52. Thus, the Iightness of the agglomerated lignin decreases during thermal stabilization.
    The thermally stabilized agglomerated lignin obtained in step b) is subjectedto heat treatment at one or more temperatures in the range of from 300°C to1500°C, wherein the heat treatment is carried out for a total time of from 30 minutes to 10 hours, to obtain granu|ar carbon.
    Preferabiy, the heat treatment comprises a preliminary heating step,preferably followed by a final heating step. The preliminary heating step ispreferably carried out at a temperature of between 300 and 800°C, such asbetween 500 and 700°C under inert atmosphere, preferably nitrogenatmosphere. The duration of the preliminary heating step is at least 30minutes and preferably less than 10 hours. The preliminary and final heatingsteps may be carried out as discrete steps or as one single step in directsequence. The surface area of the product obtained after the preliminaryheating step is typically in the range of from 300 to 700 m2/g, measured asBET using nitrogen gas.
    The final heating step is preferably carried out at a temperature between 800°C and 1500°C, under inert atmosphere, preferably nitrogen atmosphere.
    The duration of final heating step is at least 30 minutes and preferably lessthan 10 hours. After the final heating step, the surface area of the productobtained is typically 10 m2/g or less.
    Preferabiy, the heat treatment is carried out stepwise. Preferabiy, thepreliminary heating starts at about 300°C and is subsequently increased toabout 500°C. The final heating step is preferably carried out between 900°Cand 1300°C, such as at about 1000°C.
    The heat treated material, i.e. the granular carbon which is the product of stepc), is useful for example as bio-char, or as precursor to activated carbon orelectrode material.
    The heat treated material, i.e. the granular carbon which is the product of stepc) preferably has a bulk density in the range of from 0.2 g/cm3 to 0.4 g/cm3.
    The colour of the granular carbon is different from the colour of the thermallystabilized agglomerated lignin prior. The colour can be determined forexample by using a spectrophotometer and reported in accordance with theCIELAB colour space. ln the CIELAB colour space, colour can be reported aslightness (L*), green-red (a*) and blue-yellow (b*) components. Preferably,the lightness (L*) of the surface of the granular carbon is in the range of from34 to 37, preferably in the range of from 34 to 36. Thus, the lightness of theagglomerated lignin decreases during step c). 11 Examples Example 1 Lignin powder from the LignoBoost process was agglomerated by means ofroller compaction into particles with a size distribution of 0.2 - 2 mm.
    The agglomerated lignin was heated to 200 °C for 12h. During this process,the agglomerated lignin did not exhibit any melting behaviour and completelyretained its original shape. Surprisingly it was found that the individualgranules did not fuse together and remained free flowing. The materialgradually darkened during the processing until it was completely black and free of smell.
    The thermally stabilized agglomerated lignin was subsequently heated at 500-1400°C under inert atmosphere. ln this process, the formed carbon granules were rounded in shape and remained free-flowing..
    Example 2 Lignin powder from the LignoBoost process was agglomerated by means ofroller compaction, then crushed and sieved into particles with a sizedistribution of 0.5 - 1.5 mm.
    The agglomerated lignin was placed inside a laboratory rotary furnace,heated to 160°C using air-flow for 2h, followed by heating up to 220°C for 1hDuring this process, the agglomerated lignin did not exhibit any meltingbehaviour. Surprisingly it was found that the individual granules did not fusetogether or to the reactor walls and remained free flowing. The material gradually darkened during the processing until it was completely black.
    The thermally stabilized agglomerated lignin was subsequently heated to 300-350°C for 1h, and then 500°C under inert atmosphere using nitrogen for 1h. 12 Finally, this material was heated up to 1000°C under nitrogen for 1h. The resulting carbon material remained in non-agglomerated granularform.
    Example 3 (Comparative Example) ln this experiment, thermal conversion of conventional lignin powder was carried out.
    Lignin powder from the LignoBoost process was heated to 200°C for up to12h. After the heating, it was found that the lignin had melted/fused into asolid black cake free of smell. ln view of the above detailed description of the present invention, othermodifications and variations will become apparent to those skilled in the art.
    However, it should be apparent that such other modifications and variations may be effected without departing from the spirit and scope of the invention.
    权利要求:
    Claims (13)
    [1] 1. A process to produce granular carbon from lignin, said processcomprising the steps of a) providing agglomerated lignin having a particle sizedistribution such that at least 80 wt-% of the agglomerateshave a diameter within the range of from 0.2 mm to 5.0 mm; b) heating the agglomerated lignin to a temperature in therange of from 140 to 250°C for a period of at least 1.5 hours,to obtain thermally stabilized agglomerated lignin; c) subjecting the thermally stabilized agglomerated lignin toheat treatment at one or more temperatures in the range offrom 300°C and 1500°C, wherein the heat treatment iscarried out for a total time of from 30 minutes to 10 hours, to obtain granular carbon.
    [2] 2. A process according to claim 1, wherein the agglomerated lignin usedin step a) is produced byi. providing lignin in the form of a powder, wherein the particle sizedistribution of the lignin in the form of a powder is such that at least80 wt-% of the particles have a diameter less than 0.2 mm and amoisture content of less than 45 wt-%; ii. compacting the lignin powder of step i); iii. crushing the compacted lignin obtained in step ii); iv. optionally sieving the compacted lignin obtained in step iii) toremove particles having a particle diameter below 100 um, therebyobtaining the agglomerated lignin having a particle size distributionsuch that at least 80 wt-% of the agglomerates have a diameter within the range of from 0.2 mm to 5.0 mm.
    [3] 3. The process according to claim 1 or 2, wherein step c) comprises apreliminary heating step, followed by a final heating step.
    [4] 4. The process according to claim 3, wherein the preliminary heating stepc) is carried out at a temperature of between 400 and 800°C for atleast 30 minutes.
    [5] 5. The process according to claim 4, wherein the preliminary heating stepis carried out in inert atmosphere.
    [6] 6. The process according to any one of claims 1-4, wherein the finalheating step is carried out at a temperature between 800°C and1500°C for at least 30 minutes.
    [7] 7. The process according to claim 6, wherein the final heating step iscarried out in inert atmosphere.
    [8] 8. The process according to any one of claims 1-7, wherein the CIELABlightness (L*) of the surface of the thermally stabilized agglomeratedlignin obtained in step b) is in the range of from 37 to 39.
    [9] 9. The process according to any one of claims 1-8, wherein the CIELABlightness (L*) of the surface of the granular carbon obtained in step c)is in the range of from 34 to 37.
    [10] 10.The process according to any one of claims 1-9, wherein the granularcarbon obtained in step c) has a bulk density in the range of 0.2 g/cm3to 0.4 g/cm3.
    [11] 11.The process according to any one of claims 1-10, wherein the lignin iskraft lignin.
    [12] 12.The process according to claim 11, wherein the purity of the lignin is atleast 98%.
    类似技术:
    公开号 | 公开日 | 专利标题
    EP2603454B2|2020-11-25|Ground expanded graphite agglomerates, methods of making, and applications of the same
    KR970073368A|1997-12-10|Method for preparing animal feed supplement based on fermentation broth
    RU2018121627A|2019-12-23|GRAIN CARBON MATERIAL OBTAINED FROM RENEWABLE RAW MATERIALS AND METHOD FOR PRODUCING IT
    SE1950320A1|2020-09-15|Process for producing agglomerated lignin
    US10773962B2|2020-09-15|Preparation method for binder-free, coal-based, briquetted activated carbon
    SE2050699A1|2021-12-12|Process for producing carbon from heat treated lignin
    US2476335A|1949-07-19|Purification of red phosphorus
    SE544157C2|2022-02-08|Process for producing thermally stabilized lignin
    US622054A|1899-03-28|Material for packing
    US4360487A|1982-11-23|Process for hot briquetting of organic solid materials
    US4102812A|1978-07-25|Production of carbon from coal granules prepared in a fluid energy mill
    US2219660A|1940-10-29|Production of calcium hypochlorite products
    CA2502652C|2012-01-31|Method for producing dust-free alkaline earth peroxides
    KR100770967B1|2007-10-30|A method for producing shaped inorganic cyanide bodies and briquets obtained by said method
    RU2073643C1|1997-02-20|Method for production of activated carbon
    RU2628606C1|2017-08-21|Method of manufacturing carbon material and carbon material
    JP2574686B2|1997-01-22|Method for producing mesocarbon microbeads
    JP6326953B2|2018-05-23|Coke oven coal charging method
    TW355180B|1999-04-01|A composition of an active carbon pellet and process for preparing of it
    JP4181238B2|2008-11-12|Granulation method of dithiocarbamate
    CN112556424A|2021-03-26|Method for reducing dust of high-temperature melting oxidation furnace and improving melting rate
    CA3117089A1|2020-05-07|Process for coal fine aggregation
    SU1700025A1|1991-12-23|Method of producing calcium carbonate base filler
    GB2196642A|1988-05-05|Agglomerated solid fuel briquettes
    RU2422363C1|2011-06-27|Method of producing granular potassium chloride
    同族专利:
    公开号 | 公开日
    WO2021250604A1|2021-12-16|
    SE544158C2|2022-02-08|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    FI126818B|2015-02-06|2017-06-15|Valmet Technologies Oy|Process for the treatment of lignin-based material|
    CN106966390B|2017-03-15|2018-12-04|北京林业大学|A kind of preparation method and products therefrom of alkali lignin matrix activated carbon|
    SE543284C2|2019-03-14|2020-11-17|Stora Enso Oyj|Process for producing agglomerated lignin|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    SE2050699A|SE544158C2|2020-06-11|2020-06-11|Process for producing carbon from heat treated lignin|SE2050699A| SE544158C2|2020-06-11|2020-06-11|Process for producing carbon from heat treated lignin|
    PCT/IB2021/055103| WO2021250604A1|2020-06-11|2021-06-10|Process for producing carbon from heat treated lignin|
    [返回顶部]