EP0037912B1 - Process and apparatus for chemical conversion of cellulose waste to glucose - Google Patents

Process and apparatus for chemical conversion of cellulose waste to glucose Download PDF

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Publication number
EP0037912B1
EP0037912B1 EP19810101951 EP81101951A EP0037912B1 EP 0037912 B1 EP0037912 B1 EP 0037912B1 EP 19810101951 EP19810101951 EP 19810101951 EP 81101951 A EP81101951 A EP 81101951A EP 0037912 B1 EP0037912 B1 EP 0037912B1
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EP
European Patent Office
Prior art keywords
reaction zone
continuously
cellulose
feeding
valve
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
EP19810101951
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German (de)
English (en)
French (fr)
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EP0037912A3 (en
EP0037912A2 (en
Inventor
Barry Rugg
Robert Stanton
Walter Brenner
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
New York University NYU
Original Assignee
New York University NYU
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from US06/131,340 external-priority patent/US4316747A/en
Priority claimed from US06/131,339 external-priority patent/US4316748A/en
Application filed by New York University NYU filed Critical New York University NYU
Priority to AT81101951T priority Critical patent/ATE15074T1/de
Publication of EP0037912A2 publication Critical patent/EP0037912A2/en
Publication of EP0037912A3 publication Critical patent/EP0037912A3/en
Application granted granted Critical
Publication of EP0037912B1 publication Critical patent/EP0037912B1/en
Expired legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
    • C13K1/00—Glucose; Glucose-containing syrups
    • C13K1/02—Glucose; Glucose-containing syrups obtained by saccharification of cellulosic materials

Definitions

  • the present invention relates to a process and an apparatus for the quasi-continuous or continuous chemical conversion of materials, and in particular to a process and an apparatus for the conversion of waste cellulose to glucose by acid hydrolyzation.
  • Acid hydrolysis of cellulose has been extensively studied for the better part of the century, particularly in connection with the manufacturing of ethanol from wood wastes. It has long been known that cellulose can be hydrolyzed in acid solutions and converted to its monomer, glucose, and the reaction has been experimentally investigated since this discovery. The reaction results from the fact that the monomers of cellulose are in anhydroglucose units, and that during hydrolyzation, a water ion is added to the cellulose monomer units to obtain the heavier molecular weight glucose.
  • the kinetically predicted sugar yields assume that the cellulose reactant has appropriate chemical reactivity for the acid hydrolysis.
  • the technical problems of cellulose hydrolysis are to a great extent due to the fact that this is not the case.
  • the lack of an adequate amount of chemical reactivity in cellulose is called lack of accessibility. This is related to the highly inert character and crystalline organization on a molecular level of the high molecular weight cellulose, and also the presence of lignin. Hydrogen-bonding almost certainly plays a very important role in the structure of cellulose, and may be a key factor in explaining its chemical inertness.
  • a process step is effected in such a cyclical or periodic manner so as to take on the resemblance of and sufficiently approximate a continuous process step so as to take on the attributes thereof and be considered continuous by any further process or apparatus elements downstream thereof.
  • a process and apparatus for the conversion of fibrous material to a derivative thereof and in particular for the continuous acid hydrolysis of cellulose to glucose is described in Chemical and Engineering News 57 No. 41, pages 19-20. It is based primarily upon a hydrolysis reactor which is capable of feeding, conveying and discharging hydrolyzable cellulosic materials continuously while maintaining appropriate temperatures and/ or pressures in the reaction zone thereof. Because this hydrolysis requires exposure of the reactor components to dilute acids at high temperatures and pressures, all materials of construction are advantageously resistent to corrosion especially in the reaction zone.
  • the hydrolysis reactor is a Werner and Pfleiderer ZDS-K 53 (53 mm) corotational two screw extruder which was selected because of its capaicity for conveying, mixing and extruding the required amounts of cellulosic feedstock.
  • the extruder allows accurate control of temperature, pressure, residence, time, etc. as a result of the further novel features of the present invention as explained hereinafter.
  • the extruder has the working elements of intermeshing twin screws which rotate in the same direction and which eliminate material build-up in the processing section and make feasible close control of residence time, etc., with intensive mixing.
  • the reactor was coupled with an appropriate feeding mechanism for cellulose slurries and a discharge system for reacted material, while maintaining the necessary elevated pressure and/or temperature in the reaction zone.
  • the feeding means included a steam jacked crammer feeder also produced by the Werner & Pfleiderer Corp. so as to maximize throughout with preheating as required.
  • hydropulped recycled newspaper feedstock is obtained in an aqueous slurry form approximately 10% solid content and is optionally irradiated with a dosage of 10 megarads.
  • This pulp feedstock is then introduced into the reactor by means of a slurry pump and crammer feeder and the waste cellulose is then conveyed with heating by the twin screws into the reaction zone where the required amount of steam and acid is introduced.
  • Hydrolysis then takes place at a predetermined temperature and pressure and the product is properly discharged.
  • the dynamic seal is achieved by the formation of a dynamic plug zone in the extruder, at the inlet end of the reaction zone.
  • the dynamic seal may be formed in the conventional manner, by utilizing a left handed screw thread in the conventional manner, by utilizing a left handed screw thread in the dynamic seal zone with right handed threads disposed downstream and upstream thereof.
  • An object of the present invention is to improve the above mentioned process and apparatus by effecting the dynamic seal by a plug formed by an unthreaded and radially recessed portion of the screws in the dynamic plug zone.
  • a further object of the present invention is to obtain a continuous discharge of the extruder by use of the continuously open valve which is continuously open in response to a preselected pressure in the reaction zone.
  • a still further object is to provide a process and apparatus capable of handling both wet and dry fixed inputs.
  • Fig. 1 shows the basic apparatus for carrying out the process according to the present invention.
  • the apparatus includes the Werner and Pfleiderer ZDS-K 53 twin screw extruder 120 having two corotational screws therein driven by a motor 121.
  • the housing includes a feed inlet in which the material to be converted is received.
  • dry solid fibrous material in the form of shredded paper, sawdust, etc. is fed into the extruder 120 by means of a screw feeder 110, which as shown in Fig. 2, continuously feeds the material into the extruder to be conveyed thereby.
  • the input of the dry fibrous material is illustrated, the material, in particular cellulose paper pulp or sawdust can be fed-in in a slurry form in an alternative form.
  • the extruder 120 includes a reaction zone 125 which is bounded on its inlet side by a dynamic seal zone 124 and a discharge valve 180 at its outlet side. Upstream of the reaction zone is the inlet portion or preheating zone 122a of twin screws 122 wherein the fibrous input is first received and thereby conveyed into the reaction zone.
  • a dewatering drain 123 is provided upstream of the dynamic seal.
  • the dewatering drain is not necessary since the liquid added thereto is just sufficient to act as a carrier or, in the case of hydrolysis to act as the reactant and therefore no water is lost as in the case of a slurry input. Water is added, as needed, in the preheating zone and with the acid through input port . 134.
  • the apparatus further includes means 130 for adding an acid catalyst comprising a tank 131 and a metering pump 132 which feeds the acid along pipe 133 into the acid input port 134 for the extruder housing.
  • the acid catalyst input port 134 is shown to be at the beginning of the reaction zone 125 so that the acid acts on the reactants during substantially the entire residence time of the reactants in the reaction zone.
  • the input position of the acid catalyst port 134 can be varied, depending upon the temperature in the reaction zone. At higher temperatures, the reaction will generally take place faster and thus the acid can be introduced into the reaction zone at a position closer to the outlet thereof.
  • steam supply means 140 are provided including steam pipe 141 and steam input port 142.
  • the steam may also be used as a supply of water for the hydrolysis cellulose upon its condensation in the reaction zone.
  • a pressure indicator port 151 which in conjunction with pressure indicator means 150 enables a monitoring of the elevated pressure within the reaction zone.
  • temperature input ports 143 are also provided to enable monitoring of the temperature within the various zones of the extruder assembly.
  • a pressure release valve 160 is provided at the outlet end of the reaction zone 125 to provide pressure relief when the pressure within the reaction zone exceeds acceptable limits.
  • the continuous discharge of the reactants from the extruder is effected by the discharge valve means 180 which discharges the reactants into the collection vessel 170 which has a gas vent 171 and a flushing drain 172.
  • the valving means 180 of the present invention for effecting a continuous discharge of the reactants in response to a predetermined pressure in the reaction zone 125 is illustrated.
  • the valving means 180 comprises a spherical valve body 181 which coacts with the flanges end of the extruder housing 127 having the valve aperture 126 therein.
  • the spherical valve body 181 is preferably a 2" valve body.
  • the valve body 181 is seated in a valve plate 182 which has means including spring 185 acting thereon to bias the valve body 181 into the closed position shown in Fig. 3.
  • the biasing is carried out by the use of four screws 183 which are fixed at one end into the flange portion 127 and have threaded portion 183a at the other end thereof. Fitted onto the threaded portions 183a, is plate 184 which is prevented from moving to the right in Fig. 4 by nuts 186 which are threadably engaged with the threaded portions 183a.
  • the valve assembly is sealed by the plate 187 which is screwed by screws 188 onto the housing 189 so that the only outlet of the discharge material through aperture 126 is through the outlet 190.
  • valve body 181 In use, when the pressure within the reaction zone 125 exceeds the force exerted on the valve body 181 by the spring 185, the valve body 181 is moved to the right as shown in Fig. 4 and the discharge passes through the aperture 126 and through the outlet 190. In a working apparatus, the pressure within the reaction zone will be continuously maintained so that after the initialization of the process, the valve body 181 will remain in the open position and the discharge will continually pass through valving means 180.
  • the pressure at which the valving means 180 will respond to be maintained in the continuously open position shown in Fig. 4 can be preset by use of the aforementioned nuts 186 which engage with the threded portions 183a.
  • the nuts 186 are turned clockwise to move the plate 184 to the left thereby increasing the force that the spring 185 exerts on the plate 182 and thereby the valve body 181. Accordingly, the pressure can be decreased by reversing the above-mentioned process.
  • Fig. 5 discloses in greater detail the means forming the dynamic seal zone 124 according to the present invention.
  • the dynamic seal zone 124 is formed by the use of a radially recessed unthreaded screw section 240 on each screw with optional left handed screw sections 124a upstream thereof and 124b downstream thereof.
  • the unthreaded radially recessed portions 240 with the optionally left handed screw thread portions 124a, 124b, when taken in conjunction with the right hand screw threaded portions 122a upstream thereof and 122b downstream thereof act to produce the dynamic plug which seals the reaction zone and prevents gases from escaping through the input, while enabling the fed in material to be conveyed thereby into the reaction zone.
  • the dynamic seal in conjunction with the valve means 180, maintains the elevated pressure and, where desirable, the elevated temperature in the reaction zone while enabling the screw elements to convey the fed in material into the reaction zone and out of the reaction zone and to enable the reaction process to take place therein.
  • Feed Material sawdust.
  • Screw Feeder Rate 150 pounds (68 kg) per hour dry.
  • Acid Sulfuric Acid 1.0% by weight introduced in at 120 pounds (54,36 kg) per hour in solution.
  • Machine Screw RP 300 RPM drive torque 85%.
  • Glucose conversion 50% based on available cellulose.
  • Reaction zone input 150 pounds (68 kg) per hour solid, 30 pounds (13,6 kg) per hour water, 120 pounds (54,36 kg) per hour acid solution.
  • Product output 50% solids including 50 pounds (22,6 kg) per hour glucose, 33 pounds (15 kg) per hour cellulose, 38 pounds (17,2 kg) per hour lignin, 24 pounds (10,9 kg) per hour hemi cellulose or decomposed products, 143 pounds (64,8 kg) per hour water, 12 lb. (5;43 kg) acid.
  • Screw configuration total length 2250 mm preplug feed zone 630 mm of 30 mm pitch elements conveying material, 30 mm forward per revolution.
  • Plug zone 90 mm long with two 30 mm 90 mm left hand pitch elements and a 30 mm unthreaded element therebetween.
  • Reaction zone 1590 mm long with 45 mm pitch stainless steel elements Reaction zone 1590 mm long with 45 mm pitch stainless steel elements.
  • Discharge valve 2" ball valve with a pressure setting of 420 psi (2,89 x 10 6 Pa).
  • the process parameters of the invention can vary within a wide degree as is set forth hereinafter.
  • the feed material for wet feeds can have a consistency of 5% to 50% slurry with a limited viscosity and any cellulose containing material such as paper pulp, wood pulp, waste pulp, pulped municipal solid waste etc. can be used.
  • the feed rate can vary from 100 pounds (45,3 kg) per hour to 900 pounds (407,7 kg) per hour depending upon the consistency of the feed material and the RPM of the screw elements.
  • reaction temperature can vary from 350°F to 545°F (176°C to 285°C) at 1000 psi (6,89 x 10 6 Pa), and may also be higher depending upon the available steam pressure and the ability to discharge quickly. Alternate energy transfer modes are possible such as superheated steam or water or direct heat.
  • the reaction pressure can vary from 135 to 1000 psi (9,3 x 10 5 to 6,89 x 10 6 Pa) or higher depending upon the available steam pressure and the ability to discharge quickly.
  • the acid concentration for the process can be from 0 to 10% acid injection at rates of from 0 to 300 pounds (0 to 135,9 kg) per hour.
  • Alternative acids for producing derivatives of fibrous materials such as cellulose can be HCI, HN03, organic acids, S0 2 gas, etc.
  • Dewatering varies with the screw speed and the crammer speed, as well as the screw configuration. It may vary from 80 pounds her hour at 100 pounds per hour feed up to 720 pounds per hour at a 900 pounds per hour feed.
  • the solids in the dewater outlet vary from 0.05% to 5%.
  • the screw machine RPM can vary from 40 RPM to 300 RPM with the given screw converter for both embodiments and the crammer feeder can operate from 8% to 100%.
  • the torque varies from 20% to 100% resulting from the screw RPM, the crammer rate, the consistency of feed, the screw configuration, the temperature profile, rate of acid injection, conversion rate and discharge rate.
  • the glucose conversion depends on all of the parameters noted above such as residence time, acid concentration, temperature, mixing which all depend on the machine parameters and can vary from 5% to 90% of the theoretical conversion maximum.
  • composition in the reaction zone will vary with the feed and the product composition also varies with the feed and the reaction conditions.
  • the forward conveying preheating zone 122a can be any combination of right handed elements up to 2000 mm in length with 30, 45, 60 or 90 mm pitch elements. Also included therein can be mixing, pulverizing, kneading, etc. elements to provide a homogeneous material to the dynamic seal zone.
  • the dynamic seal zone 124 which forms the dynamic plug can be from 15 to 360 mm and comprises 30, 45, 60 or 90 mm left handed pitch elements.
  • the dynamic seal zone which forms the dynamic plug 124 can be from 15 to 360 mm can comprise 30, 45, 60 or 90 mm left handed pitch elements with the unthreaded element 240 constituting a portion of or the entire plug zone and thus can be from 15 to 360 mm in length.
  • the unthreaded cylindrical spacer elements are radially recessed to the extent that they have no screw flights.
  • the screw configuration in the reaction zone comprises the right handed forward conveying elements which is up to 2000 mm in length and includes 30, 45, 60 or 90 mm pitch right handed elements.
  • the thermal configuration is such that all of the zones 2-4 are interchangeable and can vary in length from 1 to 3 barrel sections.
  • the preheating zone temperature can vary from 32 to 212°F (0°C to 100°C) and the reaction zone temperatures can vary from 350 to 545°F (176°C to 285°C).
  • the discharge parameters result from variations in the hydraulic or pneumatic pressure and flow rate results in the valve speed and varies from .1 seconds at 1000 psi (6,89 x 10 6 Pa) with unrestricted flow to several seconds for restricted flow.
  • the cycle rate is controlled by a preset timer which signals a solenoid actuating the ball valve from 2 seconds to one minute for the cycle time.
  • the discharge parameters result from variations in the spring compression pressure and the flow rate results in unrestricted flow for the entire reaction pressure range in the reaction zone.
  • the apparatus and process of the present invention is capable of handling variations in the feed rate to handle both wet and dry feed, from 5 to 100% solids.
  • the feed rate range is from 20 pounds (9,06 kg) per hour to 150 pounds (67,95 kg) per hour of sawdust, corn-stover wheat straw, wood chips, MSW, etc.
  • Other additives may be used to aid in plug formations such as polypropylene, oils, dewatering from previous batches so as to control torque and reduce wear.
  • water When water is injected, it may be injected in the zone 122a forward of the plug zone wherein preheating takes place and equivalent amount of water is added with the acid injection in the reaction zone to maintain equivalent acid concentrations in the reaction zone.
  • pretreatments for the waste feed stock in particular for newspaper, can be used to improve the cellulose to glucose conversion yield.
  • the most effective pretreatment found was hydropulping and irradiation.
  • the irradiations are carried out at ambient temperatures and in the presence of air with an electron beam accelerator. Irradiation dosages ranging from 5 to 50 megarads can be used and the 10 megarad dosage has been found to be the most commercially effective.
  • slurries of hydropulped waste newspapers replaced in polyethylene bags and the bags were heat sealed, each bag containing about 20 pounds (9,06 kg) of hydropulped waste newspaper slurry of known concentration. The bags were then replaced on a conveyor that moved past the beam of an electron beam accelerator and a dosage of 5 megarads per pass was produced thereon.
  • Figure 6 respectively illustrates the results obtained with various process parameters as shown in the embodiment.
  • lignins can be extracted from cellulose by contacting a lignocellulosic slurry or pulp with calcium bisulfite liquor (1% CaO, 4% S0 2 ) at a pH of 9.8 injected into the reaction zone and at a temperature of 180-200°C by way of the injection of steam into the reaction zone.
  • a highly sulfonated lignosul- fonic acid is formed rapidly which is water soluble and can be extracted from the cellulose.
  • Lignosulfonates can be used as binders, etc. for various applications.

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  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • General Health & Medical Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Biochemistry (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
  • Polysaccharides And Polysaccharide Derivatives (AREA)
EP19810101951 1980-03-18 1981-03-16 Process and apparatus for chemical conversion of cellulose waste to glucose Expired EP0037912B1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT81101951T ATE15074T1 (de) 1980-03-18 1981-03-16 Verfahren und vorrichtung fuer die chemische umwandlung von cellulosehaltigen abfallstoffen zu glukose.

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US06/131,340 US4316747A (en) 1980-03-18 1980-03-18 Process for the chemical conversion of cellulose waste to glucose
US131340 1980-03-18
US06/131,339 US4316748A (en) 1980-03-18 1980-03-18 Process for the acid hydrolysis of waste cellulose to glucose
US131339 1980-03-18

Publications (3)

Publication Number Publication Date
EP0037912A2 EP0037912A2 (en) 1981-10-21
EP0037912A3 EP0037912A3 (en) 1982-04-21
EP0037912B1 true EP0037912B1 (en) 1985-08-21

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EP19810101951 Expired EP0037912B1 (en) 1980-03-18 1981-03-16 Process and apparatus for chemical conversion of cellulose waste to glucose

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EP (1) EP0037912B1 (pt)
AU (1) AU548717B2 (pt)
BR (1) BR8101561A (pt)
CA (1) CA1190923A (pt)
DE (1) DE3171880D1 (pt)
IN (1) IN153348B (pt)

Cited By (4)

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US8409357B2 (en) 2011-05-04 2013-04-02 Renmatix, Inc. Self-cleaning apparatus and method for thick slurry pressure control
US8546561B2 (en) 2008-07-16 2013-10-01 Renmatix, Inc. Nano-catalytic-solvo-thermal technology platform bio-refineries
US8546560B2 (en) 2008-07-16 2013-10-01 Renmatix, Inc. Solvo-thermal hydrolysis of cellulose
US8759498B2 (en) 2011-12-30 2014-06-24 Renmatix, Inc. Compositions comprising lignin

Families Citing this family (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2525236A1 (fr) * 1982-04-15 1983-10-21 Creusot Loire Procede et dispositif d'hydrolyse d'une matiere cellulosique
US4728367A (en) * 1985-01-31 1988-03-01 Wenger Manufacturing, Inc. Extrusion method and apparatus for acid treatment of cellulosic materials
SE501141C2 (sv) * 1993-04-16 1994-11-21 Regalco Ab Förfarande för hydrolys av cellulosa- och/eller stärkelsehaltiga material
ES2606281T3 (es) * 2005-07-19 2017-03-23 Inbicon A/S Método y aparato para la conversión de material celulósico en etanol
WO2009076760A1 (en) * 2007-12-19 2009-06-25 Fpinnovations Conversion of knot rejects from chemical pulping
CA2638160C (en) 2008-07-24 2015-02-17 Sunopta Bioprocess Inc. Method and apparatus for conveying a cellulosic feedstock
CA2638152C (en) 2008-07-24 2013-07-16 Sunopta Bioprocess Inc. Method and apparatus for treating a cellulosic feedstock
EP2767633A1 (en) 2009-08-24 2014-08-20 Abengoa Bioenergy New Technologies, Inc. Method for producing ethanol, and co-products from cellulosic biomass
RU2597588C2 (ru) 2010-01-19 2016-09-10 Ренмэтикс, Инк. Производство сбраживаемых сахаров и лигнина из биомассы, использующее сверхкритические текучие среды
JP5933578B2 (ja) * 2010-11-25 2016-06-15 シュトゥディエンゲゼルシャフト・コーレ・ミット・ベシュレンクテル・ハフツングＳｔｕｄｉｅｎｇｅｓｅｌｌｓｃｈａｆｔ Ｋｏｈｌｅ ｍｂＨ セルロースを酸触媒解重合する方法
AU2012250575B2 (en) 2011-05-04 2015-03-26 Renmatix, Inc. Lignin production from lignocellulosic biomass
US9809867B2 (en) 2013-03-15 2017-11-07 Sweetwater Energy, Inc. Carbon purification of concentrated sugar streams derived from pretreated biomass
EP3186286B1 (en) 2014-09-26 2024-04-10 Renmatix Inc. Cellulose-containing compositions and methods of making same
RS63528B1 (sr) 2014-12-09 2022-09-30 Sweetwater Energy Inc Brzi predtretman
EP3583223A4 (en) 2017-02-16 2020-12-23 Sweetwater Energy, Inc. HIGH PRESSURE ZONES FOR PRE-TREATMENT
CN207828156U (zh) * 2017-12-06 2018-09-07 易高环保能源研究院有限公司 利用木质纤维素类原料连续水解制糖的装置
AU2020412611A1 (en) 2019-12-22 2022-07-14 Apalta Patents OÜ Methods of making specialized lignin and lignin products from biomass
CN115157452B (zh) * 2022-09-08 2022-11-22 山西钢建鼎元混凝土制品有限公司 一种用于混凝土浇筑加工的上料装置

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2000822B (en) * 1977-07-11 1982-08-11 Canadian Patents Dev Method of rendering lignin separable from cellulose and hemicellulose in lignocellulosic material and the product so produced

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8546561B2 (en) 2008-07-16 2013-10-01 Renmatix, Inc. Nano-catalytic-solvo-thermal technology platform bio-refineries
US8546560B2 (en) 2008-07-16 2013-10-01 Renmatix, Inc. Solvo-thermal hydrolysis of cellulose
US8409357B2 (en) 2011-05-04 2013-04-02 Renmatix, Inc. Self-cleaning apparatus and method for thick slurry pressure control
US8759498B2 (en) 2011-12-30 2014-06-24 Renmatix, Inc. Compositions comprising lignin

Also Published As

Publication number Publication date
BR8101561A (pt) 1981-09-22
EP0037912A3 (en) 1982-04-21
AU548717B2 (en) 1986-01-02
AU6812681A (en) 1981-09-24
IN153348B (pt) 1984-07-07
EP0037912A2 (en) 1981-10-21
CA1190923A (en) 1985-07-23
DE3171880D1 (en) 1985-09-26

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