Comparison of processing lines to convert lignocellulosic C5 sugar - PowerPoint PPT Presentation

sede Manizales Comparison of processing lines to convert lignocellulosic C5 sugar platform to furfural and biogas V. Aristizábal-Marulanda 1 , J. A. Poveda G. 1 , C. A. Cardona A. 1 varistizabalm@unal.edu.co, japovedag@unal.edu.co, ccardonaal@unal.edu.co 1 Instituto de Biotecnología y Agroindustria, Departamento de Ingeniería Química, Universidad Nacional de Colombia at Manizales, Km 07 vía al Magdalena, (+57) (6) 8879300 Ext. 55354, Manizales – Caldas, Colombia 1 Research Group in Chemical, Catalytic and Biotechnological Processes

Overview sede Manizales Introduction 1 1.1 Platform products 1.2 Challenges of lignocellulosic Materials and Methods biomass 2 2.1 Raw material 2.2 Stand-alone processes 2.3 Technical, economic and environmental Results and Discussion assessment 3 3.1 Experimental results 3.2 Techno-economic results 3.3 Environmental results Conclusions 4 Acknowledgments 5 References 2 Research Group in Chemical, Catalytic and Biotechnological Processes

1. Introduction sede Manizales 1.1 Platform products Building blocks Syngas, biogas, C6 sugar Platform product and C5/C6 sugars, plant- Pillars based oil, algae oil, organic Feedstocks Products solutions, lignin, pyrolysis Bulk chemicals oil Physical Chemical Biochemical Thermochemic Sugar crops, al Biofuels, energy, organic lignocellulosic crops, acids, biofertilizers, etc. algae crops, etc. CONVERSION START FINAL PROCESSES STAND-ALONE PROCESSES BIOREFINERIES 3 Research Group in Chemical, Catalytic and Biotechnological Processes

1. Introduction sede Manizales 1.2 Challenges of lignocellulosic biomass SEARCH Lignocellulosic HEMICELLULOSE: C5 SUGARS biomass with high availability and low PLATFORM cost SYSTEMATIC RESEARCH REVISE Appropriate T o demonstrate the confjgurations best processing processes in order to alternative to achieve the effjcient effjciently use and use of lignin and transform C5 sugars hemicellulose fractions to added-value CHOOSE products. Suitable pretreatment technologies Enzymes with the best performance 4 Research Group in Chemical, Catalytic and Biotechnological Processes

2. Materials and Methods sede Manizales 2.1 Raw material and sample analysis RAW MATERIAL: CCS CHARACTERIZATION • NREL standards (National Renewable Energy Laboratories) for moisture, extractives, ashes CCS were obtained from a farm calculation. placed at Salamina, a town of • TAPPI (T echnical Association of the north of Departamento de Caldas, Pulp and Paper Industry) standards located in the center of Colombia were use to determine cellulose, hemicellulose, Klason lignin and soluble lignin content (T-264-cm-07; T-211-cm-93; T-249-em-85). YSIS • Sugars (glucose and xylose): SAMPLE ANAL High-Performance Liquid Chromatography (HPLC- ELITE LaChrom). • Furfural and hydroxymethylfurfural (HMF)): UV spectrophotometry. • Biogas: Displacement of water volume and biogas analyzer. 5 Research Group in Chemical, Catalytic and Biotechnological Processes

2. Materials and Methods sede Manizales 2.2 Stand-alone processes Chemical Characterization B A Moisture, extractives, cellulose, Cofgee cut- Cofgee cut- hemicellulose, lignin and ashes stems stems Particle size Particle size reduction reduction Chemical Characterization Moisture, cellulose, hemicellulose Drying Drying and lignin Solid Solid Dilute-acid hydrolysis Dilute-acid hydrolysis Analysis C5 sugars C5 sugars Glucose, xylose and furans Anaerobic digestion Dehydration reaction BIOGAS FURFURAL Figure 1. Flowsheet of stand-alone processes for the obtaining of, A) biogas and B) furfural. 6 Research Group in Chemical, Catalytic and Biotechnological Processes

2. Materials and Methods sede Manizales 2.2 Stand-alone processes OPERATING CONDITIONS Slices of 3-5mm of width and 10-30mm of diameter. The slices were milled Particle size reduction using a knife mill. the material was sieving to pass meshes of 40 (0.425mm) and 60 (0.250mm). The obtained materials were dried in an oven (Thermo Precision model 6545) Weaknesses Drying at 40°C and 24h. Opportunities Milled CCS sample (25g) were mixed with sulfuric acid at 2% (v/v) to obtain a Dilute-acid hydrolysis 1:10 solid-liquid mass ratio [8]. In autoclave the operating conditions were, Threats 115°C and 3h. The C5 sugars fraction was used for the biogas production at 37°C, 20 days Anaerobic digestion and a pH of 7.0 in a thermostatic bath using as inoculum, sludge from spent cofgee grounds treatment in Cofgee Factory . Catalyzed by CrCl 3 at 180°C and 11bar for 2h 11 . A HP-Autolab Reactor with a Dehydration reaction maximum capacity of 300mL. 7 Research Group in Chemical, Catalytic and Biotechnological Processes

2. Materials and Methods sede Manizales 2.3 Technical, economic and environmental assessment The energy Software SimaPro v8.3 (PRe consumption was Sustainability, Netherlands) and determined using the Ecoinvent database were used Aspen Energy to measure the environmental Analyzer v9 impact of the cradle-to-gate approach Climate change (CC), Ozone depletion (OD), T errestrial acidifjcation (TA), Freshwater eutrophication (FE), Human Politics Technical Environment toxicity (HT), Photochemical oxidant formation (POF), Particulate matter formation (PMF), Freshwater ecotoxicity (FET), Agricultural land occupation (ALO) Experimental Economic and Fossil depletion (FD) Mass and energy balances Economic parameters CAPEX. Fixed capital costs of were experimentally as CAPEX and OPEX equipment. obtained and then were calculated using OPEX. Sum of costs of raw materials, translated to simulation the software Aspen utilities, maintenance, labor, fjxed and procedures. Process Economic general costs and overhead. Analyzer v9 Analysis of scale. 234, 180, 108 and 50 ton/h 8 Research Group in Chemical, Catalytic and Biotechnological Processes

3. Results and Discussion sede Manizales 3.1 Experimental results Table 1. Physicochemical characterization of CCS (% w/w dry). Quintero et Aristizábal Component al. (2013) This work et al. [15] (2015) [16] 9.11±0.39 4.12 Moisture 11 14.18±0.85 Cofgee tree 9.36±0.12 Extractive 8.38 0.96±0.13 1.27±0.03 Ash 2.27 Cellulose 35.13±0.81 40.39±2.20 37.35 Hemicellulose 11.42±0.31 34.01±1.20 27.79 Lignin 34.01±0.56 10.13±1.30 19.81 High amounts of lignin content hinders the access to hemicellulose and cellulose polymers, therefore, to their monomers ( i.e., xylose and Cofgee cut- glucose) stems 9 Research Group in Chemical, Catalytic and Biotechnological Processes

3. Results and Discussion sede Manizales 3.1 Experimental results Kaparaju et al. (2009) performed Table 2. Experimental yields and conversions obtained in the process units. assays of the biological methane potential (BMP) at 55°C from Process unit Yield Units Conversion wheat straw hydrolysates obtained from hydrothermal g xylose/g hemicellulose 0.75 Hemicellulose: pretreatments [21]. For this confjguration, a methane yield 0.12 g furfural/g hemicellulose 97.57% of 384 ml/g VS is obtained. Dilute-acid g glucose/g cellulose* hydrolysis 0.06 Cellulose*: g HMF/g cellulose 25.17% 0.09 Martin and Grossman (2016) Biogas presented the furfural production 509.50 mL accumulated biogas/g VS N.R. using the same process mL accumulated CH 4 /g VS 81.15 N.R. confjguration that in this work, and reported a conversion of 82 Xylose: 63% 0.07 g furfural/g xylose Furfural and 70% for glucose and xylose, N.R. Non-reported respectively [8]. *Minimum hydrolysis due to the use of acid. Despite the high lignin content in the CCS, the acid hydrolysis fulfjlls with its target , that is to release sugars contained in material structure, specially, xylose from hemicellulose with a yield of 0.75 10 Research Group in Chemical, Catalytic and Biotechnological Processes

3. Results and Discussion sede Manizales 3.2 Techno-economic results PURIFICATION Biomethane: High pressure water scrubbing Furfural: Distillation Figure 1. Process schemes A) Biomethane production and B) Furfural production. 11 Research Group in Chemical, Catalytic and Biotechnological Processes

3. Results and Discussion sede Manizales 3.2 Techno-economic results Table 3. Energy requirements of both processes. Utilities cost without using wastewater as cooling water Furfural Biomethan Utility (MJ kg -1 e (MJ kg -1 CCS) CCS) Biomethane: 31.950 M- 2.247 USD/year Cooling water 1.085 Furfural: 60.976 M-USD/year 20.551 N.A. Low pressure steam Utilities cost using 0.009 Medium pressure 0.009 steam wastewater as cooling water N.A. 3.021 High pressure steam Electricity Biomethane: 7.082 M-USD/year 0.007 0.008 Furfural: 9.016 M-USD/year N.A. Non-Apply. 12 Research Group in Chemical, Catalytic and Biotechnological Processes

3. Results and Discussion sede Manizales 3.2 Techno-economic results: Furfural M-USD/year 350 300 The equipment costs such as, dehydration 250 reactor and distillation columns are the 200 main contributors to CAPEX. 150 Raw materials cost represents 100 approximately 86% of OPEX, followed by utilities cost with 10%. 50 0 After 108ton/h of processing capacity, the 50 108 180 234 profjts are higher than OPEX. Processing capacity (ton/h) CAPEX OPEX Depreciation Profits Figure 2. Distribution of the production costs and profjts of furfural production. 13 Research Group in Chemical, Catalytic and Biotechnological Processes