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Life-cycle assessment of transportation biofuels from hydrothermal liquefaction of forest residues in… Nie, Yuhao; Bi, Xiaotao Feb 3, 2018

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Nie and Bi  Biotechnol Biofuels  (2018) 11:23 https://doi.org/10.1186/s13068-018-1019-xRESEARCHLife-cycle assessment of transportation biofuels from hydrothermal liquefaction of forest residues in British ColumbiaYuhao Nie1  and Xiaotao Bi1,2*Abstract Background: Biofuels from hydrothermal liquefaction (HTL) of abundantly available forest residues in British Colum-bia (BC) can potentially make great contributions to reduce the greenhouse gas (GHG) emissions from the transporta-tion sector. A life-cycle assessment was conducted to quantify the GHG emissions of a hypothetic 100 million liters per year HTL biofuel system in the Coast Region of BC. Three scenarios were defined and investigated, namely, supply of bulky forest residues for conversion in a central integrated refinery (Fr-CIR), HTL of forest residues to bio-oil in dis-tributed biorefineries and subsequent upgrading in a central oil refinery (Bo-DBR), and densification of forest residues in distributed pellet plants and conversion in a central integrated refinery (Wp-CIR).Results: The life-cycle GHG emissions of HTL biofuels is 20.5, 17.0, and 19.5 g  CO2-eq/MJ for Fr-CIR, Bo-DBR, and Wp-CIR scenarios, respectively, corresponding to 78–82% reduction compared with petroleum fuels. The conversion stage dominates the total GHG emissions, making up more than 50%. The process emitting most GHGs over the life cycle of HTL biofuels is HTL buffer production. Transportation emission, accounting for 25% of Fr-CIR, can be lowered by 83% if forest residues are converted to bio-oil before transportation. When the credit from biochar applied for soil amend-ment is considered, a further reduction of 6.8 g  CO2-eq/MJ can be achieved.Conclusions: Converting forest residues to bio-oil and wood pellets before transportation can significantly lower the transportation emission and contribute to a considerable reduction of the life-cycle GHG emissions. Process perfor-mance parameters (e.g., HTL energy requirement and biofuel yield) and the location specific parameter (e.g., elec-tricity mix) have significant influence on the GHG emissions of HTL biofuels. Besides, the recycling of the HTL buffer needs to be investigated to further improve the environmental performance of HTL biofuels.Keywords: GHG emissions, Life-cycle assessment, Hydrothermal liquefaction, Transportation biofuels, Forest residues, British Columbia© The Author(s) 2018. This article is distributed under the terms of the Creative Commons Attribution 4.0 International License (http://creativecommons.org/licenses/by/4.0/), which permits unrestricted use, distribution, and reproduction in any medium, provided you give appropriate credit to the original author(s) and the source, provide a link to the Creative Commons license, and indicate if changes were made. The Creative Commons Public Domain Dedication waiver (http://creativecommons.org/publicdomain/zero/1.0/) applies to the data made available in this article, unless otherwise stated.BackgroundIn British Columbia (BC), transportation consumes nearly 85% of total refined petroleum fuels [1] and gener-ated about 25 million tonnes of carbon dioxide equivalent  (CO2-eq) in 2014, which corresponds to approximately 38% of total greenhouse gas (GHG) emissions and leads all other economic sectors [2]. To address the concerns of global warming, BC government released its Climate Action Plan in 2008 and set up stepwise GHG emission reduction targets. The interim and ultimate targets aim at achieving 33 and 80% GHG reduction below 2007 levels by 2020 and 2050, respectively [3]. Besides the improve-ments in technology and operation efficiencies of trans-portation, displacing fossil fuels with biofuels is expected to make important contributions to reducing the GHG emissions.Forest residues from logging operations, which con-tain branches, barks, tree tops, etc., are generally of no merchantable value and are burned as part of the for-estry management strategy in BC [4]. The total volume Open AccessBiotechnology for Biofuels*Correspondence:  xbi@chbe.ubc.ca 1 Department of Chemical and Biological Engineering, University of British Columbia, 2360 East Mall, Vancouver, BC V6T 1Z3, CanadaFull list of author information is available at the end of the articlePage 2 of 14Nie and Bi  Biotechnol Biofuels  (2018) 11:23 of woody biomass available for bioenergy production in BC in 2016 was estimated to be around 21 million  m3, of which 15.7% is forest logging residues [5]. Forest residues make up of 5–10% of the feedstock of BC wood pellet industry, which produces about 2 million tonnes of pellets annually, representing 61% of the total capac-ity of Canada [6]. However, 84% of the wood pellets pro-duced end up being exported to Europe for district/home heating and power generation because of a lack of local markets [7, 8]. In BC, residential heating is mostly done by electricity and natural gas (NG), and more than 90% power is generated from hydro [9]. Besides, according to Pa et al. [10], the long-distance transportation of pel-lets could also result in a high-carbon footprint (295 kg  CO2-eq/tonne of pellets). Therefore, one of the potential applications of abundant forest residues in BC is to pro-duce liquid transportation fuels, such as gasoline, jet fuel, diesel, and heavy oil.Hydrothermal liquefaction (HTL) of forest residues to intermediate product bio-oil with subsequent upgrad-ing to finished products is one of the promising conver-sion pathways for transportation biofuel production. HTL decomposes biomass in subcritical to nearly criti-cal water under moderate temperature (280–370 °C) and high pressure (10–25  MPa) [11], thus avoiding the pre-drying step in the conventional gasification and pyroly-sis [12, 13]. Moreover, in contrast to pyrolysis, HTL can produce high quality and stable bio-oil with lower oxy-gen content (5–15 wt%) [14] and higher heating value (30–37 MJ/kg) [11], which has the potential to be directly co-processed with crude oil in a refinery [15–17]. In 2016, Licella reported that their HTL facility has suc-cessfully demonstrated the conversion of wood and agri-culture wastes at commercial scale [18], and recently, it announced to collaborate with Canfor, a Canadian for-est product company, to form a joint venture to integrate its HTL technology with Canfor’s pulp mills in Prince George, BC, to convert woody biomass to biofuels [19].Many current researches on biofuels from HTL are trying to solve the technical obstacles, e.g., the design of HTL reactor for scale up [20], the integration of HTL with other systems [21], process parameter optimization [22] and the co-upgrading potential of HTL bio-oil with crude oil [16, 23], etc. There has been little investiga-tion of HTL [17, 24] in terms of its GHG emission per-formance in comparison with gasification [25–30] and pyrolysis [17, 24, 30–37], based on a systematic review of the state-of-art life-cycle assessment (LCA) studies performed to quantify the GHG emissions of transporta-tion biofuels from lignocellulosic biomass. The criteria of selecting the literatures for review are as follows: (1) only studies assessing thermochemical conversion technolo-gies, i.e., pyrolysis, gasification, and HTL were included; (2) only studies focused on the lignocellulosic biomass were included, because this type of feedstock is abun-dantly available in BC with an established supply chain. Other types of feedstock like oil seed or algae are either unsustainable over short term nor short of stable supply; and (3) only LCA studies on the following liquid trans-portation fuels were included: jet, gasoline, and diesel, while ethanol was not considered. The detailed informa-tion of the reviewed studies is summarized in Additional file  1. According to the review, the following observa-tions can be derived: (1) HTL is a promising conversion pathway in terms of GHG emission performance and (2) the results of LCA varied from study to study, due to the variation in geographic locations, settings of system, feedstock, analytical methods, and the treatment of by- or co-products. A review study focused on the pyrolysis technologies by Roy and Dias [38] has reported similar observations on the variability of LCA results based on feedstock, technology, etc.In view of the great interest in deploying HTL technol-ogy to convert abundant but under-utilized forest resi-dues in BC to biofuels, a specific LCA is timely needed to quantify its environmental impact. To our best knowl-edge, there has been no similar LCA study of HTL biofu-els from forest residues based on BC context. Therefore, the results from this study could help provide a prelimi-nary insight for other researchers and local companies or investors as well as a reference for government policy makers.The following points were addressed in this study: (1) quantification of the life-cycle GHG emissions of HTL biofuel system based on different scenarios; (2) identifi-cation of the “hot spots” of the life-cycle processes that intensively emit GHGs; (3) analysis of the large propor-tional change of GHG emissions under different sce-narios; (4) comparison of the GHG emissions of HTL biofuels produced in BC with general values reported in the literatures; (5) sensitivity analysis on the key param-eters impacting the GHG emissions of HTL biofuels; and (6) making recommendations for improving the GHG emission performance of HTL biofuels.MethodsDescription of case study and processesA total liquid biofuel production rate of 100 million liters per year (MLPY) was assumed as the basis for this study, as proposed in an UBC–Boeing joint project report on evaluating the viability of bio-jet fuel production in west-ern Canada, based on the availability and distribution of forest residues in BC [4]. The Coast Region of BC (see Fig. 1) was chosen as the study area for deploying the 100 MLPY hypothetic HTL biofuels system due to the abun-dantly available forest residues as feedstock, existing oil Page 3 of 14Nie and Bi  Biotechnol Biofuels  (2018) 11:23 refining infrastructure for bio-oil upgrading, and local markets for biofuel product consumption in this area. BC government partitions the Coast Region into several timber supply areas (TSAs) and a sales office is estab-lished for timber marketing in each TSA. The locations of these timber sales offices, namely, Chilliwack, Squamish, Powell River, and Port Alberni, where biomass feedstock was assumed to be supplied to the conversion facilities, are referred to as the feedstock delivery points (FDPs) in this study. There is an existing Chevron oil refinery in Burnaby with a throughput of 8700 m3/days [39], and we assumed that this oil refinery was utilized to upgrade the bio-oil produced in HTL biorefinery. Four different bio-fuel products: gasoline, jet fuel, diesel, and heavy oil are produced and distributed to local markets for end use, specifically, gasoline and diesel for light- and heavy-duty vehicles, respectively, at City of Vancouver, jet fuel for air-planes at Vancouver International Airport, and heavy oil for marine vessels at Port of Vancouver. The geographic locations of all the places mentioned above are schemati-cally shown in Fig. 1.The forest residues availability for each TSA was esti-mated using the method proposed by MacDonald et  al. in a BC government report [40]. The essence is to mul-tiply the annual log harvest volume in that TSA by a biomass ratio, which is defined as the volume of forest residues recovered from unit volume of merchantable logs harvested in the logging operation. The annual log harvest volume was retrieved from the  Harvest Billing System of BC based on the 5-year average data of August 2011–July 2016 [41]. In this study, we assumed that the biomass ratio was 15% based on the situation that most of the timbers in the BC Coast Region are the second growth Hemlock and the harvesting mode is ground-based and cable [40]. In ground-based harvesting sys-tems, a machine travelling over the ground is used to carry the fell trees or logs from the stump to the landing. While in cable systems, the fell trees or logs are carried by a stationary machine with an overhead cable attached [42]. The density (dry basis) and moisture contents (wet basis) of forest residues used in this study are 420  kg/m3 and 49 wt%, respectively. Due to the lack of specific feedstock analysis data, i.e., proximate analysis and ulti-mate analyses, for forest residues in the Coast Region of BC, the feedstock analysis data from Tews et al. [17] were used in our models. The 5-year average annual volumes of harvest logs and estimated available forest residues are shown in Table 1.The case study was developed based on three different scenarios. Although the processes vary with each sce-nario, the realm is from well to wheel. The basic structure of the HTL biofuel system includes the following stages: Study AreaBritish ColumbiaUnited States     Coast RegionPort Alberni ChilliwackSquamishPowell RiverSouth Coast RegionCanadaChevron oil refineryTSA boundary Feedstock deliver pointCity of VancouverStudy TSAWest Coast RegionVancouver AirportPort of VancouverFig. 1 Schematic diagram of geographic information of HTL biofuels system (Powell River, Squamish and Chilliwack lie in the South Coast Region; Port Alberni lies in the West Coast Region)Page 4 of 14Nie and Bi  Biotechnol Biofuels  (2018) 11:23 biomass feedstock collection and transportation, pre-processing, biomass-to-biofuel thermochemical conver-sion, and biofuel product distribution and end use. The main differences between these three scenarios lie in the configuration of biorefinery (integrated with oil refinery or distributed at FDPs) and the type of feedstock (bulky forest residues or forest residues derived bio-oil or wood pellets) supplied to refinery for conversion. For scenario 1 (denoted as Fr-CIR scenario), the collected bulky forest residues from each FDP are directly transported to the central integrated refinery for conversion. For scenario 2 (denoted as Bo-DBR scenario), forest residues are first converted to bio-oil at distributed biorefineries and then transported to a central oil refinery for upgrading. For scenario 3 (denoted as Wp-CIR scenario), forest residues are first densified to wood pellets at distributed pellet plants located at FDPs and then transported to the cen-tral integrated refinery for conversion. The system con-figuration schematic and boundary of each scenario are shown in Fig. 2.Description of case study and processes: biomass collectionBiomass collection stage is the same for three scenarios and was modeled by two steps. The piled forest residues on forest stands of each TSA are first gathered, chipped to smaller size and loaded to dump trucks, and then shut-tled to the FDP. Due to the lack of specific location and productivity of each forest stand in the  corresponding TSA, we simply assumed that the forest residues after logging operation were uniformly distributed around the FDP, and  12.5  km was used as the average distance for shuttling.To meet the 100 MLPY biofuel production target, for Fr-CIR and Bo-DBR scenarios, a total of ~  300,000 dry tonnes of forest residues are needed. While for Wp-CIR scenario, due to the consumption of forest residues as drying fuel in pellet plants, additional ~  36,000 dry tonnes are required. The detailed methods of calculating the annual forest residues supply for different scenarios are given in Additional file 2.Description of case study and processes: transportationThe transportation of biomass feedstock from FDPs to conversion facility varies with scenarios. For Fr-CIR sce-nario, forest residues arriving at FDPs are reloaded to semi-trailers (STs) and then directly transported to the central integrated refinery for conversion. However, for Bo-DBR and Wp-CIR scenarios, the arriving forest resi-dues are first converted to bio-oil and wood pellets in the satellite HTL and pellet plants at FDPs, respectively, and then, the intermediate products are loaded to STs or liq-uid tanker trucks (LTTs) and transported to the refinery for further conversion. It should be noted that transpor-tation from Powell River and Port Alberni to Chevron oil refinery will undergo marine routes. STs or LTTs were thus assumed to be carried by ferries run by British Columbia Ferry Services Inc. To account for the emission associated with carrying STs or LTTs and the feedstock, the total emissions of ferry transportation were allocated by the mass of people, semi-trailers or LTTs, and other vehicles, which are estimated by the information pro-vided on the website of British Columbia Ferry Services Inc. [43]. The transportation distance from Chilliwack, Squamish, Powell River, and Port Alberni to Chevron oil refinery are 102, 74, 179 (including 37 km marine trans-portation), and 170  km (including 57  km marine trans-portation), respectively.To minimize the transportation emission, the total feedstock requirement is apportioned among four FDPs according to their feedstock availability and proxim-ity to Chevron oil refinery, that is, the closer the FDP to the refinery, the higher priority it will be given for forest residues utilization. The detailed data for the annual for-est residues transported from each FDP to the conversion facility can be found in Additional file 2.Description of case study and processes: pre‑processingFor biomass feedstock pre-processing in biorefinery, the incoming forest residues or wood pellets are first unloaded, cleaned, and sent to a grinder for further size reduction. Then, the ground feedstock is mixed with hot Table 1 Annual forest residues availability in BC Coast RegionHarvest logs  (m3/year) Biomass ratio Forest residues availabilitym3/year Dry tonne/year Wet tonne/yearChilliwack 1.21E+06 0.15 1.82E+05 7.64E+04 1.50E+05Squamish 4.98E+05 0.15 7.47E+04 3.14E+04 6.14E+04Powell River 1.93E+06 0.15 2.89E+05 1.21E+05 2.38E+05Port Alberni 5.24E+06 0.15 7.85E+05 3.30E+05 6.46E+05Total 8.87E+06 0.15 1.33E+06 5.59E+05 1.09E+06Page 5 of 14Nie and Bi  Biotechnol Biofuels  (2018) 11:23 water recycled from HTL reaction, producing biomass–water slurry with 8 wt% solids content [17]. To make the life-cycle stages consistent between different scenarios, we also incorporated pellet plant operation in Wp-CIR scenario into the pre-processing stage. For pellet plant operation emission modeling, we used the data from Pa et al. [10], which can be found in Additional file 3.Description of case study and processes: conversionConversion stage includes HTL of biomass feedstock, subsequent hydrotreating of bio-oil, and anaerobic digestion (AD) and hydrogen production processes, as depicted in Fig. 2. The AD unit was integrated with HTL system to treat and recover energy from the HTL waste-water, and a hydrogen production process was designed Bo-DBRFr-CIRWp-CIRScenarios ConversionCollection End useDistributionTransportation Pre-processingIntegrated refineryCollectionForest residuesFeedstock delivery pointTransportationCollectionCollectionCollectionPre-processing HTLSlurryHydrotreatingHydrogen plantBio-oilADBio-gas PHWWDigestateH2Off-gasGasolineHeavy oilJetDieselBiocharRecycled waterNGProcess type:Physical process :Thermochemical process:Biochemical processCompound type:Feedstock:Intermediate :By-product:Final productTransportationDigestateBiocharBio-oilPre-processing HTLSlurryADBio-gas PHWWRecycled waterOil refineryGasolineHeavy oilJetDieselHydrotreatingHydrogen plantOff-gasH2Off-gasCollectionCollectionCollectionCollectionBiorefineryForest residuesNGNGBiorefineryIntegrated refineryTransportation Pre-processing HTLSlurryHydrotreatingHydrogen plantBio-oilADBio-gas PHWWDigestateH2Off-gasGasolineHeavy oilJetDieselBiocharRecycled waterNGCollectionForest residuesWood pellet plantCollectionCollectionCollectionWood pelletFig. 2 System configuration schematic and boundary of different HTL biofuel scenarios (AD, anaerobic digestion; NG, natural gas; PHWW, post HTL waste water)Page 6 of 14Nie and Bi  Biotechnol Biofuels  (2018) 11:23 to meet the hydrogen demand for bio-oil hydrotreating. Both HTL and AD processes are located in the biorefin-ery, while hydrotreating and hydrogen production pro-cesses are located in the oil refinery. The parameters used for modeling the processes in biorefinery and oil refinery are given in Tables 2 and 3, respectively. The HTL process in this study was modeled based on the experimental and simulation data from PNNL report by Tews et al. [17]. The water–biomass slurry generated in the pre-processing process is pressurized and sent to the HTL reactor. The HTL process produces bio-oil, non-condensable gases, biochar as well as water contain-ing high concentration of dissolved organics, called post HTL waste water (PHWW). Sodium carbonate  (Na2CO3) is used as the buffer agent to prevent the pH of the slurry from dropping below 4, thus inhibiting the formation of high molecular weight compounds and solid wastes [44]. HTL bio-oil has low oxygen content and is thermally stable [17]. Therefore, we assumed that it was directly co-processed with crude oil in the Chevron oil refinery without pre-hydrotreating step. Non-condensable gases, Table 2 Major inputs and parameters for modeling HTL biorefinery processesa This value is applicable to Fr-CIR and Bo-DBR scenarios. For Bo-DBR scenario, this is the total electricity/heat input of the HTL units of four distributed biorefineriesb This value is applicable to Wp-CIR scenarioc Feedstock stands for either forest residues or wood pellets, and wood pellets were assumed to have the same conversion rate as forest residuesParameters Value ReferencesAnnual operating hours, h 8000Hydrothermal liquefaction Material and energy input  Buffer  (Na2CO3) content, wt% of slurry1 [44]  Electricity, MW 4.03a/4.10b Scaled from [17]  Heat, MW 50.42a/50.24b Scaled from [20] Products yields, kg/kg dry  feedstockc[17]  Bio-oil 0.367  Off-gases 0.173  Water (with dissolved organics) 0.404  Biochar 0.056 Off-gases composition, wt% [17]  CO2 90.2  H2 0.9  CH4 3.0  C2H6 2.5  C3H8 1.9  C4H10 1.5Anaerobic digestion Products yield, kg/kg wastewater [17]  Biogas 0.23  Solid digestate 0.01  Liquid digestate 0.76 Material and energy input Average of [46, 47]  Electricity, MJ/GJ biogas pro-duced102.32  Heat, MJ/GJ biogas produced 140.89Table 3 Major inputs and parameters for modeling oil refinery processesParameters Value ReferencesAnnual operating hours, h 8000Hydrotreating LHSV,  h−1 0.22 [17] Material and energy input  H2, g  H2/g dry bio-oil 0.033 [44]  Electricity, MW 1.12 Scaled from [17]  Catalyst   Load, kg catalyst/tonne bio-oil 0.41 Calculated based on LHSV   Life, years 1 Products distribution, wt% [17]  Deoxygenated oil 75  Water 18  Off-gases 7 Off-gases composition, wt% [17]  H2 7.8  CH4 18.2  C2H6 15.1  C3H8 13.2  C4H10 4.9  C5H12 1.5  C6H14 39.3 Deoxygenated oil distillation streams, wt%[23]  Gasoline 21  Jet 25  Diesel 35  Heavy oil 19Hydrogen plant GHSV,  h−1 4000 [51] Material and energy input  NG (feedstock), kg/m3  H2 produced0.24 Scaled from [50]  Steam (feedstock), kg/m3  H2 produced0.76 Scaled from [50]  NG (fuel), kg/m3  H2 produced 0.03 Scaled from [50]  Catalyst   Load, kg catalyst/tonne  H2 produced0.12 Calculated based on GHSV   Life, years 3  Electricity, MW 0.15 Scaled from [50]Page 7 of 14Nie and Bi  Biotechnol Biofuels  (2018) 11:23 referred to as off-gases in this study, contains the non-condensable volatile compounds, mostly  CO2, a mod-erate part of light hydrocarbons  (C1–C4), and a small portion of  H2 (see Table 2). The energy in off-gases was assumed to be recovered and reused in conversion pro-cesses. For Fr-CIR and Wp-CIR scenarios, off-gases are sent to hydrogen plant as fuel for hydrogen production, and the remaining is used as fuel for heating anaerobic digester. For Bo-DBR scenario, these gases cannot be sent to hydrogen plant, so they are consumed as heating fuel for HTL and AD. It was assumed that the carbon released from the utilization of these off-gases did not contribute to climate change, since it essentially origins from the carbon intake during tree growth. The solid-phase prod-uct biochar was assumed to be collected and applied for soil amendment in local farms, which will be described in the HTL biofuel LCA section below. Panisko et  al. [45] reported that chemical oxygen demand (COD) of PHWW ranged from 41,000 to 77,000  mg/L, compared with 200  to  1200  mg/L of raw municipal wastewater. Hence, a dedicated treatment facility must be employed at the processing facility. In this study, we assumed that an AD unit was designed for the treatment and energy recovery of PHWW, while the majority of PHWW was recycled for slurry formation in the biomass feedstock pre-processing.In the anaerobic digester, the PHWW is converted into biogas and solid and liquid digestates. Biogas is sent to the HTL unit as heating fuel. The solid and liquid diges-tates are sent to landfill and wastewater treatment plant, respectively, for further treatment, but the impact of both processes is outside the scope of this study. Due to the lack of reported data for PHWW as substrate for AD, a large-scale AD operating at mesophilic temperature (35  °C) and using liquid swine manure as feedstock was used as an approximation to quantify the heat and elec-tricity requirements [46, 47]. A typical large-scale AD can digest 20,000–60,000 tonnes of raw materials per year [47]. The PHWW input into the AD unit in this study is ~ 409,000 tonnes per year (see Additional file 2), which is about ten times larger. While the world’s largest AD plant reported in 2013 being constructed digests 270,000 tonnes organic wastes per year [48], no energy input data of this plant are available. The energy input of a typical large-scale AD is thus the best available data to be used in our study.The hydrotreating process is a catalytic reaction pro-cess, where the oxygenated compounds in bio-oil are exposed to hydrogen under elevated pressure and high temperature [49]. The catalyst utilized in hydrotreating process was assumed to be conventional NiMo/Al2O3 catalyst which is commonly used in crude oil hydro-processing. The effluent from hydrotreating reactors is cooled and separated into deoxygenated oil, wastewater, and off-gas streams. The off-gases from hydrotreating containing mainly light hydrocarbons (see Table  2) are sent to hydrogen plant as feedstock for steam reforming. The deoxygenated oil is then distilled into gasoline, jet, diesel, and heavy oil as finished products.Hydrogen for bio-oil upgrading is produced by NG steam reforming in a hydrogen plant of the oil refinery. The hydrogen demand was determined by the bio-oil production from HTL. As reported in the study of Zhu et al. [44], per gram of dry bio-oil to be treated, 0.033 g of  H2 is needed. The hydrogen production process was modeled based on an NREL report by Spath et  al. [50] with scaling to the specific hydrogen demand. Certain modifications were made on the NREL model to accom-modate the entire HTL biofuel production system. Spe-cifically, the reformer is fueled mainly by the combustible off-gases from hydrogen production, while the remain-ing 4.4 wt% [50] was assumed to be supplied by off-gases from hydrotreating as well as HTL depending on the scenarios, instead of using purchased NG. The electric-ity requirement of the hydrogen plant was modified to be met by BC grid. The catalyst utilized in hydrogen produc-tion process is assumed to be NiMo/Al2O3.Description of case study and processes: distribution and end use of biofuelsFour different liquid biofuel products: gasoline, jet fuel, diesel, and heavy oil are produced in Chevron oil refin-ery and distributed to the local markets. The gasoline and diesel were assumed to be delivered by LTT to a hypo-thetic refueling station for light- and heavy-duty vehi-cles, respectively, at City of Vancouver, which is 10  km away from Chevron refinery. The jet fuel is delivered via an existing 40  km oil pipeline from Chevron oil refin-ery to Vancouver International Airport, for airplanes. The heavy oil is delivered by LTT to Port of Vancouver, 11.3 km away from Chevron refinery, for marine vessels.HTL biofuel LCAAn attributional LCA was conducted to quantify the GHG emissions of HTL biofuels from forest residues in BC. The analysis follows the international standard for LCA, ISO 14040 [52], and the functional unit is set to be 1 megajoule (MJ) of HTL biofuel mix produced.All emissions from each process and its associated upstream supply chain were accounted for in this study. However, the emissions associated with construction of infrastructure, manufacture of equipment as well as waste  water treatment were not included within the scope. In addition, forest residues as feedstock for biofu-els production were considered to carry no environmen-tal burdens linked with the harvested timber in light of Page 8 of 14Nie and Bi  Biotechnol Biofuels  (2018) 11:23 low value of these forest residues, which otherwise will be burned to reduce the risk of wild fire in BC. We also assumed no soil carbon change due to controlled sus-tainable removal of forest residues from forest stands to produce biofuels in BC, with ~  25% of forest residues being left in forest stands to provide nutrients and for the health of the forests [4].The method of handling process by-products can sig-nificantly influence the life-cycle results of biofuel [30, 35, 53]. The by-product biochar produced in HTL plant was assumed to be shipped out to a hypothetic farm 50-km away from biorefinery and applied for soil amendment. HTL biochar contains carbon originating from for-est residues and was modeled as sequestered carbon in this analysis. Although the stability of carbon in biochar depends on many factors such as feedstock, processing, and environmental conditions, we assumed that 80% of the carbon in biochar could be stably sequestrated when it is applied for soil amendment as suggested by Roberts et  al. [54]. Wang et  al. [55] meta-analyzed 24 studies of biochar decomposition in soil and found that about 97% of biochar could contribute to long-term carbon seques-tration in soil. Hence, the 80% assumption we made in this analysis is conservative. Besides the sequestered carbon credit, N in biochar was assumed to displace the same amount of nitrogen fertilizer as suggested by Han et  al. [35]. The emissions associated with the nitrogen fertilizer production are avoided, thus creating another credit. The average data were used to calculate the credit for replacing nitrogen fertilizer. The C and N contents in biochar were assumed to be 51 and 0.5 wt%, respectively [56].Data quality and specificity are generally considered as critical issues for LCA studies. Spatial variation and local environmental uniqueness are one of the concerns that require special attention [57]. Therefore, to enhance the consistency and accuracy of the life-cycle inventory data, whenever possible, BC specific data were utilized, e.g., the feedstock availability, the locations of biofuel supply chain nodes, the transportation, and electricity mix. Oth-erwise, Canadian average, or if not available, US average, data were used with modification on the electricity mix to reflect BC specific mix. GHGenius v4.03 [58], a Cana-dian-based LCA program, was primarily employed for modeling processes such as transportation, energy and fuel production, and consumption, by setting BC as the analyzed region and 2016 as the base year. For the pro-cesses lacking built-in models in GHGenius v4.03, e.g., material production and delivery including HTL buffer agent, hydrotreating and hydrogen production catalyst, and nitrogen fertilizer, the GREET 2015 (Greenhouse gases, regulated emissions, and energy use in transporta-tion) [59] or SimaPro v8.2 coupled with Ecoinvent v3.2 database [60] was used to model the process emissions with modification on the electricity mix. When the data could not be found in the software database described above, they are collected from peer-reviewed journal articles or reports issued by government and widely rec-ognized scientific organizations (e.g., IPCC) or laborato-ries (e.g., PNNL and NREL).The emissions from each process are obtained based on the emission factor method. Concretely, materials and energy consumptions were first calculated for each pro-cess through mass and energy balances and then multi-plied by the corresponding emission factors. The detailed mass and energy balances of pre-processing and conver-sion stages can be found in Additional file 2. The equip-ment energy input and processes emission factors used in modeling are summarized in Additional file 3. The col-lected raw data from the various sources described above were first compiled in Microsoft Excel to build the life-cycle inventory of HTL biofuels, and then, IPCC 2007 global warming potential factors were used to convert  CO2,  CH4, and  N2O into  CO2-eq for a time horizon of 100 years.Results and discussionLife‑cycle GHG emissionsFigure  3 shows the life-cycle stagewise GHG emissions of three different HTL biofuel production scenarios. The life-cycle GHG emissions for Fr-CIR, Bo-DBR, and Wp-CIR scenarios are 20.5-, 17.0-, and 19.5-g  CO2-eq/MJ, respectively, corresponding to 78, 82, and 79% reduc-tion relative to 2005 gasoline baseline 93-g  CO2-eq/MJ [61]. When considering the credit from biochar applied for soil amendment, the life-cycle GHG emissions of HTL biofuels can be further reduced by 6.8-g  CO2-eq/MJ, corresponding to 85, 89, and 86% reduction of the life-cycle GHG emissions compared to petroleum fuels for Fr-CIR, Bo-DBR, and Wp-CIR scenarios, respec-tively. The detailed GHG emission profile of individual processes is given in Table 4. For all three scenarios, the -10-505101520259095Fr-CIR Bo-DBR Wp-CIRGHGemissions(gCO2eq/MJ biofuel)End useFuel distributionConversionPre-processingFeedstock transportationFeedstock collectionBiochar creditNet emissions2005 gasoline baseline=93 g CO2eq/MJ-87% (With biochar credit)-80% (Without biochar credit)-16.9% -4.7%Fig. 3 Stagewise GHG emissions of HTL biofuels from three different scenariosPage 9 of 14Nie and Bi  Biotechnol Biofuels  (2018) 11:23 most dominant contributor to GHG emissions is biofuel conversion, which makes up more than 50%, followed by feedstock delivery, including collection and transporta-tion of biomass feedstock, accounting for 19–39% of total emissions depending on specific scenario. The process having the highest global warming impact over the whole life cycle of HTL biofuels is the HTL buffer agent  Na2CO3 production. In this study, due to the lack of industrial data of  Na2CO3 consumption in the HTL process, we used the bench test data reported by Zhu et al. [44] and Panisko et  al. [45] from PNNL, i.e.,  Na2CO3 was con-sumed at 1 wt% of the total feed slurry. This value could be higher than the demonstration- or industrial-scale data because of the assumed no-recycling of  Na2CO3. Although we assumed that PHWW was recycled for the slurry formation, we did not consider the remaining  Na2CO3 in the recycled waste water, because no data are currently available about the buffer consumption rate in the HTL reaction. The contribution of biomass collec-tion is similar among the three scenarios (13–16%), while the transportation varied significantly. In Fr-CIR sce-nario, feedstock transportation accounts for about 25% to the GHG emissions of HTL biofuel. The long-distance transportation and the low  energy density of bulky for-est residues lead to the high transportation emissions. In contrast, for Bo-DBR and Wp-CIR scenarios, the bulky forest residues are first densified into high  energy den-sity intermediate products, bio-oil, and wood pellets, which are transported to refinery for further conversion. Compared with Fr-CIR scenario, Bo-DBR and Wp-CIR scenarios can lower the transportation emissions by 83 and 44%, respectively. However, the configuration change also causes increase of GHG emissions in other stages. For Wp-CIR scenario, due to the use of biomass feed-stock as heating fuel in pellet plant operation, more for-est residues need to be collected from forest stands, thus increasing the emissions of collection stage. Besides, pel-let plant operation is linked with upstream (heating fuel production and electricity generation) and downstream (fuel combustion) emissions [10], which contribute to the increased emissions in pre-processing stage compared with the other two scenarios. For Bo-DBR scenario, the off-gases produced in the distributed HTL plants could not be used in the refinery as in integrated systems, i.e., Fr-CIR and Wp-CIR, so NG is needed as a feedstock for hydrogen production, thus increasing hydrogen produc-tion emissions. Overall, Bo-DBR and Wp-CIR scenarios can achieve 16.9 and 4.7% reduction of total GHG emis-sions compared with Fr-CIR scenario. In Fr-CIR and Wp-CIR scenarios, AD operation is an important con-tributor to the life-cycle GHG emissions of HTL biofuels, accounting for around 14%. NG is used as heating fuel for maintaining the AD operating temperature, since off-gases produced by HTL are sent to refinery for hydrogen production. However, in Bo-DBR scenario, the impact of AD operation can be considerably reduced due to the use of remaining off-gases from HTL as heating fuel for AD. Comparison with peer‑reviewed literaturesTo check whether the HTL biofuel GHG emission results from this study are consistent with those from peer-reviewed literatures, we have conducted a comparison using the results from part of the reviewed studies, as presented in Additional file  1. The studies were chosen for comparison only when the following criteria are met: (1) the system boundary is well-to-wheel or well-to-wake and (2) the functional unit is MJ of biofuel. Figure 4 pre-sents the analyzed life-cycle GHG emissions of this study and those of literatures. The bar in Fig. 4 stands for the median value of the GHG emission results of all studies of a specific conversion pathway, instead of the mean value, because we found that the mean can be easily influenced by the extreme values of certain studies, and the error bar represents the standard deviation. It should be noted that the GHG emission results of this study used to compare are the net emission results including the biochar credit, since the results from majority of the selected literatures consider the by- or co-products credit.According to the results shown in Fig.  4, gasifica-tion generally has the best GHG emission perfor-mance (11.6  ±  4.14  g  CO2-eq/MJ), followed by HTL Table 4 Percent contribution of each process stage to the life-cycle GHG emissions of HTL biofuelsHTL biofuel life‑cycle stage Fr‑CIR (%) Bo‑DBR (%) Wp‑CIR (%)Feedstock collection 13.12 15.79 15.47 Loader and chipper operation 7.53 12.28 12.22 Forest residues shuttling to FDPs5.59 3.51 3.25Feedstock transportation 25.47 5.29 14.90Pre-processing 2.88 3.47 8.07 Grinder and dust collector operation2.25 2.71 2.36 Loader operation 0.63 0.76 0.66 Pellet plant operation N/A N/A 5.04Conversion 53.36 69.23 56.11 Electricity 4.17 5.02 4.44 HTL buffer 34.44 41.46 36.15 AD gas combustion in HTL burner1.10 1.32 1.15 AD operation 13.53 5.02 14.24 Hydrogen production 0.07 16.34 0.07 Hydrotreating catalyst 0.06 0.07 0.06Fuel distribution 0.17 0.20 0.17End use 5.00 6.02 5.28Page 10 of 14Nie and Bi  Biotechnol Biofuels  (2018) 11:23 (12.67  ±  1.46  g  CO2-eq/MJ from this study and 23.58  ±  4.18  g  CO2-eq/MJ from literatures) and finally pyrolysis (33.77 ± 16.24 g  CO2-eq/MJ). Our results seem to be consistent with the general trend, although it is about 46% lower than the median value of HTL biofuel results from the literatures. This could be explained by the much lower emission intensity of the BC electricity mix compared with the US electricity mix, which was used in the two HTL LCA studies we reviewed [17, 24]. Another major reason could be the credit assigned for by-products. In this study, we assumed that by-product biochar applied for soil amendment could create credits both from carbon sequestration in the soil as well as the avoidance of nitrogen fertilizer production. In contrast, the other two studies did not consider the credit from biochar produced by HTL.Sensitivity analysisTo investigate key factors influencing the GHG emissions of HTL biofuels, a sensitivity analysis was conducted by adjusting the nominal values of uncertain parameters to − 10 and + 10%. For electricity mix sensitivity analysis, BC electricity mix was entirely displaced with Alberta (AB) electricity mix with keeping all other modeling parameters unchanged. The parameters as well as their values used for sensitivity analysis are categorized and are listed in Table 5. It should be noted that the life-cycle GHG emissions are the net values with the biochar credit considered.As shown in Fig.  5, although each scenario presented different results, in general, the most sensitive parame-ters are associated with process performance. The change of HTL energy requirement and biofuel yield by 10% can lead to more than 10% variation of the GHG emissions for all scenarios. However, it should be noted that for Bo-DBR scenario, the 10% decrease of HTL energy require-ment does not have appreciable impact on the GHG emissions. This is because at the nominal HTL energy requirement level, the HTL and AD units can be self-energized by biogas from AD as well as off-gases from HTL in Bo-DBR scenario. Therefore, further lowering the HTL energy requirement will not make a difference.The 10% change in biomass content in slurry and car-bon sequestrated in biochar shows a moderate impact (range of ± 5 to ± 10%). With a fixed biomass input, the biomass content in slurry can influence the total weight of slurry, which further determines the electricity con-sumption of pumping as well as the input of HTL buffer  Na2CO3. As the results in Table 4 suggest, the consump-tion of  Na2CO3 is a crucial contributor to the GHG emis-sions of HTL biofuels. Biochar, in this study, was assumed to be applied for soil amendment and created GHG cred-its from carbon sequestration as well as the avoidance of nitrogen fertilizer production. Although there is uncer-tainty regarding the biochar carbon stability in the soil, reported studies [55, 62] generally show a stable property of the biochar carbon. However, specific models need to 0 10 20 30 40 50 60HTLHTL GasificationPyrolysisThis studyLiteraturesLife cycle GHG emissions (g CO2eq/MJ)Fig. 4 Comparison of HTL biofuel life-cycle GHG emissions results with literaturesTable 5 List of parameters used for sensitivity analysis of GHG emissions of HTL biofuelsa From [9], average of 2010–2012, detailed emission factors are shown in Additional file 3b From [9], average of 2010–2012, detailed emission factors are shown in Additional file 3Category Parameters Nominal − 10% + 10%Feedstock property Moisture content of forest residues: wt% 48.91 44.02 53.80Feedstock supply Feedstock collection distance: km 12.5 11.25 13.75Process performance Biomass content in slurry for HTL: wt% 8.0 7.2 8.8Bio-oil yield: kg/kg dry wood 0.367 0.330 0.404HTL energy requirement: MW 50.4 45.38 55.46Biofuel yield: kg/kg bio-oil 0.75 0.68 0.83By-product credit Carbon sequestered in biochar: wt% 80 72 88Location specificity Electricity mix: %BC electricity  mixa: hydro: 90.4; biomass: 4.9; NG: 2.9; fuel oil: 1.5; wind: 0.3AB electricity  mixb: Coal: 72.4; NG: 19.6; wind: 3.6; hydro: 3.5; fuel oil: 0.9Page 11 of 14Nie and Bi  Biotechnol Biofuels  (2018) 11:23 be developed in the future to verify the carbon sequestra-tion potential of HTL biochar.The  10% change in other parameters such as bio-oil yield, moisture content of forest residues, and feedstock collection distance has modest (within ± 5%) impact on the GHG emissions. It should be mentioned that although moisture content of forest residues is considerably sensi-tive to Fr-CIR scenario, it makes little impact for Bo-DBR and Wp-CIR scenarios. Bio-oil yield does not influence the GHG emissions of HTL biofuels as much as bio-fuel yield, because the bio-oil yield has larger impact on the biochar credit, which can offset the impact of other life-cycle stages, than biofuel yield. The biochar credit is directly related to biochar yield, which can be influenced by bio-oil yield from two layers. First, the change of bio-oil yield can impact the feedstock requirement, which leads to parallel change of the yield of all HTL products, i.e., bio-oil, off-gases, biochar, and PHWW. The second layer is that the bio-oil yield can influence HTL products pro-file. For example, the decrease of bio-oil yield will increase the fraction of biochar in HTL products. In contrast, the change of biofuel yield only has the first layer effect.Moisture content of feedstockDistance for biomass collectionBiomass content in slurryBio-oil yieldHTL energy requirementBiofuel yieldCarbon sequestered by biocharIncrease (+10%)Decrease (-10%)Wp-CIRBase LC GHG emissions=12.67 g CO2eq/MJMoisture content of feedstockDistance for biomass collectionBiomass content in slurryBio-oil yieldHTL energy requirementBiofuel yieldCarbon sequestered by biocharIncrease (+10%)Decrease (-10%)Bo-DBRBase LC GHG emissions=10.21 g CO2eq/MJ-30% -20% -10% 0% 10% 20% 30% 40%Moisture content of feedstockDistance for biomass collectionBiomass content in slurryBio-oil yieldHTL energy requirementBiofuel yieldCarbon sequestered by biocharChange of life cycle (LC) GHG emissions/% Increase (+10%)Decrease (-10%)Fr-CIRBase LC GHG emissions=13.69 g CO2eq/MJFig. 5 Sensitivity analysis of net life-cycle GHG emissions of HTL biofuels for different scenariosPage 12 of 14Nie and Bi  Biotechnol Biofuels  (2018) 11:23 The significant impact of electricity mix on the HTL biofuel GHG emissions is indicated in Fig. 6. With more than 90% renewable composition, BC’s electricity mix is more favorable than that of AB. A change from BC elec-tricity mix to AB electricity mix can lead to a 168, 225, and 182% increase in the GHG emissions for Fr-CIR, Bo-DBR, and Wp-CIR scenarios, respectively. Therefore, locating the potential HTL system in a place with clean electricity mix like BC can considerably lower the GHG emissions of HTL biofuels.Improving the GHG emission performance of HTL biofuelsBased on the life-cycle “hot spots” and the key parame-ters impacting the GHG emissions of HTL biofuels iden-tified in this study, the following recommendations can be made to help improve the GHG emission performance of HTL biofuels produced in BC as well as to provide insights for companies or investors who want to deploy such a facility:1. Increase the recycling rate of HTL buffer  Na2CO3 with the understanding of energy and material con-sumption of the recycling process.  Na2CO3 use has been identified to contribute mostly to the life-cycle GHG emissions of the proposed HTL plant in BC. According to our analysis, if the recycling rate of the buffer increases by 25%, the GHG emissions can be reduced by 13–17%. This is a promising way to fur-ther increase the environmental performance of HTL biofuels, while the energy and material input associ-ated with the recycling need to be first clearly under-stood.2. Lower the transportation emission by densifying bio-mass feedstock before transportation to conversion facilities. For long-distance transportation of feed-stock with high moisture content, we recommend to first convert these raw materials into high energy density intermediate product such as bio-oil or wood pellets. If the infrastructure is available within a rea-sonable distance, it will be ideal to utilize such exist-ing facility. Otherwise, the economics of constructing the new infrastructure, or alternatively purchasing the mobile conversion devices, needed to be first investigated.3. Increase the process performance of the HTL biofuel system. Specifically, the main efforts need to be put on increasing the energy efficiency of HTL and maxi-mizing the biofuel yield. This relies on the optimiza-tion of HTL system design, e.g., integrated with AD, to reduce the fossil energy input. Other improvement can be made in increasing the biomass content in the slurry. With the advancement of pump technol-ogy, transmission of large-scale biomass–water slurry would be feasible.4. Make full use of the processe by-products, i.e., off-gases, biochar, and PHWW, to create GHG savings. Off-gases can be used as either heating fuel for dif-ferent operation units or feedstock for hydrogen production to avoid the input of external NG. Bio-char applied for soil amendment can create credits from both carbon sequestration and the avoidance of nitrogen production, while specific models need to be developed to verify the carbon sequestration potential of biochar to reduce the uncertainty. HTL can be integrated with an AD unit to recover energy from the PHWW, hence increase the energy effi-ciency of HTL.5. Locate the HTL biofuel system in a place with favora-ble electricity mix. This can make a big difference, as shown in the comparison of the electricity mix of BC and AB.ConclusionsThis study quantified the life-cycle GHG emissions of a hypothetic 100 MLPY HTL biofuel production system in British Columbia based on three different system con-figurations. The results suggest that compared with the conventional petroleum fuels, up to 89% GHG emission reduction can be achieved by HTL biofuels with the bio-char credit considered. The conversion stage dominates the total emissions, contributing more than 50%. The process emitting most GHGs over the life cycle of HTL biofuels is HTL buffer production, resulted from the large amount of buffer consumed to maintain the pH of biomass slurry in the HTL process. Recycling of the HTL buffer thus needs to be further investigated to reduce the impact. Converting forest residues to bio-oil and wood pellets before transportation can significantly lower the transportation emission and contribute to the consider-able reduction of the life-cycle GHG emissions of HTL 13.710.212.736.733.235.7051015202530354045Fr-CIR Bo-DBR Wp-CIRGHGemissions(gCO2eq/MJ)BC electricity mix AB electricity mix168%225%182%Fig. 6 Sensitivity of electricity mix on net life-cycle GHG emissions of HTL biofuels for different scenariosPage 13 of 14Nie and Bi  Biotechnol Biofuels  (2018) 11:23 biofuels. A sensitivity analysis indicates the importance of process performance parameters, such as HTL energy requirement and biofuel yield, as well as the location spe-cific parameter such as the electricity mix. Therefore, the main efforts can be put on increasing the energy effi-ciency of HTL and maximizing the biofuel yield to fur-ther improve the GHG emission performance of HTL biofuels.AbbreviationsLCA: life-cycle assessment; GHG: greenhouse gas; HTL: hydrothermal liquefac-tion; BC: British Columbia; AB: Alberta; NG: natural gas; MLPY: million liters per year; TSA: timber supply area; FDP: feedstock delivery point; ST: semi-trailer; LTT: liquid tanker truck; AD: anaerobic digestion; PHWW: post HTL waste water; LHSV: liquid hourly space velocity; GHSV: gas hourly space velocity.Authors’ contributionsYN participated in the system design, collected the data and built the life-cycle inventory, conducted the analysis, and drafted the manuscript. XB participated in the system design, supervised the analysis, and provided suggestions on refining the manuscript. All authors critically reviewed the manuscript and contributed to its contents. Both authors read and approved the final manuscript.Author details1 Department of Chemical and Biological Engineering, University of British Columbia, 2360 East Mall, Vancouver, BC V6T 1Z3, Canada. 2 Clean Energy Research Center, University of British Columbia, 2360 East Mall, Vancouver, BC V6T 1Z3, Canada. AcknowledgementsThis project is supported financially by the BiofuelNet Canada, the Boeing Company and the Mitacs Canada. We also would like to thank Zhengyang Liu and Xianwen Chen for collecting part of the data used for developing the initial case study.Competing interestsThe authors declare that they have no competing interests.Availability of data and materialsThe data used for modeling were taken from peer-reviewed articles [10, 17, 41, 44, 46, 50], GHGenius v4.03 database [58], GREET databases [59], and SimaPro v8.2 Ecoinvent v3.2 database [60]. Except Ecoinvent v3.2 database, other data sources are publicly available. Other supporting data in the article are provided in “Additional files 1, 2 and 3”.Ethics approval and consent to participateNot applicable.FundingThe funding is provided by the NSERC via its BiofuelNet Strategic Research Network program, the Boeing Company, and the Mitacs Canada graduate fellowship program.Publisher’s NoteSpringer Nature remains neutral with regard to jurisdictional claims in pub-lished maps and institutional affiliations.Additional filesAdditional file 1. 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