Energetic, ecologic and fluid-dynamic analysis of a fluidized bed gasifier operating with sugar cane bagasse

This work aims to study the thermodynamic, ecological and fluid-dynamic aspects of a circulating fluidized bed gasifier using sugar cane bagasse as biomass, in order to estimate a model of its normal operation. In the initial stage was analysed the composition of biomass selected (sugar cane bagasse) and its lower heating value (LHV) was calculated. The energy balance of the gasifier was done, being the volumetric flow of air, synthesis gas and biomass estimated. Also the power produced by this gasifier was theoretically estimated. Then the circulating fluidized bed gasifier was designed for operation with approximately 100 kg/h of processed biomass. Cross-sectional area of the reactor, feeder size, diameter of the exit zone of the gases and minimum height of the expanded bed were selected. Some bed gasifier hydrodynamic factors were also studied. The minimum fluidization velocity, fluidization terminal velocity, and average fluidizing velocity were calculated, in order to understand the fluid-dynamic behaviour of gasification of this fuel. It was obtained a theoretical model that can support a possible prototype of circulating fluidized bed gasifier biomass. Finally, there were studied the ecological aspects of the gasifier, through an overall methodology. Ecological efficiencies were estimated for two scenarios: first considering the carbon cycle and thereafter disregarding the carbon cycle. In both cases, it can be proved the ecological viability of the project. © 2013 Elsevier Ltd. All rights reserved.

Cogeração a partir da biomassa residual de cana-de-açúcar: estudo de caso

Coordenação de Aperfeiçoamento de Pessoal de Nível Superior (CAPES)

Caracterização química, física e térmica de pellets de madeira produzidos no Brasil

Coordenação de Aperfeiçoamento de Pessoal de Nível Superior (CAPES)

Análise energética da madeira e do carvão de híbridos entre Corymbia citriodora (Hook.) K.D. Hill & L.A.S. Johnson e Corymbia torelliana (F. Muell.) K.D. Hill & L.A.S. Johnson

This research aimed to evaluate the wood and charcoal quality of hybrids clone of the crossing C. citriodora with C. torelliana in two different locations for charcoal production. Seven with 3,75 years old clones, planted at country of Itamarandiba – MG, and six 6,42 years old clones, planted in Dionísio – MG, were studied. For wood and charcoal quality analysis, samples were collected along the stem of the trees until the commercial height. Properties study of the wood was done by chemical analysis, basic density, superior heat power, and thermogravimetric analysis. The wood samples were carbonized in laboratory conditions with heating rate of 1.67 0 C.min -1 , starting at 100 0 C until 450 0 C and keeping on this temperature for 30 minutes. It were determined the carbonizations gravimetric yield, all in dry basis. The wood quality was evaluated based on the chemical immediate analysis, relative apparent density, and gross heating value. The experiment was installed according to the completely randomized design, with five repetitions. The collected data were submitted to analysis of variance and, when the evaluated effects were significant by “F” test, was applied the Scott-Knott test at 5% probability for multiple comparisons. For correlation analysis, Pearson correlation coefficient, tested by the "t" test at 5% probability was used. Results showed variability of wood between the genetic materials evaluated in relation to place and plant crossing. The thermal analysis of the wood showed significant variation between clones and it was possible to differentiate two stages of degradation (hemicelluloses and cellulose). The majority of the clones presented satisfactory properties for the charcoal production, while, clone 3, planted in Itamarandiba, obtained the best performance due it have the higher yield and energetic efficiency, thus, achieving the best potential for charcoal production. However, clone 9, planted in Dionísio, was the less indicated for charcoal production since it presented the lowest energetic efficiency, gravimetric yield, and densities.

Thermodynamic analysis and comparison of downdraft gasifiers integrated with gas turbine, spark and compression ignition engines for distributed power generation

The objective of the present article is to assess and compare the performance of electricity generation systems integrated with downdraft biomass gasifiers for distributed power generation. A model for estimating the electric power generation of internal combustion engines and gas turbines powered by syngas was developed. First, the model determines the syngas composition and the lower heating value; and second, these data are used to evaluate power generation in Otto, Diesel, and Brayton cycles. Four synthesis gas compositions were tested for gasification with: air; pure oxygen; 60% oxygen with 40% steam; and 60% air with 40% steam. The results show a maximum power ratio of 0.567 kWh/Nm(3) for the gas turbine system, 0.647 kWh/Nm(3) for the compression ignition engine, and 0.775 kWh/Nm(3) for the spark-ignition engine while running on synthesis gas which was produced using pure oxygen as gasification agent. When these three systems run on synthesis gas produced using atmospheric air as gasification agent, the maximum power ratios were 0.274 kWh/Nm(3) for the gas turbine system, 0.302 kWh/Nm(3) for CIE, and 0.282 kWh/Nm(3) for SIE. The relationship between power output and synthesis gas flow variations is presented as is the dependence of efficiency on compression ratios. Since the maximum attainable power ratio of CIE is higher than that of SIE for gasification with air, more research should be performed on utilization of synthesis gas in CIE. (C) 2014 Elsevier Ltd. All rights reserved.

Performance and emissions of a gas turbine engine using ox tallow ethyl-ester blended with kerosene

The performance and emissions behavior of a Rover 1S/60 turboshaft engine when operated with several blends of aviation kerosene and ox tallow ethyl-ester are shown in this article. The tests were performed with a compressor shaft coupled to an hydraulic dynamometer where data of power and mass fuel flow were collected to determine the brake specific fuel consumption. A flue gas analyzer was positioned at the exhaust duct to collect oxygen, carbon dioxide, carbon monoxide and nitrous oxides. An increase in the specific fuel consumption was observed due to the lesser lower heating value of the most oxygenated blends. However, reductions of CO, CO2 and NO (x) have been observed and no-significant ill effects have occurred in the turbine operation.

Caracterização de biomassa lignocelulósica para uso em processos térmicos de geração de energia

Pós-graduação em Química - IQ

The Mutagenic Potential Caused by the Emissions from Combustion of Crude Glycerin and Diesel Fuel

Conselho Nacional de Desenvolvimento Científico e Tecnológico (CNPq)

Caracterização físico-química da biomassa produzida em sistemas florestais de curta rotação para geração de energia

Pós-graduação em Agronomia (Energia na Agricultura) - FCA

Tar reduction in downdraft biomass gasifier using a primary method

Coordenação de Aperfeiçoamento de Pessoal de Nível Superior (CAPES)

Bioenergy from stillage anaerobic digestion to enhance the energy balance ratio of ethanol production

Fundação de Amparo à Pesquisa do Estado de São Paulo (FAPESP)

Biomass Gasification - Process analysis and dimensioning aspects for downdraft units and gas cleaning lines

In such territories where food production is mostly scattered in several small / medium size or even domestic farms, a lot of heterogeneous residues are produced yearly, since farmers usually carry out different activities in their properties. The amount and composition of farm residues, therefore, widely change during year, according to the single production process periodically achieved. Coupling high efficiency micro-cogeneration energy units with easy handling biomass conversion equipments, suitable to treat different materials, would provide many important advantages to the farmers and to the community as well, so that the increase in feedstock flexibility of gasification units is nowadays seen as a further paramount step towards their wide spreading in rural areas and as a real necessity for their utilization at small scale. Two main research topics were thought to be of main concern at this purpose, and they were therefore discussed in this work: the investigation of fuels properties impact on gasification process development and the technical feasibility of small scale gasification units integration with cogeneration systems. According to these two main aspects, the present work was thus divided in two main parts. The first one is focused on the biomass gasification process, that was investigated in its theoretical aspects and then analytically modelled in order to simulate thermo-chemical conversion of different biomass fuels, such as wood (park waste wood and softwood), wheat straw, sewage sludge and refuse derived fuels. The main idea is to correlate the results of reactor design procedures with the physical properties of biomasses and the corresponding working conditions of gasifiers (temperature profile, above all), in order to point out the main differences which prevent the use of the same conversion unit for different materials. At this scope, a gasification kinetic free model was initially developed in Excel sheets, considering different values of air to biomass ratio and the downdraft gasification technology as particular examined application. The differences in syngas production and working conditions (process temperatures, above all) among the considered fuels were tried to be connected to some biomass properties, such elementary composition, ash and water contents. The novelty of this analytical approach was the use of kinetic constants ratio in order to determine oxygen distribution among the different oxidation reactions (regarding volatile matter only) while equilibrium of water gas shift reaction was considered in gasification zone, by which the energy and mass balances involved in the process algorithm were linked together, as well. Moreover, the main advantage of this analytical tool is the easiness by which the input data corresponding to the particular biomass materials can be inserted into the model, so that a rapid evaluation on their own thermo-chemical conversion properties is possible to be obtained, mainly based on their chemical composition A good conformity of the model results with the other literature and experimental data was detected for almost all the considered materials (except for refuse derived fuels, because of their unfitting chemical composition with the model assumptions). Successively, a dimensioning procedure for open core downdraft gasifiers was set up, by the analysis on the fundamental thermo-physical and thermo-chemical mechanisms which are supposed to regulate the main solid conversion steps involved in the gasification process. Gasification units were schematically subdivided in four reaction zones, respectively corresponding to biomass heating, solids drying, pyrolysis and char gasification processes, and the time required for the full development of each of these steps was correlated to the kinetics rates (for pyrolysis and char gasification processes only) and to the heat and mass transfer phenomena from gas to solid phase. On the basis of this analysis and according to the kinetic free model results and biomass physical properties (particles size, above all) it was achieved that for all the considered materials char gasification step is kinetically limited and therefore temperature is the main working parameter controlling this step. Solids drying is mainly regulated by heat transfer from bulk gas to the inner layers of particles and the corresponding time especially depends on particle size. Biomass heating is almost totally achieved by the radiative heat transfer from the hot walls of reactor to the bed of material. For pyrolysis, instead, working temperature, particles size and the same nature of biomass (through its own pyrolysis heat) have all comparable weights on the process development, so that the corresponding time can be differently depending on one of these factors according to the particular fuel is gasified and the particular conditions are established inside the gasifier. The same analysis also led to the estimation of reaction zone volumes for each biomass fuel, so as a comparison among the dimensions of the differently fed gasification units was finally accomplished. Each biomass material showed a different volumes distribution, so that any dimensioned gasification unit does not seem to be suitable for more than one biomass species. Nevertheless, since reactors diameters were found out quite similar for all the examined materials, it could be envisaged to design a single units for all of them by adopting the largest diameter and by combining together the maximum heights of each reaction zone, as they were calculated for the different biomasses. A total height of gasifier as around 2400mm would be obtained in this case. Besides, by arranging air injecting nozzles at different levels along the reactor, gasification zone could be properly set up according to the particular material is in turn gasified. Finally, since gasification and pyrolysis times were found to considerably change according to even short temperature variations, it could be also envisaged to regulate air feeding rate for each gasified material (which process temperatures depend on), so as the available reactor volumes would be suitable for the complete development of solid conversion in each case, without even changing fluid dynamics behaviour of the unit as well as air/biomass ratio in noticeable measure. The second part of this work dealt with the gas cleaning systems to be adopted downstream the gasifiers in order to run high efficiency CHP units (i.e. internal engines and micro-turbines). Especially in the case multi–fuel gasifiers are assumed to be used, weightier gas cleaning lines need to be envisaged in order to reach the standard gas quality degree required to fuel cogeneration units. Indeed, as the more heterogeneous feed to the gasification unit, several contaminant species can simultaneously be present in the exit gas stream and, as a consequence, suitable gas cleaning systems have to be designed. In this work, an overall study on gas cleaning lines assessment is carried out. Differently from the other research efforts carried out in the same field, the main scope is to define general arrangements for gas cleaning lines suitable to remove several contaminants from the gas stream, independently on the feedstock material and the energy plant size The gas contaminant species taken into account in this analysis were: particulate, tars, sulphur (in H2S form), alkali metals, nitrogen (in NH3 form) and acid gases (in HCl form). For each of these species, alternative cleaning devices were designed according to three different plant sizes, respectively corresponding with 8Nm3/h, 125Nm3/h and 350Nm3/h gas flows. Their performances were examined on the basis of their optimal working conditions (efficiency, temperature and pressure drops, above all) and their own consumption of energy and materials. Successively, the designed units were combined together in different overall gas cleaning line arrangements, paths, by following some technical constraints which were mainly determined from the same performance analysis on the cleaning units and from the presumable synergic effects by contaminants on the right working of some of them (filters clogging, catalysts deactivation, etc.). One of the main issues to be stated in paths design accomplishment was the tars removal from the gas stream, preventing filters plugging and/or line pipes clogging At this scope, a catalytic tars cracking unit was envisaged as the only solution to be adopted, and, therefore, a catalytic material which is able to work at relatively low temperatures was chosen. Nevertheless, a rapid drop in tars cracking efficiency was also estimated for this same material, so that an high frequency of catalysts regeneration and a consequent relevant air consumption for this operation were calculated in all of the cases. Other difficulties had to be overcome in the abatement of alkali metals, which condense at temperatures lower than tars, but they also need to be removed in the first sections of gas cleaning line in order to avoid corrosion of materials. In this case a dry scrubber technology was envisaged, by using the same fine particles filter units and by choosing for them corrosion resistant materials, like ceramic ones. Besides these two solutions which seem to be unavoidable in gas cleaning line design, high temperature gas cleaning lines were not possible to be achieved for the two larger plant sizes, as well. Indeed, as the use of temperature control devices was precluded in the adopted design procedure, ammonia partial oxidation units (as the only considered methods for the abatement of ammonia at high temperature) were not suitable for the large scale units, because of the high increase of reactors temperature by the exothermic reactions involved in the process. In spite of these limitations, yet, overall arrangements for each considered plant size were finally designed, so that the possibility to clean the gas up to the required standard degree was technically demonstrated, even in the case several contaminants are simultaneously present in the gas stream. Moreover, all the possible paths defined for the different plant sizes were compared each others on the basis of some defined operational parameters, among which total pressure drops, total energy losses, number of units and secondary materials consumption. On the basis of this analysis, dry gas cleaning methods proved preferable to the ones including water scrubber technology in al of the cases, especially because of the high water consumption provided by water scrubber units in ammonia adsorption process. This result is yet connected to the possibility to use activated carbon units for ammonia removal and Nahcolite adsorber for chloride acid. The very high efficiency of this latter material is also remarkable. Finally, as an estimation of the overall energy loss pertaining the gas cleaning process, the total enthalpy losses estimated for the three plant sizes were compared with the respective gas streams energy contents, these latter obtained on the basis of low heating value of gas only. This overall study on gas cleaning systems is thus proposed as an analytical tool by which different gas cleaning line configurations can be evaluated, according to the particular practical application they are adopted for and the size of cogeneration unit they are connected to.

Air-steam gasification of sewage sludge in a bubbling bed reactor: Effect of alumina as a primary catalyst

Numerous references can be found in scientific literature regarding biomass gasification. However, there are few works related to sludge gasification. A study of sewage sludge gasification process in a bubbling fluidised bed gasifier on a laboratory scale is here reported. The aim was to find the optimum conditions for reducing the production of tars and gain more information on the influx of different operating variables in the products resulting from the gasification of this waste. The variables studied were the equivalence ratio (ER), the steam-biomass ratio (SB) and temperature. Specifically, the ER was varied from 0.2 to 0.4, the SB from 0 to 1 and the temperature from 750 °C (1023 K) to 850 °C (1123 K). Although it was observed that tar production could be considerably reduced (up to 72%) by optimising the gasification conditions, the effect of using alumina (aluminium oxide, of proven efficacy in destroying the tar produced in biomass gasification) as primary catalyst in air and air-steam mixture tests was also verified. The results show that by adding small quantities of alumina to the bed (10% by weight of fed sludge) considerable reductions in tar production can be obtained (up to 42%) improving, at the same time, the lower heating value (LHV) of the gas and carbon conversion.

Utilización del cultivo plurianual de pataca (Helianthus tuberosus L.) para la producción de hidratos de carbono fermentables a partir de los tallos

La pataca (Helianthus tuberosus L.) es una especie de cultivo con un alto potencial en la producción de hidratos de carbono de reserva en forma de polifructanos, especialmente inulina, que se acumulan temporalmente en los tallos en forma de polisacáridos para translocarse posteriormente a los tubérculos, donde son almacenados. Aunque tradicionalmente el producto de interés del cultivo son los tubérculos, que acumulan gran cantidad de hidratos de carbono fermentables (HCF) cuando se recogen al final del ciclo de desarrollo, en este trabajo se pretende evaluar el potencial de la pataca como productor de HCF a partir de los tallos cosechados en el momento de máximo contenido en HCF, mediante un sistema de cultivo plurianual. Se han realizado los siguientes estudios: i) Determinación del momento óptimo de cosecha en ensayos con 12 clones ii) Potencial del cultivo plurianual de la pataca en términos de producción anual de biomasa aérea y de HCF en cosechas sucesivas, iii) Ensayos de conservación de la biomasa aérea, iv) Estimación de los costes de las dos modalidades de cultivo de pataca para producción de HCF y v) Estimación de la sostenibilidad energética de la producción de bioetanol mediante la utilización de los subproductos. Para la determinación del momento óptimo de la cosecha de la biomasa aérea se ensayaron 12 clones de diferente precocidad en Madrid; 4 tempranos (Huertos de Moya, C-17, Columbia y D-19) y 8 tardíos (Boniches, China, K-8, Salmantina, Nahodka, C-13, INIA y Violeta de Rennes). El máximo contenido en HCF tuvo lugar en el estado fenológico de botón floral-flor que además coincidió con la máxima producción de biomasa aérea. De acuerdo con los resultados obtenidos, la cosecha de los clones tempranos se debería realizar en el mes de julio y en los clones tardíos en septiembre, siendo éstos últimos más productivos. La producción media más representativa entre los 12 clones, obtenida en el estado fenológico de botón floral fue de 23,40 t ms/ha (clon INIA), con un contenido medio en HCF de 30,30 % lo que supondría una producción potencial media de 7,06 t HCF/ha. La producción máxima en HCF se obtuvo en el clon Boniches con 7,61 t/ha y 22,81 t ms/ha de biomasa aérea. En el sistema de cultivo plurianual la cantidad de tallos por unidad de superficie aumenta cada año debido a la cantidad de tubérculos que van quedando en el terreno, sobre todo a partir del 3er año, lo que produce la disminución del peso unitario de los tallos, con el consiguiente riesgo de encamado. El aclareo de los tallos nacidos a principios de primavera mediante herbicidas tipo Glifosato o mediante una labor de rotocultor rebaja la densidad final de tallos y mejora los rendimientos del cultivo. En las experiencias de conservación de la biomasa aérea se obtuvo una buena conservación por un período de 6 meses de los HCF contenidos en los tallos secos empacados y almacenados bajo cubierta. Considerando que el rendimiento práctico de la fermentación alcohólica es de 0,5 l de etanol por cada kg de azúcar, la producción potencial de etanol para una cosecha de tallos de 7,06 t de HCF/ha sería de 3.530 l/ha. El bagazo producido en la extracción de los HCF de la biomasa aérea supondría 11,91 t/ha lo que utilizado para fines térmicos supone más de 3 veces la energía primaria requerida en el proceso de producción de etanol, considerando un poder calorífico inferior de 3.832,6 kcal/kg. Para una producción de HCF a partir de la biomasa aérea de 7,06 t/ha y en tubérculos al final del ciclo de 12,11 t/ha, los costes de producción estimados para cada uno de ellos fueron de 184,69 €/t para los HCF procedentes de la biomasa aérea y 311,30 €/t para los de tubérculos. Como resultado de este trabajo se puede concluir que la producción de HCF a partir de la biomasa aérea de pataca en cultivo plurianual, es viable desde un punto de vista técnico, con reducción de los costes de producción respecto al sistema tradicional de cosecha de tubérculos. Entre las ventajas técnicas de esta modalidad de cultivo, cabe destacar: la reducción de operaciones de cultivo, la facilidad y menor coste de la cosecha, y la posibilidad de conservación de los HCF en la biomasa cosechada sin mermas durante varios meses. Estas ventajas, compensan con creces el menor rendimiento por unidad de superficie que se obtiene con este sistema de cultivo frente al de cosecha de los tubérculos. Jerusalem artichoke (Helianthus tuberosus L.) (JA) is a crop with a high potential for the production of carbohydrates in the form of polyfructans, especially inulin, which are temporarily accumulated in the stems in the form of polysaccharides. Subsequently they are translocated to the tubers, where they are finally accumulated. In this work the potential of Jerusalem artichoke for fermentable carbohydrates from stems that are harvested at their peak of carbohydrates accumulation is assessed as compared to the traditional cultivation system that aims at the production of tubers harvested at the end of the growth cycle. Tubers are storage organs of polyfructans, namely fermentable carbohydrates. Studies addressed in this work were: i) Determination of the optimum period of time for stem harvesting as a function of clone precocity in a 12-clone field experiment; ii) Study of the potential of JA poly-annual crop regarding the annual yield of aerial biomass and fermentable carbohydrates (HCF) over the years; iii) Tests of storage of the aerial biomass, iv) Comparative analysis of the two JA cultivation systems for HCF production: the poly-annual system for aerial biomass harvesting versus the annual cultivation system for tubers and v) Estimation of the energy sustainability of the bioethanol production by using by-products of the production chain. In order to determine the best period of time for aerial biomass harvesting twelve JA clones of different precocity were tested in Madrid: four early clones (Huertos de Moya, C-17, Columbia and D-19) and eight late clones (Boniches, China, K-8 , Salmantina, Nahodka, C-13, INIA and Violeta de Rennes). Best time was between the phenological stages of floral buds (closed capitula) and blossom (opened capitula), period in which the peak of biomass production coincides with the peak of HCF accumulation in the stems. According to the results, the early clones should be harvested in July and the late ones in September, being the late clones more productive. The clone named INIA was the one that exhibited more steady yields in biomass over the 12 clones experimented. The average potential biomass production of this clone was 23.40 t dm/ha when harvested at the floral buds phenological stage; mean HCF content is 30.30%, representing 7.06 t HCF/ha yield. However, the highest HCF production was obtained for the clone Boniches, 7.61 t HCF/ha from a production of 22.81 t aerial biomass/ha. In the poly-annual cultivation system the number of stems per unit area increases over the years due to the increase in the number of tubers that are left under ground; this effect is particularly important after the 3rd year of the poly-annual crop and results in a decrease of the stems unit weight and a risk of lodging. Thinning of JA shoots in early spring, by means of an herbicide treatment based on glyphosate or by means of one pass with a rotary tiller, results in a decrease of the crop stem density and in higher crop yields. Tests of biomass storing showed that the method of keeping dried stems packed and stored under cover results in a good preservation of HCF for a period of six months at least. Assuming that the fermentation yield is 0.5 L ethanol per kg sugars and a HCF stem production of 7.06 t HCF/ha, the potential for bioethanol is estimated at 3530 L/ha. The use of bagasse -by-product of the process of HCF extraction from the JA stems- for thermal purposes would represent over 3 times the primary energy required for the industrial ethanol production process, assuming 11.91 t/ha bagasse and 3832.6 kcal/kg heating value. HCF production costs of 7.06 t HCF/ha yield from aerial biomass and HCF production costs of 12.11 t HCF/ha from tubers were estimated at 184.69 €/t HCF and 311.30 €/t HCF, respectively. It can be concluded that the production of HCF from JA stems, following a poly-annual cultivation system, can be feasible from a technical standpoint and lead to lower production costs as compared to the traditional annual cultivation system for the production of HCF from tubers. Among the technical advantages of the poly-annual cultivation system it is worth mentioning the reduction in crop operations, the ease and efficiency of harvesting operations and the possibility of HCF preservation without incurring in HCF losses during the storage period, which can last several months. These advantages might compensate the lower yield of HCF per unit area that is obtained in the poly-annual crop system, which aims at stems harvesting, versus the annual one, which involves tubers harvesting.

Biokerosene from Babassu and Camelina Oils: production and properties of their blends with fossil kerosene

Babassu and camelina oils have been transesterified with methanol by the classical homogeneous basic catalysis method with good yields. The babassu fatty acid methyl ester (FAME) has been subjected to fractional distillation at vacuum, and the low boiling point fraction has been blended with two types of fossil kerosene, a straight-run atmospheric distillation cut (hydrotreated) and a commercial Jet-A1. The camelina FAME has been blended with the fossil kerosene without previous distillation. The blends of babassu biokerosene and Jet-A1 have met some of the specifications selected for study of the ASTM D1655 standard: smoke point, density, flash point, cloud point, kinematic viscosity, oxidative stability and lower heating value. On the other hand, the blends of babassu biokerosene and atmospheric distillation cut only have met the density parameter and the oxidative stability. The blends of camelina FAME and atmospheric distillation cut have met the following specifications: density, kinematic viscosity at −20 °C, and lower heating value. With these preliminary results, it can be concluded that it would be feasible to blend babassu and camelina biokerosenes prepared in this way with commercial Jet-A1 up to 10 vol % of the former, if these blends prove to accomplish all the ASTM D1655-09 standards.