Integrated catalytic adsorption (ICA) steam gasification system for enhanced hydrogen production using palm kernel shell

This paper investigates the integrated catalytic adsorption (ICA) steam gasification of palm kernel shell for hydrogen rich gas production using pilot scale fluidized bed gasifier under atmospheric condition. The effect of temperature (600–750 °C) and steam to biomass ratio (1.5–2.5 wt/wt) on hydrogen (H₂) yield, product gas composition, gas yield, char yield, gasification and carbon conversion efficiency, and lower heating values are studied. The results show that H₂ hydrogen composition of 82.11 vol% is achieved at temperature of 675 °C, and negligible carbon dioxide (CO₂) composition is observed at 600 °C and 675 °C at a constant steam to biomass ratio of 2.0 wt/wt. In addition, maximum H₂ yield of 150 g/kg biomass is observed at 750 °C and at steam to biomass ratio of 2.0 wt/wt. A good heating value of product gas which is 14.37 MJ/Nm³ is obtained at 600 °C and steam to biomass ratio of 2.0 wt/wt. Temperature and steam to biomass ratio both enhanced H₂ yield but temperature is the most influential factor. Utilization of adsorbent and catalyst produced higher H₂ composition, yield and gas heating values as demonstrated by biomass catalytic steam gasification and steam gasification with in situ CO₂ adsorbent.     

城市生活垃圾原位水蒸气气化制氢研究

在固定床反应器中对城市生活垃圾进行原位水蒸气气化制氢研究,考察了加热方式、反应温度以及含水率对城市生活垃圾原位水蒸气气化特性的影响。结果表明,快加热方式有利于提高燃气品质和降低焦油含量;随着反应温度的增加,气体产物含量增加,焦油含量和半焦含量下降,气体组分中H2和CO含量升高,碳转化率从30.49%增加到56.79%;当城市生活垃圾含水率为39.45%时,产气品质最高,气体成分中H2含量达到最高值25.8%,气体的低位热值达到17.02 MJ/m3;温度升高和蒸汽引入能改变半焦产物的表观形貌,并能提高半焦产物的BET以及灰分含量。     

A CFD approach on simulation of hydrogen production from steam reforming of glycerol in a fluidized bed reactor

Hydrogen production from steam reforming of glycerol in a fluidized bed reactor has been simulated using a CFD method by an additional transport equation with a kinetic term. The Eulerian–Eulerian two-fluid approach was adopted to simulate hydrodynamics of fluidization, and chemical reactions were modelled by laminar finite-rate model. The bed expansion and pressure drop were predicted for different inlet gas velocities. The results showed that the flow system exhibited a more heterogeneous structure, and the core-annulus structure of gas–solid flow led to back-mixing and internal circulation behaviour, and thus gave a poor velocity distribution. This suggests the bed should be agitated to maintain satisfactory fluidizing conditions. Glycerol conversion and H₂ production were decreased with increasing inlet gas velocity. The increase in the value of steam to carbon molar ratio increases the conversion of glycerol and H₂ selectivity. H₂ concentrations in the bed were uneven and increased downstream and high concentrations of H₂ production were also found on walls. The model demonstrated a relationship between hydrodynamics and hydrogen production, implying that the residence time and steam to carbon molar ratio are important parameters. The CFD simulation will provide helpful data to design and operate a bench scale catalytic fluidized bed reactor.     

Energy and exergy analysis and optimization of biomass gasification process for hydrogen production (based on air,steam and air/steam gasifying agents)

Growing the consumption of fossil fuels and emerging global warming issue have driven the research interests toward renewable and environmentally friendly energy sources. Biomass gasification is identified as an efficient technology to produce sustainable hydrogen. In this work, energy and exergy analysis coupled with thermodynamic equilibrium model were implemented in biomass gasification process for production of hydrogen. In this regard, a detailed comparison of the performance of a downdraft gasifier was implemented using air, steam, and air/steam as the gasifying agents for horse manure, pinewood and sawdust as the biomass materials. The comparison results indicate that the steam gasification of pinewood generates a more desired product gas compositions with a much higher hydrogen exergy efficiency and low exergy values of unreacted carbon and irreversibility. Then the effects of the inherent operating factors were investigated and optimized applying a response surface methodology to maximize hydrogen exergy efficiency of the process. A hydrogen exergy efficiency of 44% was obtained when the product gas exergy efficiency reaches to the highest value (88.26%) and destruction and unreacted carbon efficiencies exhibit minimum values of 7.96% and 1.9%.     

Hydrogen-rich gas from catalytic steam gasification of municipal solid waste (MSW): Influence of steam to MSW ratios and weight hourly space velocity on gas production and composition

The present work deals with a study coupling experiments and modeling of catalytic steam gasification of municipal solid waste (MSW) for producing hydrogen-rich gas or syngas (H₂ + CO) with calcined dolomite as a catalyst in a bench-scale downstream fixed bed reactor. The influence of steam to MSW ratios (S/M) on gas production and composition was studied at 900 °C over the S/M range of 0.39–1.04, for weight hourly space velocity (WHSV) in the range of 1.22–1.51 h⁻¹. Over the ranges of experimental conditions examined, calcined dolomite revealed better catalytic performance at the presence of steam. H₂ and CO₂ contents increased with S/M increasing, while CO and CH₄ contents decreased sharply, the contents of CH₄, C₂H₄ and C₂H₆ were relatively small, and the influence of S/M was insignificant. The highest H₂ content of 53.22 mol %, the highest H₂ yield of 42.98 mol H₂/kg MSW, and the highest H₂ potential yield of 59.83 mol H₂/kg MSW were achieved at the highest S/M level of 1.04. Furthermore, there was a good agreement between the experimental gas composition and that corresponding to thermodynamic equilibrium data calculated using GasEq model. Consequently, a kinetic model was proposed for describing the variation of H₂ yield and carbon conversion efficiency with S/M during the catalytic steam gasification of MSW. The kinetic model revealed a good performance between experimental results and the kinetic model.     

Comparison of Response Surface Methodology (RSM) and Artificial Neural Network (ANN) in modelling of waste coconut oil ethyl esters production

The attributes of renewability and environmental friendliness have made ethanol a preferable alternative to methanol in the production of biodiesel from lipid feedstocks. For the first time, this study adopted Response Surface Methodology (RSM) and Artificial Neural Network (ANN) to model coconut oil ethyl ester (CNOEE) yield. Transesterification parameters such as reaction temperature and ethanol/coconut oil molar ratio and catalyst dosage were varied. Maximum CNOEE yield of 96.70% was attained at 73 °C reaction temperature, 11.9:1 molar ratio, and catalyst dosage of 1.25 wt. %. The experimental yield was in agreement with the predicted yield. Central Composite Design was adopted to develop the RSM while feed-forward back propagation neural network algorithm was employed for the ANN model. Statistical indices were employed to compare the models. The computed coefficient of determination (R²) of 0.9564, root-mean-squarce-error (RMSE) of 0.72739, standard error of prediction (SEP) of 0.008021, mean average error (MAE) of 0.612, and average absolute deviation (AAD) of 0.674901 for RSM model compared to those of R² (0.9980), RMSE (0.68615), SEP (0.007567), MAE (0.325), and AAD (0.3877) for ANN indicated the superiority of the ANN model over the RSM model. The key fuel properties of the CNOEE met with those of biodiesel international standards.     

Effects of catalyst preparation route and promoters (Ce and Zr) on catalytic activity of CuZn/CNTs catalysts for hydrogen production from methanol steam reforming

Ce or Zr promoted CuZn/CNTs (carbon nanotubes) catalysts were synthesized by microwave-assisted polyol, co-precipitation and impregnation methods and were used to generate hydrogen by methanol steam reforming (MSR) process. The physico-chemical properties of the prepared catalysts were analyzed by BET, XRD, FT-IR, TEM, FE-SEM, EDX-dot mapping and H₂-TPR methods. The effect of various operating parameters on methanol conversion and selectivity of gaseous products was investigated. The results indicated that the addition of 2 wt% CeO₂ promoter on CuZn/CNTs catalyst synthesized by impregnation route (CuZn/CNTs (Imp)) increased its methanol conversion from 81.3 to 85.2%, and decreased its CO selectivity from 6.2 to 3.8% at 300 °C, WHSV of 7.5 h^?1 and S/C molar ratio of 2. In addition, the CeCuZn/CNTs catalyst prepared via the microwave-assisted polyol route (CeCuZn/CNTs (Pol)) exhibited the best catalytic activity with 98.2% hydrogen selectivity, 2.6% CO selectivity and 94.2% methanol conversion at 300 °C. Furthermore, a 48 h continuous MSR reaction at 300 °C, identified CeCuZn/CNTs (Pol) as the most stable catalyst due to its higher metal particle dispersion and better interaction between the active phase and the CNTs support.     

Effect of nickel loading on hydrogen production and chemical oxygen demand (COD) destruction from glucose oxidation and gasification in supercritical water

Gasification and partial oxidation of 0.25 molar glucose solution was conducted over different metallic nickel (Ni) loadings (7.5, 11, and 18 wt%) on different catalyst supports (θ-Al₂O₃ and γ-Al₂O₃) in supercritical water. Experiments were carried out at three different temperatures (T) of 400, 450, and 500 °C at constant pressure of 28 MPa and a 30 min reaction time (t). For comparison, some experiments were conducted using high loading commercial catalyst (65 wt% Ni on Silica–alumina). Hydrogen peroxide (H₂O₂) was used as a source of oxygen in the partial oxidation experiments. Oxygen to carbon molar ratios (MR) of 0.5–0.9 were examined to increase the hydrogen production via carbon monoxide (CO) production. Results showed that in the absence of the catalyst, the optimum molar ratio was 0.8 i.e. 80% of the amount of oxygen required for complete oxidation of glucose. At a molar ratio of 0.8, the hydrogen yield was 0.3 mol/mol, as compared to 0.2 mol/mol glucose at molar ratio of 0.5 and 0.9. This optimized oxygen dose was adopted as a base line for catalysts evaluation. The main gaseous products were carbon dioxide (CO₂), carbon monoxide (CO), hydrogen (H₂), and methane (CH₄). Results also showed that the presence of Ni increased the total gas yield increased in the 7.5–18 wt Ni/Al₂O₃ catalyst. An increase in MR from 0.55 to 0.8 increased the of carbon dioxide and hydrogen yields from 1.8 to 3.8 mol/mol glucose and from 0.9 to 1.1 mol/mol. The carbon monoxide and methane yields remain constant at 2 and 0.5 mol/mol glucose, respectively. The introduction of hydrogen peroxide (H₂O₂) prior to the feed injection inhibited the catalyst activity and did not increase the hydrogen yield whereas the introduction of H₂O₂ after 15 min of reaction time increased the hydrogen yield from 0.62 mol/mol to 1.5 mol/mol. This study showed that approximately the same hydrogen yield can be obtained from the synthesized low nickel alumina loading (18 wt%) catalyst as with the 65 wt% nickel on silica–alumina loading commercial catalyst. The highest H₂ yield of 1.5 mol/mol glucose was obtained with commercial Ni/silica–alumina with a BET surface area of 190 m²/g compared to 1.2 mol/mol with the synthesized Ni/θ alumina with a BET surface area of 46 m²/g.     

Energy,exergy, economic and environmental (4-E) analyses of plasma gasification steam cycle integrated molten carbonate fuel cell for hydrogen and power co-generation based on residual waste feedstocks

Two newly emerging technologies: (a) plasma gasification and (b) molten carbonate fuel cell (MCFC) are integrated for hydrogen and power production for various system configurations. Due to the emission concerns of fossil fuels, wastes such as refused derived fuel (RDF) is chosen as feedstock. The simulation of the power plants is performed using Aspen plus and consequently, 4-E (energy, exergy, economic and environmental) analyses are executed. The highest energy and exergy efficiencies attained are 54.12% and 52.02% for the system Syngas:CH₄ [PSA: MCFC], respectively. Moreover, the cost of electricity considering all the configurations is ranged between 77.48 and 107.93 $/MWh while the LCOH is between 1.01 and 3.94 $/kg. Likewise, introduction of MCFC for 0:100 [PSA: MCFC] case reduced the annual CO₂ emissions ∼5 times than of 100:0. Therefore, the 4-E analyses reported that integrated plasma gasification with MCFC introducing waste as feed could possibly favour H₂ and power co-generation and a cleaner environment.     

Hydrogen-rich gas production by steam gasification of char derived from cyanobacterial blooms (CDCB) in a fixed-bed reactor: Influence of particle size and residence time on gas yield and syngas composition

Char derived from cyanobacterial blooms (CDCB), by-product of fast pyrolysis of cyanobacterial blooms from Dianchi Lake (Yunnan Province, China) at a final pyrolysis temperature of 500 °C were used as feedstock material in this study. Steam gasification characteristics of CDCB were investigated in a fixed-bed reactor to evaluate the effect of particle size (below 0.15 mm, 0.15–0.3 mm, 0.3–0.45 mm, 0.45–0.9 mm, 0.9–3 mm) and solid residence time (3, 6, 9, 12, 15 min) on gas yield and composition, and experiments were carried out at bed temperature range of 600–850 °C, steam flow rate of 0.178 g/min. The results showed that solid residence time played an important role on steam gasification process, while particle size presented less effect on gasification process; proper particle size and longer residence time were favorable for dry gas yield and carbon conversion efficiency (CCE). At the same time, higher reaction temperature reduced influence of particle size on gasification process, and smaller particle size required less residence time for reaction completed. Maximum dry gas yield and CCE reached 1.84 Nm³ kg⁻¹ and 98.82%, respectively, achieved at a temperature of 850 °C, flow rate of 0.178 g/min, solid residence time of 15 min and particle size range of 0.45–0.9 mm.