Abstract: Understanding the concentrations and origins of trace elements in coal is both practically and theoretically significant in the utilization of potentially valuable trace metals in coal combustion byproducts and revealing origins of coalformation. The contents, occurrence modes, and origin of trace elements in the Late Permian coals from the Puan Coalfield of western Guizhou Province were studied using inductively coupledplasma mass spectrometry (ICPMS), Xray fluorescence spectrometry (XRF), coldvapor atomic absorption spectrometry (CVAAS), atomic fluorescence spectrometry (AFS), ionselective spectrometry (ISF), scanning electron microscope equipped with dispersive Xray energy (SEMEDX), and sequential chemical extraction technology (SCET). The results show that minerals in the No.2 coal are mainly pyrite of lowtemperature hydrothermal origin and clay minerals of detrital terrigenous origin. The pyrite in the No.2 coal mainly occurs as fracturefillings and clay minerals as lenses and fine particles in collodetrinite. The elements including As 〖ＷＴＢＺ〗(36.9×10－6), Cd (10.2×10－6), Cr (167.3×10－6), Cu (365.4×10－6), Hg (2.82×10－6), Mo (92.6×10－6), Ni (82.6×10－6), Pb (184.6×10－6), Se (6.23×10－6), Zn (242.3×10－6), and U (54.6×10－6), 〖ＷＴＢ１〗are significantly enriched in the coal, as compared with those in coals from Guizhou, China, and USA. However, the contents of trace elements in the other 4 coals (No.1, No.3, No.4, and No.5) are close to those in coals from Guizhou, China, and USA. Elements of As, Cd, Hg, Ni, Pb, and Zn in No.2 coal mainly distribute in pyrite, and Cr, Cu and U are mainly in kaolinite, indicating that the lowtemperature hydrothermal fluid and detrital material of terrigenous origin play a critical role in the contents and occurrence modes of trace elements in the No.2 coal.
Abstract: A furnace equipped with a removable measuring scale in the side was applied to study on the shrinkage characteristics of semicoke/coke under gradient temperature during coking process. 1500g coking coal was used in the test. The effects of coking time, central temperature, heatingup rate and gradient temperature on lateral shrinkage were studied under different heating rates (1.0℃/min, 1.5℃/min and 3.0℃/min) and densities (880kg/m3 and 1080kg/m3), respectively. The results show that the coal begins to shrink at a central temperature range of 280℃～360℃ and ends at about 900℃. The lateral shrinkage is in a range of 5mm～8.5mm and lateral shrinkage ratio is 7%~12%. Generally, the gradient temperature increases and lateral shrinkage decreases with increasing heatingup rate and density. The central temperature of beginning shrinkage, the second shrinkage peak, gradient temperature of different locations and shrinkage coefficient of coal decreases with the increase of heating rate. The central temperature of beginning shrinkage and gradient temperature of different locations increase with increasing density. But the increase of density has no influence on shrinkage coefficient and shrinkage peak. In addition, the temperature rise rates at different locations are different during different coking stages.
Abstract: The rule of sulfur dimensional distribution in coke was studied by simulating the industrial coking process using coking coal. The result show that the content of organic sulfur and inorganic sulfur increases gradually from the center to the brim at the same height of the coke column. The content of organic sulfur and inorganic sulfur in the crack section is higher than that in the interior section at the same position. The increased quantity of organic sulfur and inorganic sulfur is about 0.035% and 0.08% in the test with a diameter 230mm coking reactor. XPS analysis shows that the different content of organic sulfur and inorganic sulfur is resulted from the different content of sulfide sulfur and thiophenic sulfur. The rule is approved further by the twodimensional simulation experiment.
Abstract: The effective utilization of residue from direct coal liquefaction is important in both economic and environmental concern. Gasification behavior of Shenhua coal and the residues from the direct liquefaction of the Shenhua coal was investigated and compared using a fluidized bed reactor combined with gas chromatography (GC) analysis. The effect of remained and enriched mineral, catalyst and heavy oil on CO2 gasification of residue char was examined. The results show that the residue char has a better gasification activity than the raw coal char. The gasification reactivity index of the residue char is 0.135 and 0.290 at 1000℃ and 1100℃，respectively; but that of raw coal char is 0.118 and 0.20, respectively. The gasification reactivity of acid washed residue char (AR) is lower than that of acid washed coal char (AC), but the gasification reactivity of untreated residue char is greater than that of the raw coal char, which indicates that the remained and enriched mineral is a good catalyst for residue gasification. The Febased catalyst added during direct liquefaction also has a catalytic effect on the gasification process. Removal of heavy oil from the liquefaction residue leads to the decrease of the gasification reactivity of residue char.
Abstract: Emissions of NO, N2O and SO2 during coal combustion in a 30kW scale circulating fluidized bed (CFB) combustor were experimentally investigated. Three kinds of coals from western China were tested. The CFB combustor consists of a riser and a downer. The riser was designed as the coal combustor and the downer was used for the solid material circulation. The influence of combustion temperature, excess air number, air staging and coal rank on the emissions of NO, N2O and SO2 were studied and discussed. The experimental results show that increasing the combustion temperature can result in an increase of NO and a decrease of N2O in the flue gas. Air staging can decrease the NO emission significantly, but no obvious changing of N2O emission is found during the combustion of coal with high volatile content. Increasing the excess air number can lead to an increase of NO and N2O emission. A large decrease of NO emission and a slight increase of N2O emission can be observed when increasing the char concentration in the riser. About 85% percent of fuelN is converted to N2 for the combustion tests performed at 1120K and with the excess air number of 1.25. However, no obvious variation is observed for SO2 and CO emission with changing the CFB operation parameters, such as excess air and air staging.
Abstract: The Zeta potential of dispersion system forming by 10 dispersants with 14 coals was determined. The effect of dispersant on the interface electrochemical property of coal particles was studied. The higher the coal rank and the more the dissolved highvalence cations from coal, the lower the Zeta potential of dispersantmodified coal particle. The more the amount of hydrophilic groups and the charge of the anionic dispersant, the higher the Zeta potential of dispersantmodified coal particle. The nonionic dispersant leads to a decrease in the Zeta potential of dispersantmodified coal particle. In general, the Zeta potential of anionic dispersantmodified coal reflects its hydrophilicity. The maximum moisture content for most of dispersantmodified coal particles increases with increasing Zeta potentials. An experiential slurryability model including natural and dispersantmodified hydrophilicity of coal particle (Mad,ΔMHC), the Zeta potential of dispersantmodified coal particle (ζ) and the adsorption amount of dispersant on unit surface area of coal (Гs ) has been set up. It can be expressed as following: CFV = 76.621.896Mad 3.430△MHC+0.489Γs·ζ. The calculated value from this formula is approximate to the experimental result.
Abstract: The USY FCC catalyst was modified by MgO for changing the matrix structure to improve the performance of sulfur transfer and was modified by Ce2O3, La2O3 and P2O5 for enhancing the activity of sulfur transfer. The properties of modified catalyst were investigated by FTIR. The effect of MgO, Ce2O3, La2O3 and P2O5 on the activity of sulfur transfer and catalytic cracking reaction were investigated. The result show that the modified catalyst keeps up good activity of sulfur transfer which is kept more than 6% after many times of oxidationreduction cycle. The introduction of a few MgO decreases the amount of stronger acid on the surface of matrix and zeolite, but does not greatly influence the activity of catalytic cracking reaction. The introduction of rare earth metal increases acid amount of the matrix and zeolite, and promotes catalytic cracking reaction. But high content of rare earth metal also promotes formation of coke. The addition of 1% P2O5 optimizes the acidic properties of the matrix and zeolite to produce the low coke yield. The good activity of catalytic cracking reaction is kept up while the olefin content in catalytic cracking gasoline is reduced 6 percent.
Abstract: The macrokinetic experiments of olefin hydrogenation in pyrolysis gasoline over an industrial CoMo/Al2O3 catalyst were carried out in an integral tubular fixedbed reactor under the following conditions: 2.0MPa~4.0MPa, 524K~644K, H2/pyrolysisgasoline molar ratio 1.5~3.5 and the partial pressure at reactor inlet for cyclopentene, 3ethyl1pentene, styrene and 1hexene 0.87kPa~5.60kPa, 1.09kPa~7.01kPa, 1.14kPa~7.35kPa and 0.25kPa~0.97kPa, respectively. By means of Powell optimal method and Merson integral method, the powerlaw type macrokinetic models of catalytic hydrogenation of olefin in pyrolysis gasoline were developed, and a good agreement with experimental data and those calculated by the kinetic models estimated was obtained. The reaction orders of cyclopentene, 1hexene, styrene and 3ethyl1pentene were 1.725, 0.685, 0.7 and 0.655, respectively. And the activation energies of hydrogenation reaction of theirs were 63455J·mol－1, 61781J·mol－1, 52105J·mol－1 and 54181J·mol－1, respectively. The CoMo/Al2O3 catalyst here shows a good catalytic activity for 1hexene hydrogenation, a better activity for the hydrogenation of cyclopentene, 3ethyl1pentene and styrene, but a poor activity for 1heptene hydrogenation. The favorable operating pressure is about 3.5MPa for this catalyst.
Abstract: The relationship between the viscosity of Luojia ultra-heavy oil from Shengli oil field and its polar fractions, heteroatoms, metallic elements was investigated. It is found that the high viscosity of the oil is related with three factors: resin and asphaltene with high molecular weight, high sulphur content and the enhanced cohesion of asphaltene by macrocyclic compound formed by V, Fe and Ni. Simultaneously the effect of the viscosity reduction was examined. The interfacial tensions of water-oils are reduced greatly by the viscosity reducing agent, thus the viscosity of the ultra-heavy oil is reduced. The electron microprobe pictures of asphaltene is compared before and after treatment .On the basis of these evidences it can be concluded that the viscosity reducing agent can infiltrate into plate-like asphaltene molecules by forming hydrogen bond, infiltration and dispersion, so that the order of aggregation of the plate-like asphaltene molecules is lowered and the plate-on-plate aggregations become randomly packed ones.
Abstract: In order to maximize the liquid yield and glucide content in biomass pyrolysis products, acid wash pretreatment was usually adopted. The analysis of microstructure and polymerization degree shows that the acid wash can alter the cellulose morphology and decrease the polymerization degree largely. A series of experiments were carried out to study the effect of acid wash on the cellulose rapid pyrolysis. Experimental results indicate that under the acid pretreatment the yield of bio-oil decreases, while the yield of gas and char increases. The effect would be greater with the increase of acid concentration. Sulphuric acid has a stronger restraint on the formation of bio-oil than hydrochloric acid and phosphoric acid. It is suggested that the acid has a catalysis to the cross linking and dehydration reaction of cellulose. According to the GC-MS analysis of bio-oil, the existence of acid would not alter the bio-oil components, but change the relative contents of bio-oil compounds. High-concentration acid wash can restrain the formation of levoglucosan by catalyzing the dehydration and cross linking reaction.
Abstract: Based on the modified Brodio-Shafizadeh mechanism, a two-stage model was proposed to simulate the formation and decomposition of intermemediate products including active cellulose (AC), levoglucosan (LG), hydroxyl-acetaldehyde (HAA), acetol and furfural in the cellulose pyrolysis. Results show that the water evaporation only decreases the heating rate of the pyrolysis prophase, while it has no effects on the temperature distribution and reaction process in the main pyrolysis stage. Cellulose material stays for a long time in the middle temperature due to the endothermic effect of primary cracking. The concentration of LG and other competitive compounds in the fabric structure is primarily determined by its competitive reaction of formation. The rising of material thickness would prolong the decomposition time of cellulose, and enhance the secondary cracking within the fabric structure. The formation process both LG and HAA shows the characteristic of fast formation and rapid escape, but HAA presents a faster accumulating tendency that will be enhanced at high temperature. For small size materials, the secondary reaction of volatile occurs largely in the gaseous phase rather than in the solid phase. The longer residence time of volatile in the high temperature region will induce deep decomposes of LG. Compared with the rapid decrease of LG yield with reaction time, the yield of tar falls slowly at high temperature. The major change exists in the distribution of components, i.e. the large molecule compounds being decomposed into small ones.
Abstract: The Cu-Mn-Zn/Y catalysts with the different content of metallic component were prepared through a coprecipitation impregnation method, and used for the synthesis of dimethyl ether (DME) from synthesis gas in a fixed-bed reactor. The optimum content of metallic component loading on per gram zeolite Y was about 30mmol, and the conversion of CO and the selectivity of DME were 65.6% and 67.0% under 2.0MPa, 245℃ and 1500h－1. XRD, BET and TPD of H2, CO and NH3 results showed that, with the metal content increasing from 20mmol to 30mmol, the dispersion of all metallic component became better, the adsorption ability of H2 and CO also increased, but the surface area and the acidity of these catalysts did not changed. As the metal content up to 35mmol, the accumulated copper and micro-structural changes occurred, the surface area of the catalysts and the adsorption ability of H2 and CO decreased rapidly, the number and strength of acid sites also decreased. Consequently, the Cu-Mn-Zn/zeolite-Y catalyst with 30mmol metal loading exhibited the best catalytic performance for direct synthesis of DME was duo to the favorable adsorption ability of H2 and CO.
Abstract: The silica modified Cu-ZnO/HZSM-5 catalysts were prepared via the co-precipitation sedimentation method using sodium silicate as silicon source, sodium carbonate as precipitant. These catalysts were characterized by means of XRD, SEM, H2-TPR, XPS techniques, and their catalytic performance in dimethyl ether (DME) synthesis from CO2 hydrogenation were evaluated in a fixed-bed reactor. It was found that the modification of SiO2 had a remarkable effect on the structures of the catalyst precursors, the diffraction peaks of aurichalcite (Zn3Cu2(OH)6(CO3)2) at 2θ=13.2° weakened and broadened with the SiO2 content, interestingly, those peaks disappeared when SiO2 content was beyond 3.5%. The XRD and SEM studies of the calcined catalysts showed that silica retarded the growth of CuO and ZnO crystals and inhibited the agglomeration of the calcined catalysts. The TPR profiles of silica modified Cu-ZnO/HZSM-5 catalysts revealed that the reduction peaks and the peak temperature were different from that of the Cu-ZnO/HZSM-5 catalyst without silica modification. The catalytic performance showed that the activity first increased and then decreases with the increase of the SiO2 content. The CO2 conversion of 28.53% and DME yield of 16.34% was obtained over 1.0% SiO2 modified Cu-ZnO/HZSM-5 catalyst, which was increased by 20% and 34%, respectively, than that of Cu-ZnO/HZSM-5 catalyst without silica modification. XPS and AES measurements of the 1.0% SiO2 modified Cu-ZnO/HZSM-5 catalyst revealed that, during the reduction of the catalyst by H2 at 250℃ or DME synthesis from CO2/H2 at 250℃, the chemical valance of copper and zinc was 0 and 2+, respectively. Cu0 was considered to be the surface active site for the synthesis of methanol from CO2 hydrogenation. The present method may offer opportunities to prepare the ultra-fine mono-component or multi-component catalysts via the coprecipitation method.
Abstract: The modification effects of K2CO3 on β-Mo2C catalysts for mixed alcohols synthesis from CO hydrogenation were studied. Un-prompted β-Mo2C produced mainly hydrocarbons of C1-C4 under the reaction conditions of 573 K, 8.0 MPa, H2/CO=1.0, GHSV=2 000 h－1. Addition of K2CO3 to β-Mo2C resulted in remarkable selectivity shift from hydrocarbons to alcohols. Moreover, the promoter of potassium enhanced the ability of chain propagation of β-Mo2C with the higher selectivity of C2+ alcohols. The investigations of the loadings of K2CO3 in β-Mo2C revealed that the maximum of alcohol yield obtained at K/Mo (molar ratio) =0.2. On K/β-Mo2C catalysts, the distribution of hydrocarbons obeyed the traditional linear Anderson-Schultz-Flory equation, while the distribution of alcohols gave a unique linear Anderson-Schultz-Flory with remarkable deviation of methanol. Thus, potassium promoter exerted a prominent function on the whole chain propagation to produce alcohols especially for the stage of methanol to ethanol.
Abstract: The kinetics of coke formation on SAPO-34 catalyst in the transformation of methanol to olefins was studied in a fixed bed reactor and the relations in a type of Voorhies equation between coke deposition and reaction temperature or the ratio of catalyst-to-methanol were obtained, which could be used easily in practice. In the condition of 450 ℃, 15 h－1 methanol WHSV and 25 min TOS, an obvious coke distribution was found in the catalyst bed with a coke content of 9.56% at the inlet of catalyst bed and 3.20% at the outlet, which corresponded to a deactivation mainly in parallel with the main reaction. The coke was formed mainly in parallel with the formation of hydrocarbons, and all the products came from intermediates generated from methanol. On the basis of this mechanism, a kinetic model for coke formation which related the coke deposition with the methanol converted in reaction was induced. This kinetic model showed a good agreement with the experimental observation and also could be used easily.
Abstract: The effect of Cr addition to Pt-Sn/γ-Al2O3 catalyst on the activity, selectivity and deactivation in the propane dehydrogenation was studied. The fresh catalysts were characterized by H2-TPR and the amount of deposited carbon on used catalysts was analyzed by O2-pulse technology. The results of propane dehydrogenation showed that the addition of Cr to Pt-Sn/γ-Al2O3 catalyst can greatly reduce the deactivation rate and increase the selectivity to propene. The mean yield of propene over Pt-CrSn/γ-Al2O3 catalyst reached 38%, which was higher than that of Pt-Sn/γ-Al2O3 catalyst (about 33%). The O2-pulse experimental showed that the amount of deposited carbon on tri-metallic catalyst was much smaller than that on bimetallic catalyst. The synergetic effect between Cr and Pt-Sn took place. Pt promoted the reduction of Cr6+ to Cr3+, which could increase the selectivity to propene. The addition of Cr to Pt-Sn/γ-Al2O3 also made the reduction of Sn more difficult and stabilizes the oxidation state of tin. The presence of oxidation state of tin would promote the stability of catalyst. This may suggest that the presence of Cr can prevent the formation of PtSn alloy and can promote the stability of Pt-Sn/γ-Al2O3 catalyst in dehydrogenation of propane.
Abstract: A series of CuNi/γ-Al2O3 catalysts with different Cu contents were prepared and evaluated by the gas-phase benzene hydrogenation as a probe reaction. After reduction at 160 ℃, the Cu-promoted CuNi/γ-Al2O3 catalysts exhibited considerably higher activity than Ni/γ-Al2O3 catalysts, and the copper content played an important role in the catalyst reducibility and catalytic activity. The catalyst, CuNi/γ-Al2O3 with copper to nickel atomic ratio 1∶1, exhibited best catalytic activity and stability. XRD(X-ray diffraction) results showed that the addition of copper to the Ni/γ-Al2O3 catalysts significantly improved the dispersion of NiO over γ-Al2O3, the CuNi/γ-Al2O3 with copper to nickel atomic ratio 1∶1 had optimal dispersion, and further addition was accommodated by the decreasing of the dispersion of NiO. TPR(temperature programmed reduction) results suggested the addition of copper promoted the reducibility of supported nickel oxide by enhancing surface segregation of a NiO-like phase, while copper to nickel atomic ratio in excess of 3∶5 had practically no additional promoting effect.
Abstract: The Monte Carlo method was employed to investigate the effect of critical solvents acetone and heptane on the desorption and extraction of methanol from porous media. The effect of molecular structure of the solvents and extrinsic factors (pore size) on the methanol synthesis process were all took into account when the model was built up. The results showed that polar acetone was beneficial to the desorption of methanol, however the effect of nonpolar heptane on the extraction of methanol was more evident. The effects of the solvents on the desorption of methanol were increased with increasing of the pore size while the effects on the extraction of methanol in the pores were decreased with increasing of the pore size.
Abstract: Thermodynamic equilibrium analysis was performed on methane autothermal reforming to generate hydrogen by using the minimization of Gibbs free energy. Effects of operation parameters such as molar ratios of steam to methane (W/M), air to methane (A/M) and adiabatic temperature on the reforming process were studied. Results showed that the optimal W/M is around 2.5~3.5 and molar oxygen to methane between 0.4 and 0.7. Thus the reforming temperature lays between 700℃ and 850℃ and H2 generating per mole methane is around 2.17mol～2.23mol. Taking example for the 1.5 of W/M, possible formation or conversion mechanisms were deduced for different constitutes under different A/W through the simulating calculations. The thermodynamic equilibrium calculations provide optimal operation parameters for methane autothermal reforming to generate hydrogen.
Abstract: Ethanol degradation at room temperature was investigated on a homemade batch reactor using Fourier Transform-Infrared Radiation (FTIR). It was found that FTIR could be used to track the degradation of ethanol. When ethanol molecules were degraded in the batch reactor, they were converted to CO2 via intermediates. One of the intermediates was gaseous acetaldehyde. In the batch reactor, the flux of the mixture had little effect on ethanol degradation rate. The Langmuir-Hinshelwood (L-H) kinetics could be successfully applied to describe the degradation of high concentrate ethanol. The effect of temperature on the degradation of ethanol was significant. With increasing temperature the initial reaction rate of ethanol was increased remarkably.
Abstract: Experimental investigation was conducted to evaluate the effect of soot reduction by eight different organometallic compounds in a direct injection diesel engine by the free acceleration method. Meanwhile, the mechanism of these compounds was studied in the paper. All eight compounds were found to be effective in reducing soot emission with the sequence of barium dinonynalphthalene sulfonate>ferrocene>iron naphthenates>petroleum barium sulfonate>manganese naphthenates>cuprum naphthenates>barium naphthenates>cerium naphthenates. When the proportion of barium dinonynalphthalene sulfonate in the fuel is 4‰, soot emission is reduced by 40.7%, and the diesel fuel blended with 1‰ ferrocene could reduce soot emission by 35.3%. The experimental results show that the organic structure of organometallic compounds makes effect on the reduction of the soot emission, as well as on the sensitivity to the content. The formation of the soot is related to the acetylene and polycyclic aromatic hydrocarbons (PAH), while the oxidation of the soot is related to the concentration of the oxygen around and the surface area of the soot particles. Most of the organometallic compounds contain oxygen, and can break down the fuel into CO rapidly which greatly decreases the PAH. Cyclopentadienyl type organometallic compound can activate CO which prohibits the formation of the precursor of the soot.
Abstract: Organic compounds deposited on titanium silicalite catalyst (TS-1) are one of the main reasons that cause the catalyst deactivation during cyclohexanone ammoximation process. The molecular structure and physicochemical properties of deposits on deactivated TS-1 are recognized and identified by means of various characterization approaches, including FT-IR, TG-DTA, GC-MS, XRD, NMR, N2 physisorption and SEM. According to the characterization results, the deposits, which locate on the pores of zeolite and result in the catalyst deactivation, consist of the ether-soluble compounds including the products of cyclohexanone oxidation/reduction, dimers of cyclohexanone, continuous reaction products of cyclohexanone oxime, tert-butylcyclohexanone as well as the insoluble deposits due to their further polymerization. The overall amount of deposits accounts for 5.0% of deactivated TS-1 in mass. The deposits closed to Ti centers can be removed preferentially at lower temperatures during the TPO process, but the removal of others needs a higher temperature and can be completed at 650℃. The catalytic activity of deactivated catalyst can be recovered after it was calcined at 700℃ in air.
Abstract: The synthesis of dimethyl ether (DME) using syngas in a bubble column slurry reactor was simulated. It was assumed that the fluid and the solid phases were mixed completely (CSTR model) and the gas phase was plug flow (PFR model). The ordinary nonlinear differential equations were solved using fourth-order Runge-Kutta integration with automatic step control. The programming language C++ was used to implement the numerical algorithm. The influences of pressure, temperature and catalyst concentration on the conversion, yield and selectivity of DME were studied. The optimal reaction conditions were obtained, which are useful for engineering scale-up and plant design.
Abstract: The combustion performance of the blend of lignite and residue from Shenhua coal liquefaction was studied. It is found that the DTG plot for the combustion of residue of coal liquefaction has three characteristic peaks, while the DTG plot of lignite combustion has one characteristic peak. With the decreasing of the blending ratio of coal liquefaction residue to lignite the three characteristic peaks become faintness. The combustion activation energies of blended coals are calculated. Compared with the blended coals, the coal liquefaction residue has the biggest activation energy, but the lignite has the lowest one. With the blending ratio decreasing the activation energy and ignite temperature of blends decrease slightly. The maximum weight loss rate DTGmax for coal liquefaction residue is bigger than that for lignite.
Abstract: The oxidation of dibenzothiophene (DBT) in decalin (as solvent) was conducted using oil-soluble oxidant cyclohexanone peroxide (CYHPO).The effects of oxidant amount, reaction temperature, reaction time were investigated in detail. The results showed that under the condition of ratio of CYHPO to sulfur 2.5∶1, reaction temperature 100℃ and reaction time 3h, the desulfurization rate was up to 87%. The little water produced after oxidation was removed by molecular sieve adsorption. The recovery ratio of model oil was up to 98% after the treatment with centrifugation and adsorption.
Abstract: Formaldehyde as an indoor pollutant is harmful to human health even with a very low content in the atmosphere. It can be removed through catalytic oxidation, and Pt/TiO2 proved to be a potential catalyst and can be operated at low temperature and high space velocity. To understand the mechanism of catalytic oxidation of formaldehyde over Pt/TiO2, the intrinsic kinetics of reaction was investigated in a fixed-bed plug flow differential reactor at atmospheric pressure. A power law rate equation was established as r=1.87×107 exp(-47.50×103/(R×T))×c1.27HCHO, which gave a good correlation to the experimental results.
Supervisor：Chinese Academy of Sciences
Sponsors by：Shanxi Institute of Coal Chemistry, Chinese Academy of Sciences Chinese Chemical Society
