氟化钠涂膜在正畸临床防脱矿和龋坏的应用研究

目的 :研究氟化钠涂膜对正畸临床固定矫治器治疗中产生的牙釉质脱矿或龋坏的预防作用。方法 :170例采用固定矫治器进行治疗的错畸形患者 ,85例做为处理组 ,在托槽粘着后立即在托槽周围的牙面上涂布氟化钠涂膜 ,以后每三个月涂布一次 ;另 85例做为对照组 ,在正畸治疗中托槽周围的牙面不做任何特殊处理。结果 :处理组患者牙釉质表面脱矿发生率 3.7% ;对照组 16 .3%。经统计学处理两组间有显著性差异 (P <0 .0 5 )。结论 :在口腔正畸使用固定矫治器治疗时 ,配合使用氟化钠涂膜对预防正畸治疗中产生的牙釉质脱矿或龋坏是有效的。

釉质表层特征及其脱矿与再矿化行为

釉质表面约30μm的高钙化区称为釉质表层,在早期龋形成时该层结构保持相对"完整"。该文将从釉质表层固有的理化性质出发,对其抗酸性,形成机制,脱矿再矿化行为及其在龋病发生发展中的作用作一综述。

牙色度分析在原位乳牙脱矿与再矿化检测中的应用

目的:验证数码照相牙色度分析法进行体内乳牙脱矿与再矿化研究的可行性。方法:选取58例平均年龄为4岁的儿童,以左上中切牙为实验牙,先染色、数码拍照,然后对实验牙面进行酸蚀、染色、数码拍照,最后在口腔环境内自然再矿化24h和1周后再染色、拍照,运用图像分析软件进行牙色度R、G、B值分析,比较酸蚀脱矿及再矿化前后牙色度的变化。用SPSS 19.0软件包对数据进行方差分析。结果:酸蚀脱矿后及再矿化24h后的色值(R、G、B)与基值有显著差异(P<0.05);在1周时间点上,只有B值与基值有显著差异(P<0.05);再矿化24h及1周后,牙色度值与酸蚀后相比有显著差异。结论:数码牙色度分析法可识别乳牙脱矿及再矿化前后牙色度的变化,可用于原位乳牙脱矿与再矿化研究。

酸蚀时间、再矿化时间对乳牙釉质再矿化的影响

目的本研究采用激光共聚焦显微镜来观测不同酸蚀时间、不同矿化时间对乳牙釉质再矿化的影响。方法采用随机区组设计,将28枚离体乳切牙的唇面分别开4个窗,随机分到酸蚀30 s、60 s、90 s、120 s 4个处理组中,采用32%磷酸凝胶对标本进行酸蚀处理,而后采用人工唾液进行再矿化,分别于脱矿后、再矿化处理2 h,再矿化处理24 h进行激光共聚焦显微镜扫描,记录其平均荧光量(AF),采用重复测量的方差分析对数据进行分析,显著性水平为0.05。结果多变量方差分析(MANOVA)结果显示:再矿化时间、酸蚀时间对再矿化后AF有显著影响(分别F=357.74,P<0.0001;F=51.62,P<0.0001);Bonferroni法多重比较显示:酸蚀时间对再矿化效果影响中,除90 s组与120 s组之间的差异没有显著性,其余各组AF两两比较差异均有显著性;矿化时间对再矿化的影响中,两两比较AF差异均有显著性。结论在进行乳牙抗酸能力及再矿化潜能检测时,酸蚀时间不可超过60 s,再矿化时间可以为24 h。

绵羊椎体骨质疏松性生物力学模型的快速建立

目的运用微量注射泵向椎体内灌注盐酸及椎体整体浸泡的脱钙方法,快速建立绵羊腰椎骨质疏松性生物力学模型。方法(1)设计一款可拧入椎弓根带侧孔的圆柱形灌注连接器,做为椎体内部与注射泵的桥接装置。(2)将(3±0.5)岁新鲜绵羊腰椎48个,随机分为4个处理组:A组(0 h脱钙,即空白组),B组(2 h脱钙),C组(4 h脱钙),D组(6 h脱钙)。每组12个椎体。(3)检测各组椎体脱钙前后BMD;进行生物力学实验:测试最大轴向拔出力(Fmax)和最大抗压强度及其能量吸收值。同时各组取少量骨质制成组织切片,对脱钙后绵羊腰椎骨小梁微观结构进行观察。结果B、C、D处理组的BMD均值、最大轴向拔出力均值和最大抗压强度及其能量吸收值均值都低于A组(P<0.01),且随脱钙时间的延长依次降低(P<0.01)。椎体的最大轴向拔出力及最大抗压强度与BMD存在正相关关系,亦与BMD的下降值存在负相关。切片显示:B、C、D组椎弓根处骨小梁较A组骨小梁厚度明显变薄、数量减少,间距增宽,部分骨小梁连续性中断,骨髓腔扩大。结论运用微量注射泵向椎体内灌注盐酸及整体浸泡的脱钙方法,可快速、有效、可控的建立近似于骨质疏松状态下的生物力学模型,为在真正骨质疏松状态下的生物力学研究提供参考依据。

Interaction of sulfur with iron compounds in sodium aluminate solutions

Reaction behaviors of sulfur and iron compounds in sodium aluminate solutions were investigated. The results show that iron compounds can remarkably remove the S2 but cannot get rid of S2Oc2-, SO^2- and SO4^-2 in sodium aluminate solutions. The removal efficiency of S^2- using ferrous compound and ferric compound can reach 86.10% and 92.70% respectively when the iron compounds were added with a molar ratio of 2：1 compared with the sulfur in liquors at 100℃. Moreover, several same compounds are formed in those two desulfurization processes with ferrous or ferric compounds, including erdite, hematite, amorphous ferrous sulfide, polymerized sulfur-iron compounds and ferric sulfate. The major difference between these two processes is that the erdite generated from ferrous compounds at the initial reaction stage will convert to a sodium-free product FeS2 at the subsequent stage.

Cyanide removal for ultrafine gold cyanide residues by chemical oxidation methods

Because of the highly toxic cyanide in the gold cyanide residues,cyanide must be removed for environmental protection.The process mineralogy of residues was studied firstly,and then cyanide removal was carried out by three chemical methods.The results showed that the residue mainly contained Si,S and Fe.Pyrite was the main metallic mineral,and the iron-complex cyanides make cyanide removal difficult.The minerals in residues were in ultrafine particle size with high monomer dissociation degrees.In H_(2)O_(2)oxidation process,the self-decomposition and side reactions resulted in high consumption of H_(2)O_(2).In Na_(2)S_(2)O_(5)-air oxidation process,the time for complete process was long because of the reactions between Na_(2)S_(2)O_(5)and O_(2).Na_(2)SO_(3)oxidation method was found to be a new method for cyanide removal without air inflation device.The cyanide content was reduced to the national standard level in 90 min at pH 9.0 with optimum Na_(2)SO_(3)dose of 2.0 g/L.

Effect of calcium compounds on direct reduction and phosphorus removal of high-phosphorus iron ore

The increasing demand for iron ore in the world causes the continuous exhaustion of magnetite resources.The utilization of high-phosphorus iron ore becomes the focus.With calcium carbonate(CaCO_(3)),calcium chloride(CaCl_(2)),or calcium sulfate(CaSO_(4))as additive,the process of direct reduction and phosphorus removal of high-phosphorus iron ore(phosphorus mainly occurred in the form of Fe_(3)PO_(7) and apatite)was studied by using the technique of direct reductiongrinding-magnetic separation.The mechanism of calcium compounds to reduce phosphorus was investigated from thermodynamics,iron metallization degree,mineral composition and microstructure.Results showed that Fe_(3)PO_(7) was reduced to elemental phosphorus without calcium compounds.The iron-phosphorus alloy was generated by react of metallic iron and phosphorus,resulting in high phosphorus in reduced iron products.CaCO_(3) promoted the reduction of hematite and magnetite,and improved iron metallization degree,but inhibited the growth of metallic iron particles.CaCl_(2) strengthened the growth of iron particles.However,the recovery of iron was reduced due to the formation of volatile FeCl_(2).CaSO_(4) promoted the growth of iron particles,but the recovery of iron was drastically reduced due to the formation of non-magnetic FeS.CaCO_(3),CaCl_(2) or CaSO_(4) could react with Fe_(3)PO_(7) to form calcium phosphate(Ca_(3)(PO_(4))_(2)).With the addition of CaCO_(3),Ca_(3)(PO_(4))_(2) was closely combined with fine iron particles.It is difficult to separate iron and phosphorus by grinding and magnetic separation,resulting in the reduced iron product phosphorus content of 0.18%.In the presence of CaCl_(2) or CaSO_(4),the boundary between the generated Ca_(3)(PO_(4))_(2) and the metallic iron particles was obvious.Phosphorus was removed by grinding and magnetic separation,and the phosphorus content in the reduced iron product was less than 0.10%.

Preparation of sodium manganate from low-grade pyrolusite by alkaline predesilication-fluidized roasting technique

Low concentration alkaline leaching was used for predesilication treatment of low-grade pyrolusite. The effects of initial NaOH concentration, liquid-to-solid ratio, leaching temperature, leaching time and stirring speed on silica leaching rate were investigated and the kinetics of alkaline leaching process was studied. The results show that silica leaching rate reached 91.2% under the conditions of initial NaOH concentration of 20%, liquid-to-solid ratio of 4：1, leaching temperature of 180 ℃, leaching time of 4 h and stirring speed of 300 r/min. Shrinking-core model showed that the leaching process was controlled by the chemical surface reaction with activation energy Ea of 53.31 k J/mol. The fluidized roasting conditions for preparation of sodium manganate were optimized by the orthogonal experiments using the desiliconized residue. The conversion rate of sodium manganate was obtained to be 89.7% under the conditions of silica leaching rate of 91.2%, NaOH/MnO2 mass ratio of 3：1, roasting temperature of 500 ℃ and roasting time of 4 h, and it increased with the increase of silicon leaching rate.

Argillization mechanics of rock from the Xing’anling Group in the Beier depression of the Hailar basin

The reservoir of the Xing'anling Group in the Beier depression of the Hailar basin is loosely cemented with many tuffaceous grains.This causes argillization and collapse of the grain framework of the reservoir sandstones.A detailed study on the characteristics of rocks and minerals was carried out through polarized microscope,X-ray diffraction,X-ray fluorescence,SEM and energy spectrum analysis.The results indicate that the reason for argillization is the abundant pyroclastic,and especially tuffaceous,grains in the reservoir.The alkaline component is relatively high in some strata.These are easily altered to montmorillonite in diagenesis.Na+montmorillonite swells strongly when exposed to water.This is the fundamental reason for the reservoir's argillization and plugging.

Utilization of coal-derived pyrite by electrolysis

The utilization of coal derived pyrite by electrolysis was studied. It is obvious that the sulfur and Fe in pyrite can be electrolyzed into Fe 3+ and SO 2- 4, and the no pollutant is drained off. In this paper, the influence of conditions, including electrolysis potential, time, temperature, the acidity of electrolysis solutions, the concentration of adding agent, the concentration of pyrite, and the rate of conversion of pyrite (Cr) was investigated. Cr increases with the rise of potential, time, temperature, acidity and the concentration of additive agent, but decreases with the rise of concentration of pyrite. At the certain conditions (at the potential of 3 0 V, temperature of 298 K, time of 12 h, the concentration of MnSO 4 of 6%, concentration of pyrite of 4%, and concentration of acid of 10%), Cr is high to 93%. In the same time, the mechanism of electrolysis of pyrite was provided. The electrolysis of pyrite is actually the recycle of Mn ion between anodic surface and pyrite. At last, the production of FeSO 4·7H 2O through electrolysis of pyrite was introduced.

Desiliconization kinetics of nickeliferous laterite ores in molten sodium hydroxide system

A novel process was proposed for treating nickeliferous laterite ores with molten sodium hydroxide.The effect on silicon extraction caused by the factors,such as stirring speed,reaction temperature,particle size and NaOH-to-ore mass ratio,was investigated.The results show that increasing stirring speed,reaction temperature and NaOH-to-ore mass ratio while decreasing particle size increases silicon extraction rate.The desiliconization kinetics of nickeliferous laterite ores in molten sodium hydroxide system was described successfully by chemical reaction control model.The activation energy of the desiliconization process was found to be 44.01 kJ/mol,and the reaction rate based on a chemical reaction-controlled process can be expressed as:1-(1-α) 1/3 = 27.67exp[-44 010/(RT)]t.

Acid leaching decarbonization and following pressure oxidation of carbonic refractory gold ore

Carbonate decomposition of carbonic refractory gold ore and the following pressure oxidation were studied.In the carbonate decomposition procedure,the effects of liquid-to-solid ratio and reaction time on decomposition ratio of carbonate were investigated.The experimental result shows that the decomposition ratio of carbonate is 98.24%under the conditions of liquid-to-solid ratio of 5:1,Fe^(3+)concentration of 20 g/L,sulfuric acid concentration of 20 g/L,reaction temperature of 80 ℃ and reaction time of 2 h.Then,the slurry obtained from carbonate decomposition was put into the titanium autoclave for pressure oxidation leaching.Effects of liquid-to-solid ratio,temperature,time and oxygen partial pressure on sulfur oxidation ratio were studied during pressure oxidation.With the prolonged time,pyrite and arsenopyrite are oxidized to ferric subsulfate,hydrated ferric sulfate and jarosite,resulting in the increasing residue ratio.The residue ratio and the sulfur content in the residue can be decreased by ferric subsulfate dissolution.The oxidation ratio of the sulfur is 99.35% under the conditions of oxidation time of 4 h,temperature of 210 ℃,oxygen partial pressure of 0.8 MPa and stirring speed of 600 r/min.

Carbon Dioxide Mineralisation and Integration with Flue Gas Desulphurisation Applied to a Modern Coal-Fired Power Plant

For Finland, carbon dioxide mineralisation was identified as the only option for CCS （carbon capture and storage） application. Unfortunately it has not been embraced by the power sector. One interesting source-sink combination, however, is formed by magnesium silicate resources at Vammala, located -85 km east of the 565 MWe coal-fired Meri-Pori Power Plant on the country＇s southwest coast. This paper assesses mineral sequestration of Meri-Pori power plant CO2, using Vammala mineral resources and the mineralisation process under development at Abo Akademi University. That process implies Mg（OH）E production from magnesium silicate-based rock, followed by gas/solid carbonation of the Mg（OH）2 in a pressurised fluidised bed. Reported are results on experimental work, i.e., Mg（OH）2 production, with rock from locations close to Meri-Pori. Results suggest a total CO2 fixation capacity -50 Mt CO2 for the Vammala site, although production of Mg（OH）2 from rock from the site is challenging. Finally, as mineralisation could be directly applied to flue gases without CO2 pre-capture, we report from experimental work on carbonation of Mg（OH）2 with CO2 and CO2-SO2-O2 gas mixtures. Results show that SO2 readily reacts with Mg（OH）2, providing an opportunity to simultaneously capture SO2 and CO2, which could make separate flue gas desulphurisation redundant.

Influence of silicate anions structure on desilication in silicate-bearing sodium aluminate solution

The structural changes of silicate anions in the desilication process with the addition of calcium hydrate alumino-carbonate were studied by measuring Raman spectra, infrared spectra and corresponding second derivative spectra. The results show that the desilication ratio in the solution prepared by the addition of sodium silicate(solution-SS) is much greater than that in the solution by the addition of green liquor(solution-GL), and low alumina concentration in the sodium aluminate solutions facilitates the desilication process. It is also shown that alumino-silicate anions in the solution-GL, and Q^3 polymeric silicate anions in solution-SS are predominant, respectively. In addition, increasing the concentration of silica favors respectively the formation of the alumino-silicate or the Q^3 silicate anions in the solution-GL or the solution-SS. Therefore, it can be inferred that the low desilication ratio in the silicate-bearing aluminate solution is mainly attributed to the existence of alumino-silicate anions.