四氟硼酸钾的制备

在国内外制备ＫＢＦ４的基础上，提出了一种新的制备方法，即用ＨＢＦ４与ＫＦ反应生成ＫＢＦ４。产率达９８．７％，纯度为９９．５５％，滤液又可回收利用，回收产率９９．０％。     

亚磷酸二甲酯尾气中氯甲烷回收的工艺实践

本文介绍了从亚磷酸二甲酯生产尾气中回收氯甲烷的工艺，采用降温干燥，固碱干燥和压缩相结合的方法，可使回收氯甲烷的浓度达９９％以上。     

有机硅废触体的综合利用

本文对有机硅废触体的综合利用进行了研究，采用氧化－还原法回收废触体中的铜，回收率可达９５％以上，获得的铜的纯度为９９％，同时回收了纯度较硅粉。具有较好的经济效益和社会效益。     

金属丝网波纹填料塔在回收甲醇中的应用及设计

叙述了甲醇回收中波纹填料塔的结构及设计，其分离效率高，可获得９９．５％的甲醇。     

高浓度含氰废水治理新工艺

研究了用硫酸亚铁新工艺有效降低高浓度含氰废水中氰含量的方法，使氰化物净化率＞９９．９９％。对工艺过程中的废渣进行了回收，制备出副产品黄血盐钠，其质量达到国家标准，消除了二次污染，提高了经济效益。     

病虫灵中吡虫啉和多菌灵的液相色谱分析

本文以液相色谱方法，采用同一内标物，同时测定病虫灵可湿性粉剂中的吡虫啉、多菌灵。在选定的色谱条件下。内标物、有效成分以及未知物相互之间能得到有效的分离，并能获得较好的检测结果。吡虫啉、多菌灵的变异系数分别为１．９％、０．９９％；平均回收分别为１００．６％、９９．６％。     

电位滴定法测定回收废料中钴的含量

介绍一种适用于回收废料中钴含量测定的铁氰化钾电位滴定法，方法的标准偏差Ｓ小于０．１５，回收率９９．４％￣１００．７％。     

铜锌混合硫酸盐溶液制氯化亚铜和氧化锌

用亚硫酸钠还原铜锌硫酸盐混合溶液，制得符合国际ＣｕＣｌ和含量９９％ＺｎＯ。铜收率８７％，锌收率９５％，并回收硫酸钠，是综合利用Ｃｕ，Ｚｎ矿新途径。     

过氧化氢生产废触媒中贵金属钯的回收

以氯代烃法处理废触媒回收金属钯的方法，钯的总收率为９５％，得到的金属钯黑纯度达９９．９％以上，可重新用于新触媒的制备。     

菲的提纯

以氯苯为溶剂，在不同温度下用５０％氢氧化钾溶液，活性白土，９０％的硫酸溶液处理工业菲，经冷却，结晶，获得纯度９８．４％－９９．２％的精菲的提纯收率８３％以上，母液可以循环使用，溶剂可以回收。     

管道内预混合成气爆炸特性

通过自主搭建的小尺寸实验平台,对比研究了当量比为1时不同氢气体积分数下,预混合成气在开口和闭口管道中的爆炸特性。研究结果表明：开口和闭口管道中合成气爆炸预混火焰传播结构具有明显差异;在闭口管道中,在所有的氢气体积分数下均观测到经典郁金香火焰结构,其中氢气体积分数为70%和90%时,能够观测到扭曲的郁金香火焰结构;在开口管道中,仅在氢气体积分数为10%、30%、50%时形成了经典郁金香火焰,且当氢气体积分数为10%、30%时,出现了扭曲郁金香火焰。开口和闭口管道中的火焰传播速度和爆炸压力峰值均随着氢气体积分数的增加而增大。当氢气体积分数较低（f < 50%）时,火焰传播速度和爆炸压力峰值随着氢气体积分数的增大而迅速增大,而在较高氢气体积分数（f≥ 50%）时,随着氢气体积分数的增加,火焰传播速度和爆炸压力峰值增加缓慢。     

Comparative study on pressure swing adsorption system for industrial hydrogen and fuel cell hydrogen

In order to improve the design of PSA system for fuel cell hydrogen production, a non-isothermal model of eight-bed PSA hydrogen process with five-component (H₂/N₂/CH₄/CO/CO₂=74.59%/0.01%/4.2%/2.5%/18.7% (vol)) four-stage pressure equalization was developed in this article. The model adopts a composite adsorption bed of activated carbon and zeolite 5A. In this article, pressure variation, temperature field and separation performance are stimulated, and also effect of providing purge (PP) differential pressure and the ratio of activated carbon to zeolite 5A on separation performance in the process of producing industrial hydrogen (CO content in hydrogen is 10 μl·L^-1) and fuel cell hydrogen (CO content is 0.2 μl·L^-1) are compared. The results show that Run 3, when the CO content in hydrogen is 10 μl·L^-1, the hydrogen recovery is 89.8%, and the average flow rate of feed gas is 0.529 mol·s^-1; When the CO content in hydrogen is 0.2 μl·L^-1, the hydrogen recovery is 85.2%, and the average flow rate of feed gas is 0.43 mol·s^-1. With the increase of PP differential pressure, hydrogen recovery first increases and then decreases, reaching the maximum when PP differential pressure is 0.263 MPa; With the decrease of the ratio of activated carbon to zeolite 5A, the hydrogen recovery increases gradually. When the CO content in hydrogen is 0.2 μl·L^-1 the hydrogen recovery increases more obviously, from 83.96% to 86.37%, until the ratio of activated carbon to zeolite 5A decreases to 1. At the end of PP step, no large amount of CO₂ in gas or solid phase enters the zeolite 5A adsorption bed, while when the CO content in hydrogen is 10 μl·L^-1, and the ratio of carbon to zeolite 5A is less than 1.4, more CO₂ will enter the zeolite 5A bed.     

柴油加氢尾气中氢气的水合物法回收工业侧线试验

常规氢气回收方法的产品氢气压力偏低,需多级增压后才可被高压加氢装置利用,具有较高的氢气增压成本。水合物法回收加氢尾气具有压降损失小、产品氢气压力高的优点,可降低高压加氢装置的氢气增压成本。为降低高压加氢装置的用氢成本,本文开发了高压尾气的水合物法氢气回收技术。针对高压柴油加氢尾气,在茂名炼油厂建立了一套柴油加氢尾气中氢气水合物法回收的工业侧线试验装置,考察了不同条件下连续搅拌釜法回收柴油加氢尾气中氢气的分离效果。试验结果表明,水合物法可高效脱除CH₄和大部分的H₂S。连续进气工况下,处理脱硫后尾气时可将氢气体积分数从83.76%提高至91.65%,处理含硫尾气时可将H₂S体积分数从0.73%降至0.07%。     

3种测试溶液对搪瓷用钢抗鳞爆性能评价指标的影响

采用3种常见的测试溶液检测了10组搪瓷用钢板的氢渗透性能,并同时采用涂搪实验进行验证。结果显示,测试溶液A适用于试验选定的各种厚度的搪瓷用钢,其检测结果准确率可达100%;而溶液B和溶液C在测试厚度1.5 mm以上的搪瓷用钢板料出现部分误判现象。溶液B若基于有效氢扩散系数D_eff,其准确率为70%,若基于TH值,其准确率仅为50%;而溶液C误判率达30%。     

Changes in crystallographic orientation of thin foils of palladium and palladium alloys after the absorption of hydrogen

The adsorption/absorption of hydrogen at room temperature by palladium, 16% silver-palladium and 5% ruthenium-palladium foils was studied using thermal desorption spectroscopy. Hydrogen readily diffused in the palladium and desorbed as one broad peak at about 650 K. Hydrogen also diffuses in the 16% silver-palladium foil and in the 5% ruthenium-palladium foil but with a smaller diffusion constant. Two hydrogen desorption peaks are observed for the Ru-Pd and Ag-Pd alloys, at 440 and around 650 K. The first hydrogen desorption peak is regarded as hydrogen desorbing from the surface sites while the second peak is regarded as hydrogen diffusing from the subsurface sites. The desorption order for surface hydrogen corresponds ton = 2 while the diffused hydrogen desorbs with a fractional order ofn = 1.25. The crystallographic orientation of the foils determined by X-ray diffraction shows a preferential (1,1,0) orientation along the direction of rolling of the foils before hydrogen absorption. This preferential orientation is destroyed after hydrogen adsorption for Pd and Pd-Ag but unaltered for the Pd-Ru alloy. This preferential orientation of the foils might have significant implications in membrane fabrication, since the absorption of hydrogen by Pd is very dependent on surface orientation.     

Effects of electric potential on hydrogen adsorption

Hydrogen adsorption isotherms of activated carbon and its mixture with platinum coated activated carbon under various electric potentials and hydrogen pressures were measured at ambient temperature. Results indicated that electric potential enhanced hydrogen adsorption. The higher the applied electric potential is, the higher the hydrogen adsorption capacity is in the experimental range of 0-3000 V. The total amount of hydrogen adsorption increases with the hydrogen pressure. However, the enhancement is more obvious at hydrogen pressures below 10 bars. The enhancement ratio can reach about 160% at 1.6 bars pressure and 3000 V applied electric potential, but decreases to about 20% at 80 bars pressure under the same voltage. The adsorption enhancement is much more significant for the mixture of platinum coated activated carbon and activated carbon at a ratio of 1-4. At 1.6 bars, the hydrogen adsorption capacity increases from 0.008 wt.% at 0 V to 0.058 wt.% at 2500 V, which is a 625% adsorption enhancement. At 83 bars, the hydrogen adsorption capacity increases from 0.43 wt.% at 0 V to 0.56 wt.% at 2500 V, about 30% adsorption enhancement.     

过碳酸钠生产的最佳工艺条件研究

以碳酸钠和双氧水为原料制备过碳酸钠,考察了双氧水浓度、反应温度、反应时间、物料配比等因素对产品收率的影响。结果表明,当反应温度为15℃,双氧水浓度为30%,反应时间0.5 h,反应物碳酸钠和双氧水的摩尔比为1∶1.5~1∶1.6,稳定剂为硅酸钠,用量为0.5%,过碳酸钠的收率大于85%。     

吸附强化乙醇水重整制氢的工艺条件

采用吸附强化技术强化了乙醇水重整制氢过程。考察了温度、水醇比、液空速对无强化乙醇水重整制氢反应特性的影响,在此基础上研究了吸附强化乙醇水重整制氢反应特性。通过响应面法确定了吸附强化乙醇水重整制氢最优工艺条件为温度422～444 ℃、水醇比10.2～10.8、液空速0.13 h?1,在此条件下的氢产率为3.2 mol/mol,同比提高了51.7%,氢含量为88.91%,同比提高了22.9%,反应温度降低了178 ℃,降低了能耗,控制了CO2排放。     

储氢提纯和氢网络的耦合优化

基于氢网络的集成以及AB₅型储氢材料LaNi_4.75Fe_0.25及LaNi_4.85Al_0.15的特性，对储氢提纯在氢网络中的应用进行研究。综合考虑LaNi_4.75Fe_0.25及LaNi_4.85Al_0.15储氢/放氢动力学，建立了储氢提纯氢网络的优化方法，根据单位质量储氢材料提纯的节氢能力和公用工程节省量与提纯参数的关系，确定最优提纯氢源浓度、最大公用工程节省量、储氢材料量和吸氢时间。用该方法对某炼厂氢网络和储氢提纯单元进行优化，结果表明，最优提纯氢源浓度为70%，提纯后公用工程可节省23.72%； LaNi_4.85Al_0.15作为储氢提纯材料优于LaNi_4.75Fe_0.25，其消耗量为991.26 kg。     

Integration strategies of hydrogen network in a refinery based on operational optimization of hydrotreating units

Inferior crude oil and fuel oil upgrading lead to escalating increase of hydrogen consumption in refineries. It is imperative to reduce the hydrogen consumption for energy-saving operations of refineries. An integration strategy of hydrogen network and an operational optimization model of hydrotreating (HDT) units are proposed based on the characteristics of reaction kinetics of HDT units. By solving the proposed model, the operating conditions of HDT units are optimized, and the parameters of hydrogen sinks are determined by coupling hydrodesulfurization (HDS), hydrodenitrification (HDN) and aromatic hydrogenation (HDA) kinetics. An example case of a refinery with annual processing capacity of eight million tons is adopted to demonstrate the feasibility of the proposed optimization strategies and the model. Results show that HDS, HDN and HDA reactions are the major source of hydrogen consumption in the refinery. The total hydrogen consumption can be reduced by 18.9% by applying conventional hydrogen network optimization model. When the hydrogen network is optimized after the operational optimization of HDT units is performed, the hydrogen consumption is reduced by 28.2%. When the benefit of the fuel gas recovery is further considered, the total annual cost of hydrogen network can be reduced by 3.21×10₇ CNY·a_-1, decreased by 11.9%. Therefore, the operational optimization of the HDT units in refineries should be imposed to determine the parameters of hydrogen sinks base on the characteristics of reaction kinetics of the hydrogenation processes before the optimization of the hydrogen network is performed through the source-sink matching methods.