硫酸吸收塔分酸器改造及填料更新

硫酸厂吸收塔原采用的槽爪式分酸器是20世纪七、八十年代的分酸技术，分酸点仅能达到10点／m^2，存在分酸点少、分酸不均匀、腐蚀性大的缺点。随着我厂硫酸产量的增加，吸收塔气速提高，槽爪式分酸器已不能满足生产需要，易造成吸收率差、吸收塔出口气体带沫，严重影响了固体亚硫铵品质。     

大塔径硫酸吸收塔阳极保护槽管式分酸器的应用

介绍阳极保护不锈钢槽管式分酸器在云南三环化工有限公司600kt/a硫磺制酸装置DN7000大塔径上的应用情况,分析分酸器在水联动试运行中出现液体分布不均匀的原因及处理办法。     

MDEA脱碳改造CO2吸收塔主要参数的确定

介绍了四川美丰化肥分公司100 kt/a合成氨装置搬迁MDEA脱碳工序改造整体更换CO2吸收塔实例,并对新的CO2吸收塔的塔径、填料压降、填料高度、贫液段填料高度等主要参数进行了确认计算.     

韶关冶炼厂1~#系统硫酸干吸改造

介绍了韶冶1#系统硫酸装置的工艺流程及设备,主要介绍了1#系统硫酸干吸塔的改造情况,通过改造,改善了有关工艺指标的控制,有效的提高了系统生产能力,并进一步的改善了环保排放和节能减排。     

二氧化碳吸收塔和再生塔改造

介绍西天然气化工有限责任公司合成氨装置脱碳系统中的吸收塔和再生塔的填料分布器工艺改造及该项目收到的良好经济效益和社会效益。     

填料吸收塔操作性能的综合研究

合理的操作是优化设计的保证,本文从这一角度对填料吸收塔作了一些探讨。分别采用空气-水系统和空气-氨-水系统对16mm×16mm×2mm瓷拉西环填料塔的流体力学性能和传质性能进行了综合实验研究。研究结果表明:若填料层内存有污垢,相同气速下的压降增加40％～260％;接近泛点气速下进行传质操作效率最佳;泛点气速的实测值与计算值相比偏差在5％以内。此外,本文还提出合理确定传质操作过程稳定时间的方法。     

管式分酸器在硫酸生产中的使用效果

管式分酸器应用于硫铁矿沸腾焙烧制酸装置,效果显著,与原挂钩槽式分酸器相比,干燥塔出口水份含量从０．４ｇ／ｍ＾３降至０．０８ｇ／ｍ＾３。     

230kt/a硫酸净化装置生产实践

大冶有色金属公司冶炼厂硫酸三系统净化工序采用了填料塔带板式酸冷却器的稀酸直接冷却净化流程取代传统的间冷净化流程,同时积极采用了高效防腐材料。经过近３年的生产实践证实：该流程工艺成熟,能满足净化工序降温、降尘、除雾的工艺要求,且抗腐蚀性能强。     

错流填料吸收塔吸收率的测定

填料塔是一种常用的气液传质设备,通过对传统填料塔内气液二相流动行为的研究,提出了一种带折流挡板的新型填料塔——错流填料塔。实验表明,错流填料塔能更好地消除壁流,改善气液二相的接触状况;错流填料塔的吸收率明显大于普通填料塔,在气液二相流量一定时,吸收率随着H/D(板间距与塔径之比)的减小而逐渐增大,当H/D=0.8时,吸收率最大;当H/D<0.8时,随着气量的增加,吸收率逐渐减小,仅在小气速下,吸收率较大,在气速较大时,由于压降过大,导致吸收操作无法正常进行。     

传质型塔间冷却器传热性能的试验研究

对传质型塔间冷却器的传热性能进行了试验研究。在换热管内填充金属填料后,冷却器的传热性能大大提高,传热系数比空管提高了４９％～１０１％,所需传热温差减少,温度分布均匀。     

规整填料在化肥工业吸收塔上的应用

介绍规整料与新型分布器的特性，及其在中、小型化肥厂的脱硫、脱碳、铜洗等工艺中应用的生产数据和成功范例。     

绝热吸收的理论模型和求解方法

本文对伴有溶剂挥发的绝热吸收过程进行分析，建立了描述填料塔内气液浓度分布和温度分布的微分方程组，采用二元三次样条插值拟合平衡数据，运用ＲｕｎｇｅＫｕｔｔａ法试差求解气液浓度分布、温度分布以及所需填料层高度。     

Impac塔填料在冷却塔中的应用

在对比国内外冷却塔填料现场应用情况的基础上，总结了Impac塔填料及喷嘴应用的优势及存在的问题，说明了Impac塔填料热力性能传质传热效果及Lantc喷头的布水情况，通过经济效益对比分析表明，该填料及喷头具有良好的应用前景；同时，该填料具有施工安装方便等特点，对解决冷却塔冬季结冰也有好处，为冷却塔改造填料喷嘴的选型提供了新途径。     

等高双抱杆对抬滑移法

等高双抱杆对抬滑移法付桂生（江西第二化肥厂）关键词等高双抱杆吊装填料塔符号说明Ｇ———每根抱杆重量,Ｇ＝６ｔ;Ｋ———动载荷系数,取Ｋ＝１．１;Ｋ′———不均衡系数,取Ｋ′＝１１;Ｋ１———滑车组机械利益系数;Ｋ２———安全系数,Ｋ２＝３５;Ｌ...     

韶关冶炼厂干吸塔分酸装置的改造

介绍了韶关冶炼厂干吸塔分酸装置的改造情况。通过对塔本身的具体情况和分酸装置的调研,先后选用多种更为先进的分酸装置更换了老式的分酸装置,改善了有关工艺指标控制,并进一步改善了环保排放,节能降耗效果较好。     

横掠钉头管对流换热的实验研究

利用热质比拟原理及萘升华技术,对横掠钉头管的对流换热进行了实验研究。对管面上及钉头上的放热系数分别进行了测量,并对其做了比较。最后给出了计算钉头管平均放热的实验关联式。     

Kinetics study of carbon dioxide absorption in aqueous solutions of 1,6-hexamethyldiamine (HMDA) and 1,6-hexamethyldiamine, N,N′ di-methyl (HMDA, N,N′)

A study towards the kinetics of CO₂ in aqueous solutions of 1,6-hexamethyl diamine (HMDA) and 1,6-hexamethyl diamine, N,N′ di-methyl (HMDA, N,N′) was performed at concentrations ranging from 0.5 to 2.5 mol/L and temperatures from 283 up to 303 K. The kinetics data were determined by CO₂ absorption experiments using a stirred cell reactor with a flat interface between gas and liquid. These new CO₂ solvents were identified in earlier work for their high CO₂ capacity and limited corrosiveness. The experimental technique was validated using kinetic experiments for a 2.5 mol/L monoethanolamine solution. In view of double amine functionality and the six carbon chain between the amine groups, attention was paid to whether the amine groups acted independently and whether or not internal cyclisation would affect the carbamate forming mechanism. The reaction order with respect to HMDA was found to vary from 1.4 to 1.8 with increasing temperature. Absorption experiments in an equimolar solution of HMDA with HCl showed that the two amine groups react independently from each other towards CO₂. The reactivity of both diamines was more than five times larger than for monoethanolamine. The secondary diamine HMDA, N,N′ was found to be even more reactive towards CO₂. Additionally, the effect of CO₂ loading on the kinetics was studied for 0.5 mol/L aqueous solutions of HMDA and HMDA, N,N′ at 293 K. Both solvents are from absorption kinetics point of view good candidates for further evaluation as solvent (-component) for CO₂ capture.     

薄管板强度计算及设计方法

本文结合目前国际上常用的几种管板计算方法以及我国国家标准所采用的方法，提出薄管板强度计算及设计方法，以供设计时参考。     

Modeling of absorption of NO<Superscript>2</Superscript> with chemical reaction in a falling raindrop

A model has been proposed for the scavenging of NO₂ in a falling raindrop. After absorption, aqueous NO, undergoes a second order reaction to form various ions such as NO ₂ ^- , NO ₃ ^- and H⁺. The model is based on the unsteady state convective diffusion equation, which was solved for given boundary conditions by using implicit alternate direction (ADI) method. The circulation of fluid inside and outside the raindrop has been taken into account to realistically describe the flow field in the numerical domain. The model predictions indicate that the pH of a raindrop is a direct function of the drop size and bulk concentration of NO,. The model predicted a pH of about 4.9 for a 100-micron raindrop falling through a 20-ppb ambient concentration of NO₂. For the same ambient concentration of NO², a 10-micron raindrop would have a pH of about 4.75. The predictions also suggested that for all practical purposes the gas phase resistance may be taken as the rate-controlling step. The predicted values of gas-side mass transfer coefficient compared well with the estimated values using standard mass transfer correlations.