浙江双林潜心研发，推出多种管材生产线

浙江双林塑料机械有限公司（以下简称“浙江双林”）成立于1987年,20多年来,该公司自主研发出了20多种具有国际先进水平的管材成套设备,包括：PP—R塑铝稳态管生产线、高速PE-RT管材生产线、搭接焊铝塑复合管生产线和对接焊铝塑复合管生产线,以及一步法PE—Xb管材生产线、PB（聚丁烯）管材生产线、铝塑PP—R管生产线、大口径PE管生产线和玻纤增强PP-R管材生产线,此外还包括：3层／5层防渗氧管材生产线、PE非开挖顶管生产线、双壁波纹管生产线、     

推介2011年度青岛塑机行业知名品牌

青岛科润http:/www.kerunsuji.cn青岛科润塑料机械有限公司研发生产各类PE/PP/PPR/PERT/PVC等塑料管材生产线、塑料异型材生产线、木塑型材生产线、塑料板材生产线、PP/PE/PVC木塑板材生产线、塑料片材生产线等。     

青岛顺德塑料机械有限公司

作为中国一家经验丰富的塑料挤出机生产厂商,青岛顺德塑料机械有限公司成盘下1991年,日前已研发出专利产品11项,并通过ISO9001旧际标准质量管理体系队证和欧州CE认证。该公司的书要产品包括：土工材料制造设备生产线,塑料板／片材生产线,管材生产线,塑料异型材生产线,丝、网、趣生产线,迥料棒生产线及回收／辅助设备。     

内黄八成陶企新建生产线

本刊讯近日,笔者从河南内黄陶瓷产业园区管委会了解到,该园区80％的陶瓷企业都在启动新生产线建设。其中,日日升陶瓷新建2条抛光砖生产线;新南亚陶瓷新建1条内墙砖生产线;福惠陶瓷新建1条微晶砖生产线、1条陶瓷刀具生产线;新明珠陶瓷新建1条抛光砖生产线;嘉德陶瓷新建1条中铝球生产线,等等。这些项目在5月中旬动工,预计年内将建成投产。     

PVC“湿碰湿”涂装生产线规划设计概述

每条新建的涂装生产线规划,关系到设备投资成本、生产线工艺流程、厂房土建成本、后期运营成本,因此对涂装生产线的规划设计需慎重对待。奇瑞公司积极响应节能降耗号召,采用PVC“湿碰湿”工艺技术,从而省去PVC独立的烘干炉,达到了节能降耗的目的。从涂装生产线规划设计的角度,阐述了这一条新建生产线的规划设计流程。     

青岛山塑相继研制推出多种塑料挤出设备

青岛山塑挤出设备有限公司不断加大自主创新力度,相继研制推出高效节能型PVC木塑板材生产线、PP/PE共挤木塑型材生产线、PVC药品包装片材生产线和PP-R玻纤稳态增强管材生产线等20多     

德国1亿欧元造特殊薄膜生产线,科思创塑料薄膜生产全球扩张战略再下一城

科思创(Covestro)在全球各地扩建高质量的聚碳酸酯特殊薄膜生产线,包括德国、泰国、中国、美国等,这些新的共挤生产线是为了满足全球不断增长的需求而制造。德国聚碳酸酯薄膜生产线继中国、泰国等地建聚碳酸酯特殊薄膜生产线后,科思创在德国也开始建新的生产线。2021年4月25日公开媒体消息称,科思创已在德国Dormagen工厂启动了高质量的聚碳酸酯特殊薄膜生产线,总投资超过1亿欧元,尽管受到新冠肺炎疫情的影响,但项目仍按计划完成。新生产线的运营将创造大约30个新工作岗位。     

聚丙烯包装生产线系统的完善及改进

我厂聚丙烯包装生产线是一种集机、电、仪一体化的自动包装生产线 ,生产线在运行的过程中 ,出现了很多问题 ,影响了正常生产。针对生产线运行中出现的具体问题 ,进行了一系列系统技术完善和改进 ,取得了满意的效果     

中材16万t玻璃纤维项目在泰安启动

中国中材股份有限公司在泰安的玻璃纤维新材料工业园近日启用,一期年产16万t的玻璃纤维生产线项目也随即启动。该工业园还将逐步建成2亿m工业用布生产线和电子细纱、电解铜箔生产线。据承担玻璃纤维生产线建设和运营的泰山玻璃纤维有限公司介绍,该生产线采用大型池窑全氧燃烧方     

生产合作的成功典范——浙江吉尔泰机械有限公司董事长阮和平先生专访

随着最后一条生产线的正式投产，浙江吉尔泰机械有限公司（以下简称“吉尔泰”）为罗马尼亚INTFOR集团提供的铝塑板生产线、热镀锌生产线和彩钢板涂层生产线、热镀锌生产线和彩钢板涂层生产线3条生产线已经全部交付完成。正如吉尔泰的董事长阮和平先生所说，这是一次成功的“双赢”合作，不仅在行业内引起了巨大的反响，也为国内的设备供应商提供了很好的借鉴。     

Spout diameters in full and half spouted beds

A fiber optic probe has been used to measure spout diameters in a half-column and a full-column based on the significantly higher counts of output electric pulses in the spout region than in the annulus. The flat wall of a semi-cylindrical spouted bed column was found to cause considerable distortion of spout shapes which became approximately semi-elliptical in cross-section. Caution must therefore be exercised when using spout diameter data from the face of half-columns for spouted bed modelling and design. The often-used McNab (1972) equation was found to underestimate the spout diameters in the full-column, with an average deviation of 35.5%.     

Numerical and experimental study on spout elevation in spout‐fluidized beds

The effect of elevating the spout on the dynamics of a spout‐fluidized bed, both numerically and experimentally is studied. The experiments were conducted in a pseudo‐two‐dimensional (2‐D) and a cylindrical three dimensional (3‐D) spout‐fluidized bed, where positron emission particle tracking (PEPT) and particle image velocimetry (PIV) were applied to the pseudo‐2‐D bed, and PEPT and electrical capacitance tomography (ECT) to the cylindrical 3‐D bed. A discrete particle model (DPM) was used to perform full 3‐D simulations of the bed dynamics. Several cases were studied, that is, beds with spout heights of 0, 2, and 4 cm. In the pseudo‐2‐D bed, the spout‐fluidization and jet‐in‐fluidized‐bed regime, were considered first, and it was shown that in the spout–fluidization regime, the expected dead zones appear in the annulus near the bottom of the bed as the spout is elevated. However, in the jet‐in‐fluidized‐bed regime, the circulation pattern of the particles is affected, without the development of stagnant zones. The jet‐in‐fluidized‐bed regime was further investigated, and additionally the experimental results obtained with PIV and PEPT were compared with the DPM simulation results. The experimental results obtained with PIV and PEPT agreed mutually very well, and in addition agreed well wtih the DPM results, although the velocities in the annulus region were slightly over predicted. The latter is probably due to the particle‐wall effects that are more dominant in pseudo‐2‐D systems compared with 3‐D systems. In the jet‐in‐fluidized‐bed regime, the background gas velocity is relatively high, producing bubbles in the annulus that interact with the spout channel. In the case of a non elevated spout, this interaction occurs near the bottom of the bed. As the spout is elevated, this interaction is shifted upwards in the bed, which allows the bubbles to remain undisturbed providing the motion of the particles in the annulus near the bottom of the bed. As a result, no dead zones are created and additionally, circulation patterns are vertically stretched. These findings were also obtained for the cylindrical 3‐D bed; although, the effects were less pronounced. In the cylindrical 3‐D bed the PEPT results show that the effect on the bed dynamics starts at h_spout =1 4 cm, which is confirmed by the ECT results. Additionally, ECT measurements were conducted for h_spout =1 6 cm to verify if indeed the effect happens at larger spout heights. The root mean square of the particle volume fraction slightly increased at h_spout =1 2 cm, whereas a larger increase is found at h_spout = 4 and 6 cm, showing that indeed more bubbles are formed. The presented results have not been reported so far and form valuable input information for improving industrial granulators. © 2011 American Institute of Chemical Engineers AIChE J, 58: 2524–2535, 2012     

Intelligent fitting of minimum spout‐fluidised velocity in spout‐fluidised bed

The experiments were carried on to study the minimum spout‐fluidised velocity in the spout‐fluidised bed. It was found that the minimum spout‐fluidised velocity increased with the rise of static bed height, spout nozzle diameter, particle density, particle diameter, fluidised gas velocity but decreased with the rise of carrier gas density. Based on the experiments, least square support vector machine (LS‐SVM) was established to predict the minimum spout‐fluidised velocity, and adaptive genetic algorithm and cross‐validation algorithm were used to determine the parameters in LS‐SVM. The prediction performance of LS‐SVM is better than that of the empirical correlations and neural network.     

Spout Shape Predictions in Spouted Beds

A theoretical study to predict spout‐annulus interface variation with bed level for different column geometries of spouted beds is proposed. A previous mathematical model (Krzywanski et al., 1989), developed for spout shape predictions in two‐dimensional spouted beds, is here proposed to be applied also for cylindrical, conical or cone‐based cylindrical columns. Its predictions depend on the average spout diameter and on the spout expansion angle. While there exists empirical equations available to estimate the first model parameter, the second one requires a rigorous stress analysis of the particles at the entrance of the bed. To avoid this difficulty, this work proposes a simple mathematical strategy to calculate the spout expansion angle. The reliability of this approach was checked by comparison with several experimental results obtained in cone‐based cylindrical (Lim et al., 1974; Wu et al., 1987; He et al., 1998) and rectangular (Zanoelo, 1994) spouted beds.     

Influence of Operating Parameters on the Average Spout Width in Two‐Dimensional Spouted Beds

In this work a set of experiments were performed in a two‐dimensional spouted bed to study the effect of different operating conditions on the spout cavity width. The measurement of spout‐annulus interface along the bed level was made by visual observations on a flat face column. A numerical integration formula was used to calculate the average spout width. The experimental runs were performed with different materials, bed dimensions, static bed heights, fluid velocities and gas inlet orifice width. The influences of these variables on average spout width were verified through a statistical analysis. An empirical correlation is proposed to predict the average spout width. The empirical model parameters were found through a statistical analysis.     

CFD–DEM investigation into the scaling up of spout‐fluid beds via two interconnected chambers

The hydrodynamics and chamber interaction in a three‐dimensional spout‐fluid bed with two interconnected chambers are investigated via computational fluid dynamics coupled with discrete element method (CFD–DEM), because multiple interconnected chambers are key to scaling up spout‐fluid beds. The overall solid motion, spouting evolution, and spout‐annulus interface is studied, followed by time‐averaged hydrodynamics, particle‐scale information, spout‐annulus interaction, and inter‐chamber interaction. The results show that inter‐chamber interactions lead to unique characteristics distinct from that for a single‐chamber system, including (1) asymmetry of the hydrodynamics within each chamber, (2) alternative spouting behavior in the two chambers, (3) smaller pressure drop in terms of magnitude and fluctuations, (4) two peaks in the solid residence time (SRT) frequency histogram of the annulus, (5) average SRT in the spout is twice that in a single‐chamber, and (6) larger solid dispersion in all three directions. The results provide meaningful understanding for the scale‐up of spout‐fluid beds. © 2016 American Institute of Chemical Engineers AIChE J, 62: 1898–1916, 2016     

Validation of a Discrete Particle Model in a 2D Spout‐Fluid Bed Using Non‐Intrusive Optical Measuring Techniques

To gain insight into the hydrodynamics of spout‐fluid beds, an experimental and numerical study was carried out. Particle image velocimetry was successfully developed and applied to determine particle velocity profiles, whereas voidage profiles were determined by digital image analysis. A 3D hard‐sphere discrete particle model was used to simulate the flow in a spout‐fluid bed. The simulations and experiments showed a similar influence of the background fluidization velocity on the spout behaviour.     

Hydrodynamics of slot‐rectangular spouted beds: Effect of slot configuration on the local flow structure

The local flow structure in a slot‐rectangular spouted bed column of 300 mm × 100 mm cross‐section was investigated with slots of equal area but different length‐to‐width ratios. Dead‐zones, spout shapes, and distributions of pressure, particle velocity, and voidage were explored. The local flow structure of the slot‐rectangular spouted bed became similar to conventional spouted beds as the height increased, with spouts from slots of different length‐to‐width ratios approaching similarity in the upper part of the bed. Static bed height was found to have little influence on the flow in the spout at a given level.     

Voidage and particle velocity profiles in a spout‐fluid bed

Detailed hydodynamic measurements have been obtained for fully cylindrical spout‐fluid beds of 1.3 mm, 1.8 mm and 2.5 mm glass beads in a fully cylindrical column of diameter 152 mm using three different types of optical fibre probes. The reallocation of up to 43% of the air to auxiliary air introduced through the conical base caused some decrease in spout voidages, but remarkably little change in spout diameter compared with spouted beds where there was no auxiliary air addition. Auxiliary air led also to some decrease in particle velocities in the spout and to a modest decrease in the net solids circulation rate.     

Improving the operational stability of the multi‐chamber spout‐fluid bed via the insertion of a submerged partition plate

The effect of a submerged partition plate on improving the gas–solid flow robustness and stability in a three‐dimensional spout‐fluid bed with multiple inter‐connected chambers is numerically investigated by means of computational fluid dynamics coupled with discrete element method (CFD‐DEM). Notably, multiple‐chamber beds are necessary in scaling up the spout‐fluid bed. The influence of plate height on gas–solid distribution, spout‐annulus interaction and chamber interaction are also studied to optimize the design. The results demonstrate that inserting a partition plate with height above a certain threshold can effectively improve the stability of spouting and uniformly re‐distribute the flux load in each chamber, giving rise to parallel fountains and lower circulation flux of the solid phase. Results indicate that the plate height should be at least 80% of the packed bed height investigated, with the most optimal being about 92% based on steady spouting, and the maximum solid and gas exchanging fluxes between the chambers. © 2016 American Institute of Chemical Engineers AIChE J, 63: 485–500, 2017