计算机与应用化学
計算機與應用化學
계산궤여응용화학
COMPUTERS AND APPLIED CHEMISTRY
2013年
8期
883-886
,共4页
李洋%李玉刚%张兵%程华农
李洋%李玉剛%張兵%程華農
리양%리옥강%장병%정화농
3,4-二氯苯胺%精制%分离流程%模拟%分析
3,4-二氯苯胺%精製%分離流程%模擬%分析
3,4-이록분알%정제%분리류정%모의%분석
3.4-dichloroaniline%purification%separation processes%simulation%analysis
通过催化加氢反应产物3,4-二氯苯胺的热稳定性实验，得出产物中的胺基盐酸盐不会受热分解成 HCl，对精馏设备不会产生腐蚀。通过抑制剂降解实验和产品热稳定性实验得出精馏塔釜温度须控制在190℃以下，可以有效避免抑制剂分解、产品色度变大。采用 ASPEN 软件对年产5000吨3,4-二氯苯胺产品分离工艺进行模拟和分析，确定精馏分离序列为先脱甲醇，再脱除水和轻组分，最后脱焦油，得到产品。脱甲醇塔常压操作，塔顶甲醇纯度为99.9%，塔底甲醇质量分率10 mg.l-1，理论板数为26，进料位置在第15块板,对应回流量为3000 kg.h-1。脱轻塔常压操作，塔底温度175℃，塔底苯胺含量10 mg.l-1，理论板数为26，进料位置在第7块板，回流量为1590 kg.h-1。焦油塔塔底强制循环，产品侧线采出，产品的质量分率可达100%，回流量为1500 kg.h-1，进料位置为第30块。整个分离过程产品的收率为99.15%。
通過催化加氫反應產物3,4-二氯苯胺的熱穩定性實驗，得齣產物中的胺基鹽痠鹽不會受熱分解成 HCl，對精餾設備不會產生腐蝕。通過抑製劑降解實驗和產品熱穩定性實驗得齣精餾塔釜溫度鬚控製在190℃以下，可以有效避免抑製劑分解、產品色度變大。採用 ASPEN 軟件對年產5000噸3,4-二氯苯胺產品分離工藝進行模擬和分析，確定精餾分離序列為先脫甲醇，再脫除水和輕組分，最後脫焦油，得到產品。脫甲醇塔常壓操作，塔頂甲醇純度為99.9%，塔底甲醇質量分率10 mg.l-1，理論闆數為26，進料位置在第15塊闆,對應迴流量為3000 kg.h-1。脫輕塔常壓操作，塔底溫度175℃，塔底苯胺含量10 mg.l-1，理論闆數為26，進料位置在第7塊闆，迴流量為1590 kg.h-1。焦油塔塔底彊製循環，產品側線採齣，產品的質量分率可達100%，迴流量為1500 kg.h-1，進料位置為第30塊。整箇分離過程產品的收率為99.15%。
통과최화가경반응산물3,4-이록분알적열은정성실험，득출산물중적알기염산염불회수열분해성 HCl，대정류설비불회산생부식。통과억제제강해실험화산품열은정성실험득출정류탑부온도수공제재190℃이하，가이유효피면억제제분해、산품색도변대。채용 ASPEN 연건대년산5000둔3,4-이록분알산품분리공예진행모의화분석，학정정류분리서렬위선탈갑순，재탈제수화경조분，최후탈초유，득도산품。탈갑순탑상압조작，탑정갑순순도위99.9%，탑저갑순질량분솔10 mg.l-1，이론판수위26，진료위치재제15괴판,대응회류량위3000 kg.h-1。탈경탑상압조작，탑저온도175℃，탑저분알함량10 mg.l-1，이론판수위26，진료위치재제7괴판，회류량위1590 kg.h-1。초유탑탑저강제순배，산품측선채출，산품적질량분솔가체100%，회류량위1500 kg.h-1，진료위치위제30괴。정개분리과정산품적수솔위99.15%。
Through the thermostability experiment of 3, 4-dichloroaniline, which is the product of catalytic hydrogenation reaction, it is found that the amine hydrochloride of 3,4-dichloroaniline will not be pyrolyzed to HCl, and no corrosion to distillation equipment. Through the experiments of inhibitor degradation and thermostability of product, it is found that the rectification tower kettle temperature must be controlled under 190℃so that the inhibitor decomposion and the chromaticity of product becoming bigger could be avoided effectively. Using ASPEN to simulate and analyze the separation technology which could produce 3, 4-dichloroaniline 5000 t per year, the separation sequence is found, that remove methyl alcohol firstly, then the water and the light constituent, then remove the tar lastly, and get the product. It is operated under atmospheric pressure in the methyl alcohol removal tower, the purity of methyl alcohol in the supertower is 99.9%, but the mass fraction of methyl alcohol in bottom is 10 mg.l-1. The theoretical plates number is 26, feed at the 15 plate, and the quantity of reflux is 3000 kg.h-1. It is also operated under atmospheric pressure in the light constituent removal tower, the bottom temperature is 175 ℃, and the mass fraction of phenylamine in bottom is 10 mg.l-1. The theoretical plates number is 26, feed at the 7 plate, and the quantity of reflux is 1590 kg.h-1. It is forced to circulate in the bottom tower of tar, the product is side-draw, and the mass fraction could reach to 100%, and the quantity of reflux is 1500 kg.h-1, and feed at the 30 plate. The yield of product is 99.15%in the whole separation process.
