【摘要】：在以鋁或沸石為載體的鉑催化劑上,直鏈烷烴脫氫生成直鏈單烯烴,作為烷基苯生產(chǎn)的工業(yè)原料。脫氫反應(yīng)通常在徑向反應(yīng)器中進(jìn)行。本論文以金陵石化公司烷基苯廠的烷烴脫氫裝置作為研究對象,該脫氫裝置是在傳統(tǒng)徑向反應(yīng)器的基礎(chǔ)上進(jìn)行技術(shù)改造,成為了有兩個(gè)催化劑床層的氣固雙環(huán)徑向反應(yīng)器。與傳統(tǒng)的徑向反應(yīng)器相比,雙環(huán)徑向反應(yīng)器具有床層壓降更低、流通面積更大、流程更短的優(yōu)點(diǎn),所以雙環(huán)徑向反應(yīng)器對于流體處理量大的反應(yīng)有更高的工業(yè)應(yīng)用價(jià)值。本文根據(jù)主流道變質(zhì)量流與顆粒床層氣固流體力學(xué)理論,利用變質(zhì)量流方程、Ergun方程和連續(xù)性方程,建立了完整的雙環(huán)徑向反應(yīng)器流體力學(xué)數(shù)學(xué)模型,開發(fā)了針對模擬計(jì)算雙環(huán)徑向反應(yīng)器內(nèi)外側(cè)催化劑床層氣相二維流場的一種數(shù)學(xué)方法及相應(yīng)的計(jì)算程序,由此可以描述內(nèi)外側(cè)催化劑床層中流體的二維流場和主流道的流體力學(xué)行為。但是和傳統(tǒng)徑向反應(yīng)器相比,雙環(huán)徑向反應(yīng)器由三個(gè)流道(內(nèi)環(huán)隙、外環(huán)隙、中心管)和兩個(gè)床層(內(nèi)外側(cè)催化劑床層)組成,特別的是,在內(nèi)環(huán)隙中,反應(yīng)物流分流分成兩部分分別流入內(nèi)外側(cè)催化劑床層,本文定義了內(nèi)環(huán)隙流體流量分配函數(shù)T,利用Powell算法對分配函數(shù)T進(jìn)行優(yōu)化。利用中心管和外環(huán)隙流道出口壓力一致的己知條件進(jìn)行工業(yè)驗(yàn)證,證明模型的可靠性。本文利用建立的數(shù)學(xué)模型模擬計(jì)算了不同結(jié)構(gòu)尺寸時(shí)雙環(huán)徑向反應(yīng)器的流場分布,主要是通過內(nèi)外側(cè)催化劑床層的質(zhì)量空速和內(nèi)外環(huán)的軸向分流均勻度的變化,尋找合適的反應(yīng)器尺寸來平衡雙環(huán)徑向反應(yīng)器的內(nèi)外環(huán)。模擬結(jié)果顯示,改變內(nèi)側(cè)催化劑床層內(nèi)徑,除了中心管的外徑改變外,其它反應(yīng)器的尺寸保持不變,內(nèi)側(cè)催化劑床層最佳的內(nèi)徑范圍是0.3175～0.3195 m;改變外側(cè)催化劑床層外徑,除了外環(huán)隙的內(nèi)徑改變外,其它反應(yīng)器的尺寸保持不變,外側(cè)催化劑床層最佳的外徑范圍是0.907～0.910 m。此時(shí)雙環(huán)徑向反應(yīng)器的內(nèi)外環(huán)基本處于平衡的狀態(tài)。該模型不僅可以用來分析現(xiàn)有工業(yè)脫氫反應(yīng)器結(jié)構(gòu)設(shè)計(jì)的合理性,還可以為以后雙環(huán)徑向反應(yīng)器的設(shè)計(jì)提供定量的參考依據(jù)。
[Abstract]:On platinum catalyst supported on aluminum or zeolite, straight chain alkanes were dehydrogenated to form straight chain monoolefins, which were used as industrial raw materials for the production of alkyl benzene. Dehydrogenation usually takes place in a radial reactor. In this paper, the alkane dehydrogenation unit of Jinling Petrochemical Company is taken as the research object. The dehydrogenation unit is based on the traditional radial reactor and has been transformed into a gas-solid double-ring radial reactor with two catalyst beds. Compared with the traditional radial reactor, the dual-loop radial reactor has the advantages of lower pressure drop, larger circulation area and shorter flow rate. Therefore, the dual-loop radial reactor has higher industrial application value for the reaction with large fluid handling capacity. Based on the theory of gas-solid fluid mechanics of variable mass flow and particle bed in mainstream channel, a complete mathematical model of hydrodynamics for dual loop radial reactor is established by using the Ergun equation and continuity equation of variable mass flow equation. A mathematical method and a corresponding program for simulating the gas phase two-dimensional flow field of the catalyst bed inside and outside the double ring radial reactor are developed. The two dimensional flow field and the hydrodynamic behavior of the main channel in the inner and outer side catalyst bed can be described. But compared with the conventional radial reactor, the double-ring radial reactor consists of three channels (inner ring, outer ring, central tube) and two beds (inside and outside the catalyst bed), especially in the inner ring. The reaction material flow is divided into two parts, which flow into the inner and outer side of the catalyst bed respectively. In this paper, the internal annular fluid flow distribution function T is defined, and the distribution function T is optimized by Powell algorithm. The model is proved to be reliable by using the known conditions of uniform outlet pressure between the central tube and the outer annular channel. In this paper, the flow field distribution of the dual ring radial reactor with different structure sizes is simulated by using the established mathematical model, mainly through the variation of the mass space velocity of the inner and outer side catalyst bed and the axial distributary uniformity of the inner and outer ring. Find the appropriate reactor size to balance the inner and outer rings of the dual loop radial reactor. The simulation results show that the inner diameter of the inner catalyst bed remains unchanged except for the outer diameter of the central tube, and the optimum inner diameter range of the inner catalyst bed is 0.3175 ~ 0.3195 m, and the outer diameter of the outer catalyst bed is changed. Except the change of inner diameter of outer ring gap, the size of other reactors remained unchanged, and the optimum outer diameter range of outside catalyst bed was 0.907 ~ 0.910 m. At this time, the inner and outer rings of the dual ring radial reactor are basically in equilibrium state. The model can not only be used to analyze the rationality of the structural design of the existing industrial dehydrogenation reactor, but also provide a quantitative reference for the design of the dual-ring radial reactor.
【學(xué)位授予單位】：華東理工大學(xué)
【學(xué)位級別】：碩士
【學(xué)位授予年份】：2017
【分類號】：TQ052.5

【相似文獻(xiàn)】

相關(guān)期刊論文 前10條

1 ;冷壁徑向反應(yīng)器使用情況[J];石油煉制與化工;1978年08期

2 ;徑向反應(yīng)器流體均布的研究[J];化學(xué)工程;1978年06期

3 張成芳,朱子彬,徐懋生,朱炳辰;徑向反應(yīng)器流體均布設(shè)計(jì)的研究(Ⅰ)[J];化學(xué)工程;1980年01期

4 張成芳,朱子彬,徐懋生,朱炳辰;徑向反應(yīng)器流體均布設(shè)計(jì)的研究(Ⅱ)[J];化學(xué)工程;1980年02期

5 陳敏恒,袁渭康,張琪宏;絕熱固定床反應(yīng)器的研究——(Ⅲ)徑向反應(yīng)器著火規(guī)律和溫度分布[J];化工學(xué)報(bào);1985年04期

6 宋續(xù)祺,汪展文,金涌,龔美珊;移動(dòng)床徑向反應(yīng)器中流體力學(xué)行為的研究[J];化工學(xué)報(bào);1992年03期

7 宋續(xù)祺,金涌,俞芷青,龔美珊;移動(dòng)床徑向反應(yīng)器中氣體離心流動(dòng)對顆粒移動(dòng)狀況的影響[J];化工學(xué)報(bào);1993年04期

8 宋續(xù)祺,金涌,龔美珊;移動(dòng)床徑向反應(yīng)器的催化劑顆粒層中應(yīng)力分布和貼壁現(xiàn)象產(chǎn)生的條件[J];高校化學(xué)工程學(xué)報(bào);1993年04期

9 董家梅，陳琳;徑向反應(yīng)器變徑段結(jié)構(gòu)的可靠性研究[J];天然氣與石油;1995年04期

10 王金福,杜曉華,金涌,俞芷青;重整徑向反應(yīng)器布?xì)庀到y(tǒng)的流體力學(xué)行為及其優(yōu)化設(shè)計(jì)[J];石油煉制與化工;1997年04期

相關(guān)碩士學(xué)位論文 前1條

1 李景;工業(yè)脫氫反應(yīng)器流動(dòng)模擬[D];華東理工大學(xué);2015年

，

本文編號：2120619