CN1309803C - 减少初分馏塔中泡沫的方法 - Google Patents
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Abstract
本发明包含改进由于聚合烃类的沉积而出现操作效率下降的初分馏塔中的操作参数的方法。本发明包括将减少泡沫量的消泡组合物加到初分馏塔处的步骤。达到减少起泡,从而在包括但不限液-气接触比、产品最高温度、压力差、汽油终馏点或其组合的操作参数的基础上改进本方法的操作效率。
Description
发明背景和发明概述
本发明涉及一种在乙烯装置中操作带有防结垢剂特别是消泡剂的初分馏塔(也称为急冷塔)的方法。
在轻质烃类产品例如乙烯的生产中,重质烃类例如石脑油或柴油在热解加热炉中在约850℃下裂解,生成小分子包括但不限于乙烯、丙烯和丁二烯的混合物。这样的混合物通常称为裂解气体,将它们在乙烯装置的不同阶段中冷却,一直到它们在乙烯装置的分馏段中分离。
在主要热量回收过程中,裂解气体在用重油急冷以前先通过一系列换热器(也称为输送管线换热器)并冷却。这种重油称为急冷油或塔底急冷油,它在初分馏塔塔底积累。初分馏塔含有燃料油的不同组分,从塔底馏分到塔精馏段的馏分。塔精馏段易发生与各种物质有关的严重结垢问题,例如苯乙烯、茚、二乙烯基苯、α-甲基苯乙烯、茚衍生物、萘和其他高级环状化合物衍生物。
这些物质的聚合产物以很高的速率不仅沉积在上部塔板表面,而且也沉积在下部塔板表面。由于这一结垢问题,塔内的压力降增加,伴随分馏效率下降。因此,对急冷水塔中冷凝的汽油质量以及体系产生的燃料油质量有不良影响。通常,由于初分馏塔的不适当操作,精馏段中结垢的问题也伴随急冷油塔塔底的粘度控制差。由于可利用的表面积下降,结垢物质(通常为聚合物)的沉积阻碍分馏塔内的汽液流动,这样的环境促使塔中产生更多的泡沫。泡沫的存在进一步使压力降增加,导致更高沸点的产物带入轻质产品,反之亦然。由于过量的起泡,塔的压力降迅速增加,并成为装置效率下降的主要原因。
随着结垢继续出现,塔中的结垢速率也增加,使装置的操作人员必需大幅降低装置的进料速率,而最终使装置停工,以便清洗初分馏塔。
本发明提供一种将适合的化学剂送入以便延长初分馏塔的操作时间来操作由于聚合物沉积而结垢的初分馏塔的方法。
附图简介
图1说明实施例1的数据,其中初分馏塔的进料速率、回流速率和塔压力对时间作图。
图2说明实施例2收集的数据,其中急冷塔的塔压力对时间作图。
发明详述
本发明包括减少由于聚合的烃类物质的沉积使操作效率下降的初分馏塔中的泡沫的方法。本发明包含将减少泡沫量的消泡组合物在初分馏塔处加入的步骤。起泡减少,从而根据操作参数提高所述方法的操作效率,这些操作参数包括但不限于液-气接触比、产物的最高温度、压力差、汽油终馏点或其组合。
优选的消泡组合物为聚硅氧烷。适用于本发明的代表性的聚硅氧烷为二甲基聚硅氧烷。它是一种商业上可得到的化学品,例如可从Dorf Ketal Chemicals India Pvt.Ltd.购买。其他适合的消泡组合物包括但不限于环氧乙烷-环氧丙烷共聚物、脂肪酸乙氧基化物、聚异丁烯和脂肪酸酯。这些化合物的适合例子也可从Dorf KetalChemicals India Pvt.Ltd得到。
可以纯的形式或在任何适合的溶剂中将消泡组合物加到本方法中。代表性的溶剂可为芳族特性的,包括但不限于甲苯、二甲苯、石脑油。优选将消泡组合物加到存在起泡问题的特定位置的上游或直接加到存在起泡问题的位置。具体地说,减少沉积的组合物可连续地或周期性地加到初分馏塔的回流中。初分馏塔本身可包含各种内部组件,包括波纹塔板、筛板塔板、泡帽塔板、浮阀塔板等。
上述优选的聚硅氧烷可以最终的使用浓度为0.0001%至0.1%加到本方法中,0.0005%至0.0025%为优选的范围(在这里所有百分数以重量/重量为基础表示)。这些百分数转换成1至约1000ppm烃类的使用剂量率。具体的剂量可由特定方法中的条件来决定。虽然提供了最优选的聚硅氧烷范围,但是应认识到本发明不受这里示出的具体化合物或浓度的限制。进一步预计本发明可用于有其他烃类处理试剂例如防腐蚀组合物的方法。
提供以下实施例仅仅为了清楚地说明本发明,这些实施例决不作为对本发明范围的限制。
实施例1
在包括乙烯、丙烯和丁二烯在内的轻质烃类的生产中,使用石脑油的乙烯生产装置出现初分馏塔的结垢,甚至在低于正常进料速率下操作时也使塔的效率下降。鉴于甚至在装置进料速率下降20%时由更高的塔压降和高的汽油终馏点所表明的塔效损失,装置操作人员试图将装置停工,以便清洗分馏塔。
但是,本发明在相应方法的基础上实施,以便达到可接受的操作参数,从而证明了本发明的实用性。将含有聚硅氧烷的消泡剂与回流一起注入到塔中。特定的消泡剂为Dorf Ketal Chemicals India Pvt.Ltd.提供的二甲基聚硅氧烷,并将它送入塔中,以致达到约100ppm的操作浓度。
在使用消泡剂数小时内,如图1所示,塔的压力降减少。观察到在结垢的条件下,汽油的终馏点提高20℃,同时也反映在相应汽油的颜色上。结垢的条件得到褐色汽油,而汽油通常为浅黄绿色。聚硅氧烷注入回流以后,装置操作人员随后观察到汽油的颜色恢复正常的浅黄绿色,同时汽油的终馏点下降,表明塔的操作得到改善。
图1说明与这一实验有关的数据,其中X轴为时间,左侧Y轴为公斤/小时表示的进料速率和回流质量。此外,右侧Y轴为公斤/厘米2表示的压力降。箭头A表示聚硅氧烷化合物初始注入回流。测量塔压力,正如X轴所示。图中的数据清楚看到塔压力明显下降。
实施例2
由于塔的压降增加,装置出现结垢问题。该装置中的压力降正常数值为0.07-0.08公斤/厘米2。但是,结垢问题使压力降达到0.135-0.15公斤/厘米2的高得多的数值。由于结垢问题,虽然塔内的压力降仍很高,但观察到进料速率和回流速率下降。
为了避免生产装置高费用的停工,装置操作人员利用了本发明,其中将聚硅氧烷注入急冷塔,按塔回流速率计,其注入速率为10-20ppm。所用的具体聚硅氧烷与实施例1相同。
在最初注入消泡剂数小时内,操作人员观察到塔压力下降到约0.109公斤/厘米2,而进料速率从175吨/小时石脑油提高到184吨/小时石脑油。在相同时期内,回流速率从20吨/小时提高到30吨/小时。图2示出塔操作的改进,其中X轴表示取样次数,而Y轴表示以公斤/厘米2表示的塔压力。
虽然已结合优选的实施方案描述了本发明,但熟悉本专业的技术人员应认识到,在不违背本发明精神实质的条件下可作出各种替代、更换和省略。因此,上面的描述仅作为例证,而不应作为以下权利要求书表明的本发明范围的限制。
Claims (24)
1.一种操作乙烯生产装置中用于主要热量回收的结垢急冷塔的方法,所述的方法包括以下步骤:
a)将裂解气体送入用于从裂解气体中除去热量的急冷塔中,其中裂解气体通过急冷塔的塔顶排出;以及
b)将选自聚硅氧烷、环氧乙烷-环氧丙烷共聚物、脂肪酸乙氧基化物、聚异丁烯和脂肪酸酯的添加剂加到急冷塔中,从而使操作中的急冷塔的压力降降低。
2.根据权利要求1的方法,其中将添加剂送入急冷塔,以便达到约0.01至约5000ppm的剂量。
3.根据权利要求1的方法,其中将添加剂送入急冷塔的回流中。
4.根据权利要求1的方法,其中将添加剂连续地送入急冷塔的回流中。
5.根据权利要求1的方法,其中将添加剂周期性地送入急冷塔的回流中。
6.根据权利要求1的方法,其中添加剂还包含选自甲苯、二甲苯和石脑油的溶剂。
7.根据权利要求1的方法,其中聚硅氧烷为二甲基聚硅氧烷。
8.根据权利要求1的方法,还包括以下步骤:
c)在液-气接触比、进料速率、回流速率和产品最高温度、汽油终馏点或压力差中至少一项的基础上测量分馏塔的操作效率。
9.一种使乙烯生产装置中用于主要热量回收的操作中的结垢急冷塔的温度分布正常化的方法,所述的方法包括以下步骤:
a)将裂解气体送入用于从裂解气体中除去热量的急冷塔中,其中裂解气体通过急冷塔的塔顶排出;以及
b)将选自聚硅氧烷、环氧乙烷-环氧丙烷共聚物、脂肪酸乙氧基化物、聚异丁烯和脂肪酸酯的添加剂加到急冷塔中,从而使操作的急冷塔中的温度分布正常化。
10.根据权利要求9的方法,其中将添加剂送入急冷塔,以便达到约0.01至约5000ppm的剂量。
11.根据权利要求9的方法,其中将添加剂送入急冷塔的回流中。
12.根据权利要求9的方法,其中将添加剂连续地送入急冷塔的回流中。
13.根据权利要求9的方法,其中将添加剂周期性地送入急冷塔的回流中。
14.根据权利要求9的方法,其中添加剂还包含选自甲苯、二甲苯和石脑油的溶剂。
15.根据权利要求9的方法,其中聚硅氧烷为二甲基聚硅氧烷。
16.根据权利要求9的方法,还包括以下步骤:
c)在液-气接触比、进料速率、回流速率和产品最高温度、汽油终馏点或压力差中至少一项的基础上测量急冷塔的操作效率。
17.一种改进裂解气体生产装置中热量回收的方法,所述的方法包括以下步骤:
a)将裂解气体送入用于从裂解气体中除去热量的急冷塔中,其中裂解气体通过急冷塔的塔顶排出;以及
b)将选自聚硅氧烷、环氧乙烷-环氧丙烷共聚物、脂肪酸乙氧基化物、聚异丁烯和脂肪酸酯的添加剂加到急冷塔中,从而使操作中的急冷塔的随后操作中的主要热量回收得到改进。
18.根据权利要求17的方法,其中将添加剂送入急冷塔,以便达到约0.01至约5000ppm的剂量。
19.根据权利要求17的方法,其中将添加剂送入急冷塔的回流中。
20.根据权利要求17的方法,其中将添加剂连续地送入急冷塔的回流中。
21.根据权利要求17的方法,其中将添加剂周期性地送入急冷塔的回流中。
22.根据权利要求17的方法,其中添加剂还包含选自甲苯、二甲苯和石脑油的溶剂。
23.根据权利要求17的方法,其中聚硅氧烷为二甲基聚硅氧烷。
24.权利要求17的方法,还包括以下步骤:
c)在液-气接触比、进料速率、回流速率和产品最高温度、汽油终馏点或压力差中至少一项的基础上测量急冷塔的操作效率。
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US10/196,725 US7906012B2 (en) | 2002-07-16 | 2002-07-16 | Method for reducing foam in a primary fractionator |
US10/196,725 | 2002-07-16 |
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EP (1) | EP1525288B1 (zh) |
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AU (1) | AU2002347587A1 (zh) |
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US7906012B2 (en) | 2002-07-16 | 2011-03-15 | Dorf Ketal Chemicals India Pvt. Ltd. | Method for reducing foam in a primary fractionator |
CN112642179B (zh) * | 2020-12-18 | 2022-09-30 | 宁波顺泽橡胶有限公司 | 一种丁腈橡胶生产凝聚破乳消泡装置 |
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- 2002-07-16 US US10/196,725 patent/US7906012B2/en not_active Expired - Fee Related
- 2002-09-30 AU AU2002347587A patent/AU2002347587A1/en not_active Abandoned
- 2002-09-30 EP EP02783511.5A patent/EP1525288B1/en not_active Expired - Lifetime
- 2002-09-30 BR BR0215808-6A patent/BR0215808A/pt not_active Application Discontinuation
- 2002-09-30 WO PCT/IN2002/000196 patent/WO2004007642A1/en active Search and Examination
- 2002-09-30 JP JP2004521071A patent/JP4227099B2/ja not_active Expired - Fee Related
- 2002-09-30 ES ES02783511.5T patent/ES2590802T3/es not_active Expired - Lifetime
- 2002-09-30 CN CNB028294211A patent/CN1309803C/zh not_active Expired - Fee Related
-
2005
- 2005-01-14 ZA ZA200500373A patent/ZA200500373B/en unknown
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Also Published As
Publication number | Publication date |
---|---|
EP1525288A1 (en) | 2005-04-27 |
JP2005539102A (ja) | 2005-12-22 |
US7906012B2 (en) | 2011-03-15 |
EP1525288B1 (en) | 2016-06-15 |
WO2004007642A1 (en) | 2004-01-22 |
ES2590802T3 (es) | 2016-11-23 |
ZA200500373B (en) | 2006-07-26 |
CN1649982A (zh) | 2005-08-03 |
BR0215808A (pt) | 2005-04-26 |
JP4227099B2 (ja) | 2009-02-18 |
AU2002347587A1 (en) | 2004-02-02 |
US20040015032A1 (en) | 2004-01-22 |
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