CN102886151A - 一种三塔甲醇精馏热能回收装置及方法 - Google Patents

一种三塔甲醇精馏热能回收装置及方法 Download PDF

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CN102886151A
CN102886151A CN2012103778472A CN201210377847A CN102886151A CN 102886151 A CN102886151 A CN 102886151A CN 2012103778472 A CN2012103778472 A CN 2012103778472A CN 201210377847 A CN201210377847 A CN 201210377847A CN 102886151 A CN102886151 A CN 102886151A
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张兆振
陈广喜
刘伟
刘建
杨明
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Anhui Jinmei Zhongneng Chemical Co Ltd
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Abstract

本发明公开了一种三塔甲醇精馏热能回收装置及方法,包括有加压塔甲醇冷却器,加压塔甲醇冷却器的出料端接入粗甲醇第二加热器,粗甲醇第二加热器的出料端接入预精馏塔,预精馏塔的出料端接入预后加热器,预后加热器的出料端接入加压精馏塔和常压精馏塔,预精馏塔底部并联有预塔再沸器和预塔第二再沸器,加压精馏塔底部并联有加压精馏塔再沸器,加压精馏塔的底部出料端接入预后加热器,加压精馏塔的顶部出料端接入粗甲醇第二加热器,预后加热器的蒸汽冷凝液出口接入预塔第二再沸器。通过本发明的应用,解决了常压精馏塔的精馏段负荷较大,塔顶出气量大,蒸汽及冷却水消耗高等不利因素,实现了节约能源,降低消耗的目的。

Description

一种三塔甲醇精馏热能回收装置及方法
技术领域
    本发明专利涉及煤化工领域,尤其涉及一种三塔甲醇精馏热能回收装置及方法。
背景技术
随着我国国民经济的迅速发展,作为基础化工原料的甲醇,广泛应用医药、染料、涂料及国防工业。近些年来,以甲醇为原料的新产品不断开发,世界对甲醇的生产量和需求量大幅增加。
国内目前对甲醇的精馏方法主要是以二塔及三塔精馏工艺为主,这两种精馏装置在工艺原理和工艺路线上基本相似,都是以甲醇精馏为主,入料温度不能满足甲醇精馏温度的要求,均存在工艺上不合理,对装置中的热量没有回收,后处理热量没有得到有效的回收利用。在传统的精馏工艺生产中加压精馏塔的采出通过循环水来降低温度,加压精馏塔的出料直接进入常压精馏塔中,不仅增加能源消耗,且常压精馏塔的精馏段负荷较大,塔顶出气量大,而且易发生事故,影响安全生产,给操作和安全生产带来一定难度。
在三塔甲醇精馏工艺加压甲醇精馏过程中,根据现有的工艺走向是,加压精馏塔出料直接进入常压精馏塔,而加压精馏塔的出料温度达128℃,远远高于常压精馏塔85℃的精馏温度。这样会导致常压精馏塔的精馏段负荷较大,塔顶出气量大,不仅增加能源消耗,而且易发生事故,影响安全生产。
发明专利内容
本发明专利的目的是为了改进已有技术的不足,提供了一种三塔甲醇精馏热能回收装置及方法。
本发明专利采用的技术方案如下:
一种三塔甲醇精馏热能回收装置及方法,其特征在于:包括有加压塔甲醇冷却器,加压塔甲醇冷却器的出料端接入粗甲醇第二加热器,粗甲醇第二加热器的出料端接入预精馏塔,预精馏塔的出料端接入预后加热器,预后加热器的出料端接入加压精馏塔和常压精馏塔,预精馏塔底部并联有预塔再沸器和预塔第二再沸器,加压精馏塔底部并联有加压精馏塔再沸器,加压精馏塔的底部出料端接入预后加热器,加压精馏塔的顶部出料端接入粗甲醇第二加热器,粗甲醇第二加热器出料端接入加压塔甲醇冷却器,预后加热器的蒸汽冷凝液出口接入预塔第二再沸器。
基于权利要求1所述的三塔甲醇精馏热能回收装置的方法,其特征在于:具体包括以下步骤:
(1)温度35℃的90%粗甲醇以30-40t/h的流量送入加压塔甲醇冷却器①,在进入粗甲醇第二加热器②;
(2)粗甲醇第二加热器②与加压精馏塔⑤以13-18t/h的流量采出的110-113℃甲醇进行换热后,粗甲醇第二加热器②内的甲醇被加热到60-70℃后,进入预精馏塔③进行精馏;
(3)通过加压精馏塔⑤下部的出料在预后加热器④内加热预后甲醇,加压精馏塔⑤下部出料的热量不足,将预后甲醇加热到到103℃左右,达不到加压精馏塔精馏工艺要求的115℃;加压精馏塔再沸器⑨以18-25t/h的流量输出140℃以上的蒸汽冷凝液将预后甲醇由103℃加热到115℃后,再进入加压精馏塔⑤进行甲醇精馏;
(4)预精馏塔③底部并联一台预塔第二再沸器⑧,从预后加热器④以18-25t/h的流量排出的115℃蒸汽冷凝液进入预塔第二再沸器⑧,从而加热预精馏塔③塔底的物料,使预精馏塔③塔底的部分物料气化;
(5)最后,从预后加热器④送入常压精馏塔的甲醇温度不高于90℃。
    本发明专利通过在预精馏、加压精馏生产系统的工艺管路增加预后加热器、粗甲醇第二加热器,使加压精馏系统的出料与预精馏系统的出料在预后加热器中充分换热,加压精馏系统的出料与粗甲醇在加压塔甲醇冷却器充分换热,不仅提高加压精馏塔进料温度,且降低加压精馏塔出料温度和采出温度;预精馏塔下部并联一台预塔第二再沸器,从预后加热器排出的蒸汽冷凝液进入预塔第二再沸器加热预精馏塔塔底的物料,降低预塔再沸器的蒸汽用量,使加压精馏塔的蒸汽冷凝液的热量得到进一步利用,降低蒸汽消耗。
与现有技术相比,本发明专利的优点在于:
本发明专利具有热能回收效率高、蒸汽消耗低等优点,提高加压精馏塔入料温度,降低了加压精馏塔甲醇采出温度,降低了常压精馏塔的入料温度,不仅减少了工艺循环水的消耗量,而且解决了常压精馏塔的精馏段负荷较大,塔顶出气量大,不仅增加能源消耗,而且易发生事故,影响安全生产的问题。
附图说明
图1为本发明的结构示意图。
具体实施方式
参见图1,一种三塔甲醇精馏热能回收装置及方法,包括有加压塔甲醇冷却器①,加压塔甲醇冷却器①的出料端接入粗甲醇第二加热器②,粗甲醇第二加热器②的出料端接入预精馏塔③,预精馏塔③的出料端接入预后加热器④,预后加热器④的出料端接入加压精馏塔⑤和常压精馏塔⑥,预精馏塔③底部并联有预塔再沸器⑦和预塔第二再沸器⑧,加压精馏塔⑤底部并联有加压精馏塔再沸器⑨,加压精馏塔⑤的底部出料端接入预后加热器④,加压精馏塔⑤的顶部出料端接入粗甲醇第二加热器②,粗甲醇第二加热器②出料端接入加压塔甲醇冷却器①,预后加热器④的蒸汽冷凝液出口接入预塔第二再沸器⑧。
三塔甲醇精馏热能回收装置的方法,具体包括以下步骤:
(1)温度35℃的90%粗甲醇以34.7t/h的流量送入加压塔甲醇冷却器①,再进入粗甲醇第二加热器②;
(2)粗甲醇第二加热器②与加压精馏塔⑤以15t/h的流量采出的112℃甲醇进行换热后,粗甲醇第二加热器②内的甲醇被加热到60-70℃后,进入预精馏塔③进行精馏,不仅提高预精馏塔③的入料温度,而且加压精馏塔⑤采出的甲醇由112℃降低到45℃,使加压塔采出甲醇的大量热量得到回收利用;
(3)通过加压精馏塔⑤下部的出料在预后加热器④内加热预后甲醇,加压精馏塔⑤下部出料的热量不足,将预后甲醇由72℃提高到103℃左右,达不到加压精馏塔精馏工艺要求的115℃;通过改进预后加热器④结构,将预后加热器④按二段进行设计,加压精馏塔再沸器⑨以20t/h的流量输出140℃蒸汽冷凝液将预后甲醇由103℃加热到115℃后,再进入加压精馏塔⑤进行甲醇精馏;不仅提高加压精馏塔⑤的入料温度,减少了加压精馏塔再沸器的蒸汽消耗,而且降低常压精馏塔⑥的甲醇入料温度;
(4)预精馏塔③底部并联一台预塔第二再沸器⑧,从预后加热器④以20t/h的流量排出的115℃蒸汽冷凝液进入预塔第二再沸器⑧,从而加热预精馏塔③塔底的物料,使预精馏塔③塔底的部分物料气化;降低预塔再沸器⑦的蒸汽用量,利用了加压精馏塔再沸器⑨蒸汽冷凝液的热量,且降低预塔再沸器⑦的蒸汽消耗,使甲醇精馏的热能实现回收利用;
(5)最后,从预后加热器④送入常压精馏塔的甲醇温度为90℃,解决常压精馏塔⑥的精馏段负荷较大,塔顶出气量大的不合理工艺。

Claims (2)

1.一种三塔甲醇精馏热能回收装置,其特征在于:包括有加压塔甲醇冷却器,加压塔甲醇冷却器的出料端接入粗甲醇第二加热器,粗甲醇第二加热器的出料端接入预精馏塔,预精馏塔的出料端接入预后加热器,预后加热器的出料端接入加压精馏塔和常压精馏塔,预精馏塔底部并联有预塔再沸器和预塔第二再沸器,加压精馏塔底部并联有加压精馏塔再沸器,加压精馏塔的底部出料端接入预后加热器,加压精馏塔的顶部出料端接入粗甲醇第二加热器,粗甲醇第二加热器出料端接入加压塔甲醇冷却器,预后加热器的蒸汽冷凝液出口接入预塔第二再沸器。
2.基于权利要求1所述的三塔甲醇精馏热能回收装置的方法,其特征在于:具体包括以下步骤:
(1)温度35℃的90%粗甲醇以30-40t/h的流量送入加压塔甲醇冷却器①,再进入粗甲醇第二加热器②;
(2)粗甲醇第二加热器②与加压精馏塔⑤以13-18t/h的流量采出的110-113℃甲醇进行换热后,粗甲醇第二加热器②内的甲醇被加热到60-70℃后,进入预精馏塔③进行精馏;
(3)通过加压精馏塔⑤下部的出料在预后加热器④内加热预后甲醇,加压精馏塔⑤下部出料的热量不足,将预后甲醇加热到103℃左右,达不到加压精馏塔精馏工艺要求的115℃;加压精馏塔再沸器⑨以18-25t/h的流量输出140℃以上的蒸汽冷凝液将预后甲醇由103℃加热到115℃后,再进入加压精馏塔⑤进行甲醇精馏;
(4)预精馏塔③底部并联一台预塔第二再沸器⑧,从预后加热器④以18-25t/h的流量排出的115℃蒸汽冷凝液进入预塔第二再沸器⑧,从而加热预精馏塔③塔底的物料,使预精馏塔③塔底的部分物料气化;
(5)最后,从预后加热器④送入常压精馏塔的甲醇温度不高于90℃。
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CN105536279A (zh) * 2015-12-21 2016-05-04 七台河宝泰隆煤化工股份有限公司 甲醇精馏装置
CN108704328A (zh) * 2018-06-01 2018-10-26 袁锟 一种新型快速蒸馏装置及其蒸馏方法
CN113087597A (zh) * 2021-03-22 2021-07-09 国家能源集团宁夏煤业有限责任公司 甲醇精馏的方法和甲醇精馏系统

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CN101693645A (zh) * 2009-10-14 2010-04-14 刘海峰 甲醇多塔精馏工艺及精馏设备

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CN105536279A (zh) * 2015-12-21 2016-05-04 七台河宝泰隆煤化工股份有限公司 甲醇精馏装置
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CN113087597A (zh) * 2021-03-22 2021-07-09 国家能源集团宁夏煤业有限责任公司 甲醇精馏的方法和甲醇精馏系统

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