CN110327849A - 一种变换触媒升温硫化系统 - Google Patents
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Abstract
本发明涉及变换触媒升温硫化技术领域,具体涉及一种变换触媒升温硫化系统,将变换硫化与拓普索工艺有机结合;本发明提供了一种变换触媒升温硫化系统,将变换硫化与拓普索工艺有机结合;燃烧炉出口物质一路进入变换炉用于硫化,硫化过程中无需补充氮气和引入新的热源,将燃烧炉0.1MPa、850℃烟气引入,减少了提压装置的使用,过程中无需引入热源,降低成本,延长设备使用寿命,另一路通过余热回收管路进入托普索制酸反应器用于二氧化硫转化;托普索制酸工艺中燃烧炉出口烟气引入,用于在升温过程中代替2.5MPa废锅加热气体,提高硫化温度,有效激活了变换触媒的活性,避免焊口开裂,保证系统长周期稳定运行,彻底解决2.5MPa废锅易泄漏和触媒硫化效果差的问题。
Description
技术领域
本发明涉及变换触媒升温硫化技术领域,更具体而言,涉及一种变换触媒升温硫化系统。
背景技术
变换触媒升温硫化操作分四个阶段,升温、硫化初期、硫化主期和降温期。罗茨机将50℃左右,含高浓度CS2的N2提压到45kPa左右,经2.5MPa废锅间接加热后送入变换炉,对变换触媒升温硫化。含CS2的N2走管程,430℃左右的过热蒸汽走壳程。该工艺在硫化过程中硫化氢对2.5MPa废锅腐蚀严重。用2.5MPa废锅作为加热源,变换炉的最高硫化温度只能达到320℃,未能达到硫化方案要求的硫化强化期380-400℃的要求,致使触媒硫化效果差,活性不好。废锅作用是管内的高温气加热管间的脱盐水,产生蒸汽,一台2.5MPa废锅100万元左右,有时维护不好只能用半年。硫化过程没有水参与,相当于干烧,设备寿命大打折扣。正常流程是管内压力高于管外压力,硫化时又是管外压力远高于管内压力,焊口很容易裂缝。硫化时需要单独开罗茨机提压,正常生产不用,增加了设备投资和维护成本,硫化时消耗电能。
发明内容
为了克服现有技术中所存在的不足,本发明提供一种变换触媒升温硫化系统,提高变换触媒升温硫化温度,保证触媒使用活性,实现系统废气废热资源化利用。
为了解决上述技术问题,本发明所采用的技术方案为:
一种变换触媒升温硫化系统,包括变换炉、水冷却器、气液分离器、燃烧炉、托普索制酸反应器和热能回收系统;所述燃烧炉出口一路进入变换炉用于变换触媒硫化反应,另一路通过余热回收管路进入热能回收系统用于回收热量;变换炉出口一路进入余热回收管路,另一路进入水冷却器;水冷却器出口进入气液分离器;气液分离器气相进入余热回收管路,液相排污;热能回收系统将余热回收管路与托普索制酸反应器中热量用于副产蒸汽;余热回收管路经热能回收系统换热后管内气体进入托普索制酸反应器;热能回收系统将热能回收用于副产蒸汽后用于其他工序。
进一步地,所述燃烧炉出口烟气温度为800-900℃、压力为0.05-0.2MPa。
进一步地,所述燃烧炉入口连接低温甲醇洗工段,在低温甲醇洗工段中吸收塔将H2S吸收,与低温甲醇形成含硫富甲醇,然后在含硫甲醇闪蒸罐中析出,经H2S浓缩塔得到34%H2S,进入燃烧炉。
进一步地,所述气液分离器气相出口H2S浓度低时,环保达标即可进入火炬线送至火炬,在火炬点火燃烧后进行排放;H2S浓度高时,通往余热回收管路循环使用。
与现有技术相比,本发明所具有的有益效果为:
本发明提供了一种变换触媒升温硫化系统,将变换硫化与拓普索工艺有机结合;燃烧炉出口物质一路进入变换炉用于硫化,硫化过程中无需补充氮气和引入新的热源,将燃烧炉0.1MPa、850℃烟气引入,减少了空分装置和罗茨机的使用,同时变换触媒硫化过程中无需引入新的热源,降低成本,减少关键设备的腐蚀,延长使用寿命,另一路通过余热回收管路进入托普索制酸反应器用于二氧化硫转化;托普索制酸工艺中燃烧炉出口烟气引入,用于在升温过程中代替2.5MPa废锅加热气体,提高硫化温度,有效激活了变换触媒的活性,保证了系统开车后的变换后CO指标,同时有效避免焊口开裂,减少停车检修的次数,保证系统的长周期稳定运行,彻底解决了2.5MPa废锅易泄漏和触媒硫化效果差的问题。
附图说明
图1为本发明提供的一种变换触媒升温硫化系统示意图。
图中:1为变换炉、2为水冷却器、3为气液分离器、4为燃烧炉、5为托普索制酸反应器、6为热能回收系统。
具体实施方式
下面将结合本发明实施例中的附图,对本发明实施例中的技术方案进行清楚、完整地描述,显然,所描述的实施例仅仅是本发明一部分实施例,而不是全部的实施例。基于本发明中的实施例,本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施例,都属于本发明保护的范围。
如图1所示,一种变换触媒升温硫化系统,包括变换炉1、水冷却器2、气液分离器3、燃烧炉4、托普索制酸反应器5和热能回收系统6;所述燃烧炉4出口一路进入变换炉1用于变换触媒硫化反应,另一路通过余热回收管路进入热能回收系统6用于回收热量;变换炉1出口一路进入余热回收管路,另一路进入水冷却器2;水冷却器2出口进入气液分离器3;气液分离器3气相进入余热回收管路,液相排污;热能回收系统6将余热回收管路与托普索制酸反应器5中热量用于副产蒸汽;余热回收管路经热能回收系统6换热后管内气体进入托普索制酸反应器5;热能回收系统6将热能回收用于副产蒸汽后用于其他工序。
进一步地,所述燃烧炉4出口烟气温度为800-900℃、压力为0.05-0.2MPa。
进一步地,所述燃烧炉4入口连接低温甲醇洗工段,在低温甲醇洗工段中吸收塔将H2S吸收,与低温甲醇形成含硫富甲醇,然后在含硫甲醇闪蒸罐中析出,经H2S浓缩塔得到34%H2S,进入燃烧炉4。
进一步地,所述气液分离器3气相出口H2S浓度低时,环保达标即可进入火炬线送至火炬,在火炬点火燃烧后进行排放;H2S浓度高时,通往余热回收管路循环使用。
在本实施例中,各反应器进出口物质为:
变换炉进口物质:
(1)流量:167269Nm3/h,其中CO:20.443%、H2:13.896%、CO2:11.766%、惰性气:0.059%、H2S:0.093%、COS:0.005%、H2O:53.5%
(2)压力:3.8Mpa
(3)温度:250℃
变换炉出口物质:
(1)流量:167269Nm3/h,其中CO:3.822%、H2:30.518%、CO2:28.387%、惰性气:0.059%、H2S:0.097%、COS:0.0007%、H2O:36.888%
(2)压力:3.67Mpa
(3)温度:412℃
燃烧炉进口物质:
(1)流量:酸性气651Nm3/h,其中CO2:56%、H2S:34%、N2:8%;空气:1874Nm3/h其中O2:21%、N2:79%;混合气:2525Nm3/h其中CO2:14.4%、H2S:8.7%、N2:60.6%、O2:15.5%
(2)压力:0.1Mpa
(3)温度:39℃
燃烧炉出口物质:
(1)流量:热工艺气2414Nm3/h,其中SO2:9.1%、CO2:15%、N2:63.5%、O2:2.5%、H2O:9.1%
(2)压力:0.1Mpa
(3)温度:850℃
托普索制酸反应器进口物质:
(1)流量:热工艺气2664Nm3/h,其中SO2:8.3%、CO2:13.6%、N2:64.9%、O2:4.3%、H2O:8.3%
(2)压力:0.1Mpa
(3)温度:420℃
托普索制酸反应器出口物质:
(1)流量:热工艺气2553Nm3/h,其中SO3:8.6%、CO2:14.2%、N2:67.7%、O2:0.1%、H2O:8.6%
(2)压力:0.1Mpa
(3)温度:383℃
上面仅对本发明的较佳实施例作了详细说明,但是本发明并不限于上述实施例,在本领域普通技术人员所具备的知识范围内,还可以在不脱离本发明宗旨的前提下作出各种变化,各种变化均应包含在本发明的保护范围之内。
Claims (4)
1.一种变换触媒升温硫化系统,其特征在于:包括变换炉(1)、水冷却器(2)、气液分离器(3)、燃烧炉(4)、托普索制酸反应器(5)和热能回收系统(6);所述燃烧炉(4)出口一路进入变换炉(1)用于变换触媒硫化反应,另一路通过余热回收管路进入热能回收系统(6)用于回收热量;变换炉(1)出口一路进入余热回收管路,另一路进入水冷却器(2);水冷却器(2)出口进入气液分离器(3);气液分离器(3)气相进入余热回收管路,液相排污;热能回收系统(6)将余热回收管路与托普索制酸反应器(5)中热量用于副产蒸汽;余热回收管路经热能回收系统(6)换热后管内气体进入托普索制酸反应器(5);热能回收系统(6)将热能回收用于副产蒸汽后用于其他工序。
2.根据权利要求1所述的一种变换触媒升温硫化系统,其特征在于:所述燃烧炉(4)出口烟气温度为800-900℃、压力为0.05-0.2MPa。
3.根据权利要求1或2所述的一种变换触媒升温硫化系统,其特征在于:所述燃烧炉(4)入口连接低温甲醇洗工段,在低温甲醇洗工段中吸收塔将H2S吸收,与低温甲醇形成含硫富甲醇,然后在含硫甲醇闪蒸罐中析出,经H2S浓缩塔得到34%H2S,进入燃烧炉(4)。
4.根据权利要求1所述的一种变换触媒升温硫化系统,其特征在于:所述气液分离器(3)气相出口H2S浓度低时,环保达标即可进入火炬线送至火炬,在火炬点火燃烧后进行排放;H2S浓度高时,通往余热回收管路循环使用。
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