CN105344293B - 加氢处理的硫化氢压缩方法及装置 - Google Patents

加氢处理的硫化氢压缩方法及装置 Download PDF

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CN105344293B
CN105344293B CN201510873452.5A CN201510873452A CN105344293B CN 105344293 B CN105344293 B CN 105344293B CN 201510873452 A CN201510873452 A CN 201510873452A CN 105344293 B CN105344293 B CN 105344293B
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王荣超
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Abstract

加氢处理的硫化氢压缩方法及装置，利用工厂富含硫化氢气体，通过新设置的隔膜式压缩机或往复式压缩机，并在压缩机不同位置配比不同比例的氢气，共同压缩到加氢处理的高压部分，以保持高压系统的硫化氢浓度。通过在新压缩机一级入口、和/或二级入口、和/或三级入口、和/或四级入口配入氢气，以避免硫化氢气体在压缩过程中液化。

Description

加氢处理的硫化氢压缩方法及装置
所属技术领域
本发明涉及加氢处理装置的硫化氢回收补硫，具体说，是通过向加氢处理装置反应系统压缩输送气体硫化氢，以保持反应系统循环氢中硫化氢含量在合理水平。
背景技术
加氢处理可包括：石油馏分的加氢精制、加氢裂化、加氢降凝等的加氢处理，也可包括煤焦油或煤、油共炼或煤直接液化等的固定床/悬浮床/沸腾床的加氢处理，即广义上的加氢脱硫、脱氧、脱氮、芳烃饱和、加氢裂化等一系列消耗氢气的催化加氢反应。
当加氢处理加工高氮低硫原料时，循环氢系统中的硫化氢浓度过低，钴、钼等金属的硫化态催化剂活性下降。如果保持一定加氢处理深度的话，操作上必须提温，这不仅会加速催化剂失活，也使催化剂的选择性变差，装置的经济效益下降。这种情况下，加氢处理的反应系统需要补硫。
传统的补硫方法是，向反应进料泵入口、或向反应系统加热炉出口注入硫化剂DMDS(二甲基二硫)，DMDS注入反应系统后，反应条件下即与氢气反应产生硫化氢。
纯净的硫化氢在标准状态下是气体。根据纯净硫化氢气体饱和蒸汽压计算公式IgP＝7.88-1080.64/T，可计算出不同温度下硫化氢的液化压力(表压)如下表：
专利CN103911176A介绍了一种补硫方案，是利用加氢处理所产的含硫化氢气体，通过压缩机直接输送到加氢处理反应系统的方法，也介绍了该含硫化氢气体压缩到补充氢压缩机入口，并借助补充氢压缩机输送到加氢处理反应系统的方法。
上述方案的两个方法各存在一个限制因素。直接输送到反应系统，加氢处理的反应压力较低(如汽柴油加氢)没有问题，当反应压力高于9Mpa后，硫化氢气体在末级压缩时进入超临界状态，压缩机无法输送接近液体密度的超临界气体(如果冷却，该气体将立即液化为液体，而压缩机无法输送液体的)；借助补充氢压缩机输送，如果在加氢处理装置设计、建设之初，补充氢压缩机考虑含硫化氢因素的话是没有问题，但如果对现有加氢装置实施该补硫方案，硫化氢气体对补充氢压缩机仍有少量腐蚀、气体密度增大影响现有压缩机功率等不利影响。
本方法提供一种不影响现有加氢处理设施的压缩硫化氢补硫方案。
发明内容
为了通过压缩方式回收硫化氢气体，弥补加氢处理反应系统的硫缺失，而不影响加氢处理装置现有新氢压缩机的运行，本方法新设置一台压缩机，可以是隔膜式压缩机，也可以是往复式活塞压缩机。并在该新增的压缩机一级入口、和/或二级入口、和/或三级入口、和/或四级入口、和/或五级入口配比一定流量的含氢气体。即该新增的压缩机，将含硫化氢气体和工厂氢气一起压缩到加氢处理的反应系统。
硫化氢是可以被液化的气体，当其压力越高、温度越低时，越容易发生液化现象。当逐步对含硫化氢气体增压时，硫化氢越容易被液化。为保证硫化氢的压缩输送，特引入工厂氢气对含硫化氢气体进行配比和稀释，以降低硫化氢分压。
参照硫化氢液化温度-压力表，比如硫化氢在3.5Mpa、39.1℃下达到气液平衡。现在要将硫化氢输送到20Mpa的加氢处理系统中，只要引入氢气比例，使硫化氢分压始终在3.5Mpa以下，就不会在压缩过程中出现液体。显而易见，补充的氢气弥补20-3.5＝16.5Mpa的压力，即：配比16.5/3.5＝4，714倍以上硫化氢体积流量的氢气物流，在后续的压缩及冷却过程中不会造成硫化氢的液化，即可以顺利输送到加氢系统中。
根据工厂的含硫化氢气体压力条件，和加氢处理反应压力条件，很容易计算出需要新设置压缩机的工况参数。输送气体选择压缩机，可以设置一台单级压缩机，或多台单级压缩机串联，也可以设置一台多级压缩机。考虑到该工况压比很大，宜选择往复式活塞压缩机，更优选压比更大、泄漏率更低的隔膜式压缩机。
配入氢气的位置，根据硫化氢饱和蒸汽压计算式，将氢气配入到可能发生液化的该级入口。氢气的引入，降低了硫化氢分压，则硫化氢将不会液化，将与氢气成混合气体，送往加氢处理的反应系统。因为硫化氢气体是逐步增压的，因此发生液化的可能性越来越大，因此常常前一级补充了配比氢气后，后一级仍需进一步配比氢气。比较经济的做法是对每级的液化可能性进行核算以确定补入氢气量，因此当设置往复式活塞压缩机输送硫化氢气体时，可能存在对每级入口均需配气的情况。但更简单的方法是，核算硫化氢最可能的液化点，统一在压缩机的入口配比氢气，这样整个压缩机系统有相同的气体组成和气体流量，压缩机工作比较平稳。
氢气本身是加氢处理所需的一种原料，压缩氢气并不会对现有加氢处理设施有不利影响。氢气引入到新增的压缩机系统，降低了压缩机单纯输送气体硫化氢的浓度和分压，在系统发生泄漏时对装置人员危害性较小。另一方面，引入一定比例的氢气，可保证硫化氢气体压缩输送期间因分压降低而不发生液化，即可避免压缩机带液爆缸而无法输送的问题。配比用氢气可来源于工厂富氢气体，或PSA净化后的高纯氢气。当向新增的压缩机系统末级入口补充氢气时，受限于PSA氢气的压力较低，不妨从现有新氢压缩机的一级、二级或三级出口引入。
为避免含氧化物气体在加氢处理系统发生加氢强放热反应，需限定含硫化氢气体的杂质含量，其中氧气、一氧化碳、二氧化碳总含量，低于硫化氢体积浓度的5％，即低于5v％ H2S。
可以新设置一台压缩装置，根据工厂条件，满足加氢处理的硫化氢压缩回收所用。将工厂含氢气体管路与含硫化氢气体管路相连，含硫化氢气体管路再与一缓冲罐或混合器相连，实现氢气与硫化氢气体的充分混合。该缓冲罐或混合器再与压缩设备相连，压缩设备与加氢处理的高压系统相连。该压缩设备可以是一级、两级或三级隔膜式压缩机，或者是两级、三级、四级或五级往复式活塞压缩机。根据降低投资和减少有毒气体泄漏考虑，优选隔膜式压缩机，两级压缩。
可以在压缩机的级间配比一定流量的氢气。该配比级的级间压力由该引入的氢气流量控制，而含硫化氢气体流量与该配比氢气流量比值控制，该比值保证含硫化氢气体压缩过程中因分压过低而不会液化。
为简化设计与操作，优选在压缩机入口配比氢气，以保持各级压缩气体的组分和流量稳定。
针对上述优选工况，为准确投用该压缩装置，需平稳控制其入口压力。现设定压缩机入口压力与配比氢气串级控制，配比氢气流量与需压缩含硫化氢气体流量比值控制。比值由压缩过程中硫化氢不发生液化的氢气配比来定(详见实施例)。比如，当压缩机入口压力下降，压力控制器作用配氢流量控制阀，令其开大，氢气流量上升，通过比例作用到硫化氢流量控制阀，使硫化氢流量按比例增大。有更多氢气和硫化氢进入压缩机入口，使压缩机入口压力升高。
对于低硫高氮原料的加氢处理，一般需要补充1-6Nm3 H2S/吨原料，但加氢处理需要的氢气则达100-1000Nm3 H2/吨原料，因此压缩硫化氢时配入的氢气，远低于新氢压缩机所输送的氢气，因此这种额外的氢气补充，不足以影响现有反应压力控制系统的工作。
本方法的有益效果是：
1、本方法解决了加氢处理装置含硫化氢气体压缩机压缩期间可能液化而不能输送的问题。
2、本方法在实现硫化氢压缩的同时，避免了对现有新氢压缩机的腐蚀和气体组分与工况改变。
附图说明
图1是在新增压缩机一级入口补入氢气的硫化氢压缩流程图。
在图1中，根据工厂条件确定硫化氢输送的工况，进而确定氢气流量控制回路与硫化氢流量控制回路的比值，混合气体经过压缩机系统输送到加氢处理的高压部分。
图2是在新压缩机其他级入口补入氢气的流程图。
在图2中，根据工厂条件，将配比氢气补充到硫化氢压缩机的某级入口，该压缩机先单纯压缩硫化氢，再混合压缩硫化氢+氢气，至加氢处理的高压部分。
具体实施方式
实施例1将0.2Mpa含硫化氢气体加压到20Mpa。
方案一选用隔膜式压缩机，按两级压缩配置。计算每级压比为10，二级入口压力定为0.2*10＝2Mpa。根据硫化氢饱和蒸汽压计算式，二级入口压力下液化温度为18.7℃，低于工厂循环水冷却温度(40℃)，因此一级压缩直到二级入口期间不会液化。现对二级压缩进行配氢计算：
二级出口通常冷却到常温40℃输送，根据硫化氢饱和蒸汽压计算式，其液化分压为3.6Mpa，那所需配比的氢气为20-3.6＝16.4Mpa，配比为16.4/3.6＝4.56。
即用隔膜式压缩机两级压缩输送指定工况下含硫化氢气体，只要在二级入口配比不低于硫化氢体积流量4.56倍氢气，压缩过程将不会出现液化现象，即可用压缩机完成输送任务。
方案二选用往复式压缩机，按四级压缩配置。计算每级压比为3.16，二级入口压力0.632Mpa，三级入口压力2.0Mpa，四级入口压力6.32Mpa。按每级入口均冷却到40℃计算，四级入口出现液化现象。按压缩机出口气体冷却到常温输送进行计算，配氢比例同上，仍为4.56。
即用往复式压缩机四级压缩输送该工况下含硫化氢气体，只需在四级入口配比不低于硫化氢体积流量4.56倍氢气，冷却后液化的硫化氢即气化，且四级压缩及输送过程也不会出现液化现象。
实施例2将0.5Mpa含硫化氢气体加压到32Mpa。
方案一选隔膜式压缩机，按两级压缩配置。计算每级压比为8，二级入口压力定为4Mpa。根据硫化氢饱和蒸汽压计算式，二级液化温度为44.4℃，高于工厂循环水冷却温度(40℃)，因此一级压缩再冷却后会液化。因此需在一级入口进行配氢。配氢比计算如下：
一级入口配氢最小比例为：根据硫化氢饱和蒸汽压计算式，40℃时硫化氢于3.6Mpa压力下液化，因此配比氢气至少0.4Mpa，即至少配氢10％才能保证一级出口不液化。
二级出口要压缩至32Mpa，其中硫化氢分压不超过3.6Mpa，那二级入口需继续配氢，累计配比的氢气为32-3.6＝28.4Mpa，二级出口H2/H2S比为28.4/3.6＝7.89。
为简化计算、操作和压缩机设计，简化为在一级入口配氢，配氢比不低于7.89，隔膜式压缩机两级压缩均不会出现液化现象，压缩机可完成输送任务。
方案二选往复式压缩机，按四级压缩配置。计算每级压比为2.828，二级入口压力1.414Mpa，三级入口压力4.0Mpa，四级入口压力11.32Mpa。按每级入口均冷却到40℃计算，三级入口出现液化现象。按压缩机出口气体冷却到常温输送进行计算，配氢比例(32-3.6)/3.6＝7.89。即在三级入口配7.89倍以上的氢气，可保持三级、四级压缩及冷却过程不会出现液化现象。

Claims (7)

1.加氢处理的硫化氢压缩方法，将含硫化氢气体输送到反应系统，保持循环氢中硫化氢浓度，其特征是：将含氢气体按比例配入含硫化氢气体中，再压缩输送到反应系统；配入含氢气体的比例，使整个压缩工况下硫化氢分压，低于纯硫化氢气体液化的压力。
2.如权利要求1所述的压缩方法，其特征是：所述压缩，借助于单台单级压缩机，或者是多台单级压缩机串联，或者是单台多级式压缩机。
3.如权利要求1所述的压缩方法，其特征是：配入含氢气体的位置，是单级压缩机的入口，或者是多级压缩机的部分级入口，或全部级入口。
4.如权利要求1所述的压缩方法，其特征是：所述含氢气体，来源于工厂富氢气体，或PSA净化后的高纯氢气，或现有新氢压缩机的一级、二级或三级出口氢气。
5.如权利要求1所述的压缩方法，其特征是：所述含硫化氢气体，限定其中的氧气、一氧化碳、二氧化碳的全部浓度，低于硫化氢浓度5v％。
6.加氢处理的硫化氢压缩装置，其特征是：含氢气体管路与含硫化氢气体管路相连，含硫化氢气体管路与一缓冲罐或混合器相连，该缓冲罐或混合器与压缩设备相连，压缩设备与加氢处理的高压系统相连；含氢气体用于控制压缩设备入口压力，含硫化氢气体与含氢气体按比值控制，该比值使整个压缩工况下硫化氢分压，低于纯硫化氢气体液化的压力。
7.如权利要求6所述的压缩装置，其特征是：该压缩设备是一级、二级或三级隔膜式压缩机，或者是两级、三级、四级或五级往复式活塞压缩机；该压缩设备的不同级间，继续连接含氢气体管路。
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1087933A (zh) * 1993-12-27 1994-06-15 中国石化洛阳石油化工工程公司 加氢处理过程用补硫剂
CN102899071A (zh) * 2012-10-08 2013-01-30 西北大学 一种煤焦油加氢工艺方法
CN103361111A (zh) * 2012-04-04 2013-10-23 中国石油化工股份有限公司 一种汽油加氢处理工艺的催化剂硫化方法
CN103911176A (zh) * 2013-08-26 2014-07-09 王生友 油品加氢装置的补硫工艺

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1087933A (zh) * 1993-12-27 1994-06-15 中国石化洛阳石油化工工程公司 加氢处理过程用补硫剂
CN103361111A (zh) * 2012-04-04 2013-10-23 中国石油化工股份有限公司 一种汽油加氢处理工艺的催化剂硫化方法
CN102899071A (zh) * 2012-10-08 2013-01-30 西北大学 一种煤焦油加氢工艺方法
CN103911176A (zh) * 2013-08-26 2014-07-09 王生友 油品加氢装置的补硫工艺

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