CN211177620U - 一种pdh分离***联产燃料电池车用氢气装置 - Google Patents
一种pdh分离***联产燃料电池车用氢气装置 Download PDFInfo
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Abstract
本实用新型公开了一种PDH分离***联产燃料电池车用氢气装置。该装置包括一级冷却器、一级分离器、二级冷却器、二级分离器、高压膨胀机、高压膨胀机后汽液分离器、低压膨胀机、低压膨胀机后汽液分离器、液体产品闪蒸罐、液体产品泵、PSA***;该PDH分离***联产燃料电池车用氢气装置,将两个***巧妙结合起来,在得到PDH制丙烯的液体产品要求的同时,又利用PDH分离***经的富含氢气的干气产品,经过PSA***提纯得到高纯度的用于燃料电池的氢气。该装置同时为燃料电池车用氢气提供了原料来源,提高了工厂和产品的经济性。
Description
技术领域
本实用新型涉及一种PDH分离***联产燃料电池车用氢气装置,特别是巧妙结合PDH分离***和PSA***,既得到丙烯的液体产品,又利用富含氢气的干气产品得到用于燃料电池的氢气。
背景技术
一种PDH项目的冷箱低温分离***,它包括四台板翅式换热器、七台汽液分离器、二台膨胀机组和一台低温泵,第一板翅式换热器有一个热流通道和两个热流通道,其中第一进料连通热流通道,在该第一板翅式换热器复热后接出分离的第一产出物通道;第二板翅式换热器设置有两个热流通道和两个冷流通道;第三板翅式换热器设置一个热流通道和一个冷流通道;第四板翅式换热器设置一个热流通道和三个冷流通道;第四板翅式换热器的第一冷流通道出口与第一板翅式换热器的第二冷流到出口并接成为第二产出物通道;第一气液分离器、第二气液分离器、第三气液分离器、第四气液分离器、第六气液分离器各自分的液体出口通过节流阀门后并接于闪蒸罐,闪蒸罐上分别接出成为第三产出物通道和第四产出物通道;具有流程简易、产品回收率高、节能、易操作、经济性能优良特点等。
一种PDH项目的冷箱低温分离***,主要适用于催化工艺的TOH项目中对进料再细分的低温区域进行有效分离及能量回收。这种***有效利用分配的低温冷量使得各个板翅式换热器具有理想的换热性能,并通过膨胀机对外发电高效回收能量,节约整个项目的能耗。
一种可回收利用不合格氢气以及富余氢气的PSA制氢***。其包括制氢原料气进气管、氢气输出管、焦炉煤气压缩机、PSA制氢装置和氢气储罐;氢气储罐和PSA制氢装置之间设有放空管,放空管上由内向外依次设有第二自动阀和放空管,放空管与氢气储罐之间设有第一自动阀,第二自动阀和放空管之间连有氢气回收管,氢气回收管与制氢原料气进气管相连接,氢气回收管上设有回收阀。该***可以在当用户氢气用量减少,氢气储罐压力升高到设定压力或者制氢装置出现故障,生产出不合格的氢气时,将不合格氢气或者富余氢气通过氢气回收管进行回收再利用,从而有效杜绝了氢气排空到大气中,避免了能源浪费及环境污染。
当前技术背景没有将PDH分离***和PSA***创造性的结合,利用PDH分离的富氢干气产品经过PSA制氢***提取高纯度的氢气,作为燃料电池的氢气来源。
发明内容
本实用新型的目的是克服现有技术的不足,提供一种PDH分离***联产燃料电池车用氢气装置,特别是利用PDH分离的富氢干气产品经过PSA制氢***提取高纯度的氢气,作为燃料电池的氢气来源。
一种PDH分离***联产燃料电池车用氢气装置包括一级冷却器、一级分离器、二级冷却器、二级分离器、高压膨胀机、高压膨胀机后汽液分离器、低压膨胀机、低压膨胀机后汽液分离器、液体产品闪蒸罐、液体产品泵、PSA***;
新鲜原料流股经一级冷却器后分为流股a和流股b,其中流股a穿过二级冷却器并与低压膨胀机后汽液分离器产出的气相流股合流后穿过二级冷却器,穿出二级冷却器后与流股b合流穿过一级冷却器;
上游的反应产物流股穿过一级冷却器并与一级分离器的进料口相连,一级分离器的气相出料流股穿过二级冷却器并与二级分离器的进料口相连,二级分离器的气相流股穿过二级冷却器并分为两股,一股进入高压膨胀机,另一股作为干气产品部分或全部进入PSA***;高压膨胀机的出口与高压膨胀机后汽液分离器相连;高压膨胀机后汽液分离器的气相出料流股经二级冷却器后与低压膨胀机相连;低压膨胀机出口与低压膨胀机后汽液分离器相连,低压膨胀机后汽液分离器的气相流股与经二级冷却器冷却的原料流股合流;
一级分离器、二级分离器、高压膨胀机后汽液分离器、低压膨胀机后汽液分离器中的液相出料流股均与液体产品闪蒸罐相连,液体产品闪蒸罐的气相出料流股经过一级冷却器、二级冷却器复热成常温后也离开反应产物分离***。液体产品闪蒸罐的液体出料流股经过液体产品泵加压后进入一级冷却器复热成常温后离开反应产物分离***
作为本实用新型的优选方案,所述的低压膨胀机设有旁路,高压膨胀机后汽液分离器的气相出料流股经二级冷却器后可全部或部分经旁路直接与低压膨胀机后汽液分离器相连。
作为本实用新型的优选方案,所述的高压膨胀机设有旁路,二级分离器的气相流股一部分作为干气产品,另一部分穿过二级冷却器后可全部或部分经旁路直接进入高压膨胀机后汽液分离器。
本实用新型弥补了PDH分离***和PSA***工艺流程领域存在的不足,创造了制备燃料电池车用氢气的联产工艺装置。该PDH分离***联产燃料电池车用氢气装置,将两个***巧妙结合起来,在得到PDH制丙烯的液体产品要求的同时,又利用PDH分离***经的富含氢气的干气产品,经过PSA***提纯得到高纯度的用于燃料电池的氢气。因两个***匹配使用,使得经过低温分离***的粗氢气相比较杂质含量低,没有甲醛甲酸等对燃料氢电池有害的杂质,故省去了除杂质的工序,该干气氢产品纯度和杂质含量正好适用于制燃料电池车用氢气。该PDH分离***简化了流程的组织,减少了相关设备,提高了换热器的最小温差,减少换热夹点出现的几率,增强了装置的可操作性和适应性,并且能在较高膨胀机效率运行的同时降低***能耗。该联产装置在提高PDH项目富氢气的利用率的同时,为燃料电池车用氢气提供了原料来源,同时提高了工厂和产品的经济性。
附图说明
图1为本实用新型一种PDH分离***联产燃料电池车用氢气装置工艺流程;
图2为本实用新型一种PSA***工艺流程;
图中,一级冷却器E-101、一级分离器D-101、二级冷却器E-102、二级分离器D-102、高压膨胀机EXP-110、高压膨胀机后汽液分离器D-110、低压膨胀机EXP-120、低压膨胀机后汽液分离器D-120、液体产品闪蒸罐D-301、液体产品泵P-301A/B、PSA***。
具体实施方式
本实用新型的一种可具体实施的PDH分离***联产燃料电池车用氢气装置如图1和2所示,它包括一级冷却器E-101、一级分离器D-101、二级冷却器E-102、二级分离器D-102、高压膨胀机EXP-110、高压膨胀机后汽液分离器D-110、低压膨胀机EXP-120、低压膨胀机后汽液分离器D-120、液体产品闪蒸罐D-301、液体产品泵P-301A/B、PSA***;
新鲜原料流股F1经一级冷却器E-101后分为流股a和流股b,其中流股a穿过二级冷却器E-102并与低压膨胀机后汽液分离器D-120产出的气相流股合流后穿过二级冷却器E-102,穿出二级冷却器E-102后与流股b合流穿过一级冷却器E-101;
上游的反应产物流股F2穿过一级冷却器E-101并与一级分离器D-101的进料口相连,一级分离器D-101的气相出料流股穿过二级冷却器E-102并与二级分离器D-102的进料口相连,二级分离器D-102的气相流股穿过二级冷却器E-102并分为两股,一股进入高压膨胀机EXP-110,另一股作为干气产品进入部分或全部PSA***;高压膨胀机EXP-110的出口与高压膨胀机后汽液分离器D-110相连;高压膨胀机后汽液分离器D-110的气相出料流股经二级冷却器E-102后与低压膨胀机EXP-120相连;低压膨胀机EXP-120出口与低压膨胀机后汽液分离器D-120相连,低压膨胀机后汽液分离器D-120的气相流股与经二级冷却器E-102冷却的原料流股合流;
一级分离器D-101、二级分离器D-102、高压膨胀机后汽液分离器D-110、低压膨胀机后汽液分离器D-120中的液相出料流股均与液体产品闪蒸罐D-301相连,液体产品闪蒸罐D-301的气相出料流股经过一级冷却器E-101、二级冷却器E-102复热成常温后也离开反应产物分离***。液体产品闪蒸罐D-301的液体出料流股经过液体产品泵P-301A/B加压后进入一级冷却器E-101复热成常温后离开反应产物分离***
根据本实用新型的一个具体实施例,所述的一种PDH分离***联产燃料电池车用氢气装置,其特征在于所述的低压膨胀机EXP-120设有旁路,高压膨胀机后汽液分离器D-110的气相出料流股经二级冷却器E-102后可全部或部分经旁路直接与低压膨胀机后汽液分离器D-120相连。
根据本实用新型的一个具体实施例,所述的一种PDH分离***联产燃料电池车用氢气装置,其特征在于所述的高压膨胀机EXP-110设有旁路,二级分离器D-102的气相流股一部分作为干气产品,另一部分穿过二级冷却器E-102后可全部或部分经旁路直接进入高压膨胀机后汽液分离器D-110。
PSA***是一种新的气体分离技术,以吸附剂分子筛为例,其原理是利用分子筛对不同气体分子“吸附”性能的差异而将气体混合物分开;从富氢气流中回收或提纯氢,改变操作条件可生产不同纯度的氢气,氢气纯度可达99.99%。本实用新型弥补了PDH分离***和PSA***工艺流程领域存在的不足,创造了制备燃料电池车用氢气的联产工艺装置。该PDH分离***联产燃料电池车用氢气装置,将两个***巧妙结合起来,在得到PDH制丙烯的液体产品要求的同时,又利用PDH分离***经的富含氢气的干气产品,经过PSA***提纯得到高纯度的用于燃料电池的氢气。
本实用新型装置的联合处理流程如下:
1)新鲜原料和上游的反应产物在一级冷却器E-101中作为热流进行冷热量交换;
2)被一级冷却器E-101冷凝后的反应产物在一级分离器D-101中进行气相与液相分离;
3)一级冷却器E-101分离出来的气体和被一级冷却器E-101冷凝后的部分新鲜原料作为热流在二级冷却器E-102中进行冷热量交换;
4)一级冷却器E-101分离出来的气体被二级冷却器E-102冷凝后在二级分离器D-102中进行气相和液相分离;
5)二级冷却器E-102分离出来的气体在二级冷却器E-102中过热后,部分进入高压膨胀机EXP-110进行膨胀制冷;另一部分作为干气产品;
6)步骤5)膨胀后的物流进入高压膨胀机后汽液分离器D-110进行气液相分离,分离出来的气体在二级冷却器E-102中复热;
7)步骤6)复热后的气体出二级冷却器E-102,部分直接进入低压膨胀机后汽液分离器D-120,另一部分经低压膨胀机EXP-120中膨胀制冷后进入低压膨胀机后汽液分离器D-120;
8)低压膨胀机后汽液分离器D-120分离的气体与被二级冷却器E-102冷凝后的新鲜原料混合作为预混合的联合进料给二级冷却器E-102提供冷量;
9)预混合的联合进料出二级冷却器E-102后,与被一级冷却器E-101冷凝后的另一部分新鲜原料进入一级冷却器E-101中作为联合进料给一级冷却器E-101提供冷量,变成常温后出反应产物分离***;
10)富含氢气的干气产品依次经过二级冷却器E-102、一级冷却器E-101复热成常温气体出反应产物分离***;
11)一级分离器D-101、二级分离器D-102、高压膨胀机后汽液分离器D-110、低压膨胀机后汽液分离器D-120中的液体经过节流降压后进入液体产品闪蒸罐D-301,液体产品闪蒸罐D-301中的气体经过一级冷却器E-101复热成常温后也离开反应产物分离***;
12)液体产品闪蒸罐D-301中的液体经过液体产品泵P-301A/B加压后进入一级冷却器E-101复热成常温,作为液体产品离开反应产物分离***;
13)富含氢气的干气产品出反应产物分离***后,部分或全部进入PSA***依次经历吸附(A)、多级压力均衡降(EID)、顺放(PP)、逆放(D)、冲洗(P)、多级压力均衡升(EIR)、最终升压(FR)处理步骤进行氢气提纯作为用于燃料电池的氢气。
为了实现上述的工艺,以上所述实施例仅表达了本实用新型的几种实施方式,其描述较为具体和详细,但并不能因此而理解为对本实用新型专利范围的限制。应当指出的是,对于本领域的普通技术人员来说,在不脱离本实用新型构思的前提下,还可以做出若干变形和改进,这些都属于本实用新型的保护范围。因此,本实用新型专利的保护范围应以所附权利要求为准。
Claims (3)
1.一种PDH分离***联产燃料电池车用氢气装置,其特征在于包括一级冷却器(E-101)、一级分离器(D-101)、二级冷却器(E-102)、二级分离器(D-102)、高压膨胀机(EXP-110)、高压膨胀机后汽液分离器(D-110)、低压膨胀机(EXP-120)、低压膨胀机后汽液分离器(D-120)、液体产品闪蒸罐(D-301)、液体产品泵(P-301A/B)、PSA***;
新鲜原料流(F1)股经一级冷却器(E-101)后分为流股a和流股b,其中流股a穿过二级冷却器(E-102)并与低压膨胀机后汽液分离器(D-120)产出的气相流股合流后穿过二级冷却器(E-102),穿出二级冷却器(E-102)后与流股b合流穿过一级冷却器(E-101);
上游的反应产物流股(F2)穿过一级冷却器(E-101)并与一级分离器(D-101)的进料口相连,一级分离器(D-101)的气相出料流股穿过二级冷却器(E-102)并与二级分离器(D-102)的进料口相连,二级分离器(D-102)的气相流股穿过二级冷却器(E-102)并分为两股,一股进入高压膨胀机(EXP-110),另一股作为干气产品(F3)部分或全部进入PSA***;高压膨胀机(EXP-110)的出口与高压膨胀机后汽液分离器(D-110)相连;高压膨胀机后汽液分离器(D-110)的气相出料流股经二级冷却器(E-102)后与低压膨胀机(EXP-120)相连;低压膨胀机(EXP-120)出口与低压膨胀机后汽液分离器(D-120)相连,低压膨胀机后汽液分离器(D-120)的气相流股与经二级冷却器(E-102)冷却的原料流股合流;
一级分离器(D-101)、二级分离器(D-102)、高压膨胀机后汽液分离器(D-110)、低压膨胀机后汽液分离器(D-120)中产出的液相出料流股均与液体产品闪蒸罐(D-301)相连,液体产品闪蒸罐(D-301)的气相出料流股经过一级冷却器(E-101)、二级冷却器(E-102)复热成常温后离开反应产物分离***;液体产品闪蒸罐(D-301)的液体出料流股经过液体产品泵(P-301A/B)加压后进入一级冷却器(E-101)复热成常温后离开反应产物分离***。
2.根据权利要求1所述的一种PDH分离***联产燃料电池车用氢气装置,其特征在于所述的低压膨胀机(EXP-120)设有旁路,高压膨胀机后汽液分离器(D-110)的气相出料流股经二级冷却器(E-102)后可全部或部分经旁路直接与低压膨胀机后汽液分离器(D-120)相连。
3.根据权利要求1所述的一种PDH分离***联产燃料电池车用氢气装置,其特征在于所述的高压膨胀机(EXP-110)设有旁路,二级分离器(D-102)的气相流股一部分作为干气产品,另一部分穿过二级冷却器(E-102)后可全部或部分经旁路直接进入高压膨胀机后汽液分离器(D-110)。
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