CN116592574B - 一种回收膨胀功的液氢运输船再液化*** - Google Patents
一种回收膨胀功的液氢运输船再液化*** Download PDFInfo
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- CN116592574B CN116592574B CN202310848549.5A CN202310848549A CN116592574B CN 116592574 B CN116592574 B CN 116592574B CN 202310848549 A CN202310848549 A CN 202310848549A CN 116592574 B CN116592574 B CN 116592574B
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- 239000001257 hydrogen Substances 0.000 title claims abstract description 163
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 163
- 239000007788 liquid Substances 0.000 title claims abstract description 66
- 125000004435 hydrogen atom Chemical class [H]* 0.000 title claims abstract description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 147
- 239000007789 gas Substances 0.000 claims abstract description 56
- 238000007906 compression Methods 0.000 claims abstract description 38
- 230000006835 compression Effects 0.000 claims abstract description 37
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 30
- 238000010992 reflux Methods 0.000 claims abstract description 26
- 238000001816 cooling Methods 0.000 claims abstract description 17
- 239000002994 raw material Substances 0.000 claims description 18
- 239000012071 phase Substances 0.000 claims description 14
- 239000003054 catalyst Substances 0.000 claims description 13
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 239000012535 impurity Substances 0.000 claims description 7
- 238000013461 design Methods 0.000 claims description 5
- 239000007791 liquid phase Substances 0.000 claims description 4
- 239000003507 refrigerant Substances 0.000 claims description 3
- 230000006837 decompression Effects 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 12
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 239000000047 product Substances 0.000 description 11
- 238000001704 evaporation Methods 0.000 description 6
- 230000008020 evaporation Effects 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 229910052751 metal Inorganic materials 0.000 description 4
- 239000002184 metal Substances 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 239000013589 supplement Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 229910052763 palladium Inorganic materials 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 230000003068 static effect Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000013526 supercooled liquid Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Abstract
本发明提供一种回收膨胀功的液氢运输船再液化***,包含:预冷单元,氢液化单元,循环单元;预冷单元包含第一换热器;氢液化单元包含第二换热器、气液分离器,过冷器;气液分离器与过冷器形成第一、第二返流流股;循环单元包含至少1台压缩机组和若干膨胀机,其选用气体轴承膨胀机,气源为氢气,由压缩机组提供;膨胀机均包含压缩端,其利用膨胀机的膨胀功给气体加压;第一返流流股从第二换热器流经膨胀机的压缩端后,通向压缩机组,并形成循环氢气流股。本发明利用氢膨胀冷却为氢气提供冷量,并且再用气氢去回收膨胀过程中产生的轴功对气氢进行压缩,在回收压缩功的同时还减少了***的压缩机的用量及体积,可以减少5%‑10%的压缩能耗。
Description
技术领域
本发明属于液氢运输领域,尤其涉及一种回收膨胀功的液氢运输船再液化***。
背景技术
氢的化学能是通过氢气和氧气反应所产生的能量,不依赖于化石燃料,主要以化合态形式存在,是一种来源丰富、绿色低碳、应用广泛的二次能源,是未来国家能源体系的重要组成部分,能够帮助可再生能源大规模消纳,实现电网大规模调峰和跨季节、跨地域储能,加速推进工业、建筑、交通等领域的低碳化。
目前,氢储存方式主要有高压气态储存和低温液态储存这两种方式,高压气态储存是最普遍和最直接的储氢方式,但是该方式的氢储存量小,且需要厚重的耐压储罐,运输成本非常高。而低温液态储存技术目前还不成熟,一直以来,许多研究者围绕着提高氢的液化效率和降低液化费用开展了大量的理论和实验研究。
而在液氢运输船上,由于液氢本身极易蒸发,因此也需要通过氢液化技术,对液氢进行补充。由于目前氢液化技术存在的主要问题仍然是液化效率低、投资大、能耗高。因此,提升液化效率和能量利用效率是一个亟待解决的问题。
氢液化普遍包含膨胀步骤,目前来看,在氢液化***中,涉及膨胀功回收的***非常少。而且膨胀机大多使用油轴承,回收膨胀功时会污染返流氢气,若返流氢气中含油过多,则油可能在循环氢气中凝固,导致堵塞换热器通道。如果需要把油除去,会增加***运行成本,不够经济。
发明内容
为解决上述技术问题,本发明提供了一种回收膨胀功的液氢运输船再液化***,以降低氢液化过程中的能耗,提升氢液化效率,并且消除回收膨胀功时对氢气产生的污染。
本发明提供了一种回收膨胀功的液氢运输船再液化***,包含:预冷单元,氢液化单元,循环单元;
所述预冷单元包含第一换热器,用于给原料氢流股预冷;
所述氢液化单元包含第二换热器、气液分离器;所述原料氢流股离开所述预冷单元,经过所述第二换热器形成气液两相后,到达所述气液分离器,其中气相记为第一返流流股,作为冷流股回流到第二换热器;而液相通往产品收集容器;
所述循环单元包含至少1台压缩机组和若干膨胀机;所述膨胀机均包含压缩端,其利用所述膨胀机的膨胀功给气体加压;所述膨胀机选用气体轴承膨胀机;轴承气为氢气,由所述压缩机组或所述膨胀机压缩端的氢气分出一股提供;所述轴承气在进入轴承前,先通过一减压阀减压至0.6~0.8MPa;所述膨胀机包含第一膨胀机和第二膨胀机,所述第一、第二膨胀机数量均为0~4台;所述第一返流流股从所述第二换热器流经所述第一膨胀机的压缩端后,及所述第二返流流股从所述第二换热器流经所述第二膨胀机的压缩端后,均通向所述压缩机组且合并,合并后的流股记为循环氢气流股;
所述循环氢气流股通过所述第一换热器预冷后分为膨胀流股和补充流股,所述补充流股经过所述第二换热器后,到达所述气液分离器;
所述膨胀流股经过所述第二换热器、以及所述膨胀机的膨胀端降温降压后,又作为冷流股依次流向所述第二换热器、第一换热器,最终回到所述压缩机组且并入所述循环氢气流股。
较佳地,所述氢液化单元还设有第一J-T阀、第二J-T阀;若干所述原料氢流股经过所述第二换热器后,还经过所述第一J-T阀降温降压,形成气液两相;所述补充流股,经过所述第二换热器后,还经过所述第二J-T阀降温降压,形成气液两相。
较佳地,所述第二换热器的原料氢通道内设有正仲氢催化剂,所述正仲氢催化剂用于对所述原料氢进行连续的正仲转化。
较佳地,所述第二返流流股从第二换热器流出后,作为冷流股经过所述第一换热器,再依次流经所述第二膨胀机的压缩端。
较佳地,所述压缩机组仅包含一台压缩机组,所述第二返流流股、第一返流流股、膨胀流股汇合形成所述循环氢气流股后,再进入所述压缩机组压缩。
较佳地,所述第一返流流股从第二换热器流出后,作为冷流股经过所述第一换热器后,再依次流经所述第一膨胀机的压缩端。
较佳地,所述膨胀流股交替经过所述第二换热器和膨胀机。
较佳地,所述预冷单元还包含第一净化器和正仲氢转化器;原料氢流股经过所述第一换热器预冷;然后依次经过所述第一净化器和正仲氢转化器,转化到正仲氢含量处于平衡态后,再次经过第一换热器,冷却至冷剂设计温区。
进一步地,还设有第二净化器,所述循环氢气流股通过所述第二净化器除去杂质,所述第一净化器和第二净化器用于吸附杂质气体。
较佳地,所述循环单元还包含第三换热器,用于给压缩机内的气体降温。
较佳地,所述膨胀机的数量为2-5台。
较佳地,所述氢液化***包含控制装置,所述第一换热器、第二换热器、正仲氢转化器中均分别设置有温度传感器、压力传感器和流量传感器并且与所述控制装置相连接。
较佳地,所述正仲氢催化剂选用金属催化剂或磁性催化剂,所述金属催化剂为铁、铂、镍、钯中的一种。
与现有技术相比,本发明提供的回收膨胀功的液氢运输船再液化***的有益效果包含:
(1)本发明利用氢膨胀冷却为氢气提供冷量,并且再用气氢去回收膨胀过程中产生的膨胀功对气氢进行压缩,在回收膨胀功的同时还减少了***的压缩机的用量及体积,在使用本***之后可以减少5%-10%的压缩能耗。
(2)本发明使用气体轴承膨胀机,轴承气为氢气,相比起油轴承,膨胀功回收过程避免了氢液化***受到污染,也无需承担除油所需的成本。
(3)本发明通过设置过冷器,减少了液氢的闪蒸,使液氢蒸发损失小,安全隐患小。
(4)理想情况下,通过对膨胀机参数的设计,所述第一返流流股和第二返流流股离开所述膨胀机的压缩端后,其压力均与离开第一换热器的膨胀流股相同。此时只需要一台压缩机组来加压。减少了压缩机数量,节约用地约20%,节约了***的成本。
(5)所述第二返流流股和第一返流流股从第二换热器流出后,作为冷流股经过所述第一换热器后,再依次流经所述膨胀机的压缩端,充分利用了这两个流股的冷能,减少冷量浪费。
(6)本发明可用于液氢运输船的再液化,也可用于陆地上的氢液化过程。
附图说明
图1是本发明提供的一种回收膨胀功的液氢运输船再液化***理想设计情况下的示意图;
图2是本发明提供的一种回收膨胀功的液氢运输船再液化***一般设计情况下的示意图。
附图标记:
11-第一净化器;12-正仲氢转化器;13-第一换热器;14-第二净化器;
21-第二换热器;22-第一J-T阀;23-气液分离器;24-过冷器;25-第三J-T阀;26-第二J-T阀;
31-第一膨胀机;32-第二膨胀机;33-三通阀;34-减压阀;41-压缩机;42-第三换热器。
具体实施方式
下面将结合附图对本发明的技术方案进行清楚、完整地描述,显然,所描述的实施例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。
在本发明的描述中,需要说明的是,除非另有明确的规定和限定,术语“安装”、“相连”、“连接”应做广义理解,例如,可以是固定连接,也可以是可拆卸连接,或一体地连接;可以是机械连接;可以是直接相连,也可以通过中间媒介间接相连,可以是两个元件内部的连通。对于本领域的普通技术人员而言,可以具体情况理解上述术语在本发明中的具体含义。
此外,术语“第一”、“第二”仅用于描述目的,并非是指对时间顺序、数量、或者重要性的限定,不能理解为指示或暗示相对重要性或者隐含指明所指示的技术特征的数量,而仅仅是为了将本技术方案中的一个技术特征与另一个技术特征相区分。由此,限定有“第一”、“第二”的特征可以明示或隐含地包括一个或多个该特征。
除非清楚地指出相斥的,这里限定的每个方面或实施方案可以与任何其他一个或多个方面或一个或多个实施方案组合。特别地,任何指出的作为优选的或有利的特征可以与任何其他指出的作为优选的或有利的特征组合。
本发明提供了一种回收膨胀功的液氢运输船再液化***,如图1、图2所示,其包含预冷单元、氢液化单元、循环单元;一些实施例中,所述预冷单元包含第一换热器13、第一净化器11和正仲氢转化器12;原料氢流股经过所述第一换热器13预冷;然后依次经过所述第一净化器11和正仲氢转化器12,第一净化器11用于除去原料氢中的杂质气体,正仲氢转化器12用于正仲转化,正仲氢含量转化到当前温度下的平衡态后,再次经过第一换热器13,冷却至冷剂设计温区;
一些实施例中,所述氢液化单元包含第二换热器21、第一J-T阀22、气液分离器23、过冷器24、第二J-T阀26、第三J-T阀25;所述原料氢流股在离开所述预冷单元后,依次经过所述第二换热器21、第一J-T阀22和气液分离器23;所述第二换热器21的原料氢通道内设有正仲氢催化剂,使原料氢冷却到30K±10K的同时,还进行连续的正仲转化,转化至仲氢含量≥95%;所述原料氢经过所述第一J-T阀22后分为气液两相,并在所述气液分离器23中分离;气相作为冷流股回流到第二换热器21;液相进入过冷器24冷却到18K±5K后,分流为产品流股和第二返流流股;所述产品流股通往产品收集容器,第二返流流股经过所述第三J-T阀25后,作为冷流股依次回流至所述过冷器24和第二换热器21,并蒸发形成第二返流流股;
一些实施例中,所述循环单元包含1-3台压缩机组41和至少一台第三换热器42,还设有若干膨胀机,包含第一膨胀机31和第二膨胀机32,根据氢液化过程的实际需要,所述第一膨胀机31和第二膨胀机32的数量均为0-4,膨胀机总和为2-5台;所述膨胀机均包含压缩端;所述压缩端能利用膨胀端进行气体膨胀时产生的膨胀功,对压缩端的气体进行压缩。所述膨胀机选取气体轴承膨胀机,轴承气为氢气,由所述压缩机组或所述膨胀机压缩端的氢气通过三通阀33分出一股提供;所述轴承气在进入轴承前,先通过一减压阀34减压至0.6~0.8MPa,使轴承气的压力符合要求;以氢气为轴承气,不会对氢液化***造成污染,无需考虑除油等事项,可选用动压气体轴承或静压气体轴承。
所述第二返流流股从第二换热器21流经所述全部第二膨胀机32的压缩端,及所述第一返流流股从第二换热器21流经所述全部第一膨胀机31的压缩端,利用所述膨胀功进行初步压缩后,均通向所述压缩机组41和第三换热器42并汇合,汇合后的流股记为循环氢气流股;进一步地,所述第二返流流股和第一返流流股从第二换热器21流出后,先进入第一换热器13加热,再进入对应的膨胀机压缩端。进一步地,本发明的氢液化***还设有第二净化器14,所述循环氢气流股通过所述第二净化器除去杂质,所述第一净化器11和第二净化器14内均设有分子筛或活性炭等吸附剂,用于吸附杂质气体。
所述循环氢气流股通过所述第一换热器13预冷后分为膨胀流股和补充流股,所述补充流股依次经过所述第二换热器21和第二J-T阀26后,到达所述气液分离器23;然后经过气液分离器23进行分离以补充产品液氢,以保持产品液氢和原料氢气量的平衡。
所述膨胀流股经过所述第二换热器21和第一膨胀机31和第二膨胀机32的膨胀端降温降压后,又作为冷流股依次流向所述第二换热器21、第一换热器13,最终回到压缩机组,形成膨胀-压缩的循环。
在比较理想的情况下,如图1所示,通过对膨胀机参数的设计,所述第一返流流股和第二返流流股离开所述膨胀机的压缩端后,其压力均与离开第一换热器13的膨胀流股相同。此时只需要一台压缩机组来加压。减少了压缩机数量,节约了***的成本。而在一般情况下,如图2所示,也可以通过设计,使得所述第一返流流股或第二返流流股与膨胀流股压力相同,可以在进入所述压缩机组前汇合,也可以减少一台压缩机组的使用。
具体的工艺步骤可参考如下实施例。
实施例
本实施例设计的是一个产量10吨/日的氢液化***,如图1所示,一种回收膨胀功的液氢运输船再液化***,其氢气液化工艺步骤包含:
S1:通过第一换热器13对原料氢气预冷、净化;采用液氮预冷,预冷后氢气的温度在90K±10K;预冷后的气氢通过第一净化器11将气氢中氧含量降到0.1ppm以下;净化后的氢气通过正仲氢转化器12,将其中的正氢部分转化为仲氢,转化后正仲氢的含量大致处于90K的平衡态;由于正仲转化,导致气氢温度升高,所以将转化后的气氢再次通过第一换热器13进行预冷,使气氢达到液氮预冷的最低温度;
S2:预冷后的气氢进入第二换热器21,换热器的原料氢通道中装有正仲氢催化剂;第二换热器21对气氢进行冷却的同时还会对其进行连续的正仲转化,直到温度达到30K±10K;冷却后的气氢通过第一J-T阀22节流降压,得到气液两相氢,然后到达气液分离器23,分离后的气相形成第一返流流股,回流到第二换热器21;液氢进入过冷器24,作为热流股被冷却到18K±5k,其目的是为了使生成的液氢减少闪蒸现象,降低蒸发损失和安全隐患。过冷后的液氢分流为产品流股和第二返流流股;大部分的液氢通过产品流股进入液氢储罐,小部分的液氢进入第二返流流股,通过第三J-T阀25进一步降压,降压后得到气液两相氢作为冷流股进入过冷器24,其中,液相在过冷器24中蒸发后,作为冷流股回流到第二换热器21,蒸发过程为过冷器24提供冷量;
S3:气液分离器23分离后的气氢在先后通过第二换热器21和第一换热器13充分利用完其中的冷量后,第一膨胀机31的压缩端充分利用其膨胀端的膨胀功对其进行压缩;第二返流流股在通过第二换热器21充分利用其冷量后进入第二膨胀机32的压缩端,充分利用其膨胀端的膨胀功对其进行压缩,之后,第一、第二返流流股与所述膨胀流股混合后进入压缩机组41进行压缩,压缩到6.5MPa(A)±1.5MPa;
S4:通过压缩机组41压缩的气氢先通过第一换热器13进行预冷;预冷后的气氢分为所述膨胀流股和补充流股,所述补充流股通过第二换热器21冷却至30K±10K后,通过第二J-T阀26节流降压,得到气液两相氢,然后通过气液分离器23进行分离以补充产品液氢,保持产品液氢和原料氢气量的平衡;所述膨胀流股分别通过第二换热器21、第二膨胀机32、第二换热器21、第一膨胀机31连续降温到30K±10K后,回到第二换热器21为所有的热流股提供冷量;最后经过第一换热器13充分利用其冷量后进入压缩机组41,并在进入压缩机组41前,与所述第一、第二返流流股汇合,形成所述循环氢气流股。
本实施例中,所述的第一净化器11内放置了高效的分子筛,可以有效的分离出氢气中的氧气使其含量低于0.1ppm。
本实施例中,所述的第一换热器13和第二换热器21为高效的多流股换热器,可以将所有流股都集成在一个换热器中,与传统的工艺相比,减小了换热器的数量,减少了换热器与换热器之间的管路连接,减少了换热器和外接换热产生的能量损失,减少了冷箱的体积,减小了冷箱抽真空的体量,大大减小了真空泵的能耗。
本实施例中,所述的压缩机组41选用高效无油全平衡压缩机,与传统有油压缩机相比可以减少后端的油过滤器的使用,减少了通过油过滤器的压损,全平衡压缩机的使用减少了压缩机的占地面积,也减少了压缩机的使用台数。
本实施例中,所述的催化精制采用的催化剂为金属催化剂,金属催化剂为铁、铂、镍、钯中的一种,也可以使用磁性催化剂。
本实施例中,所述的第二膨胀机32、第一膨胀机31选用的是高效的气体轴承膨胀机,可以使用动压气体轴承也可使用静压气体轴承,轴承气为氢气,可以降低对膨胀机轴承密封的要求;轴承气由所述第一膨胀机31的压缩端提供,所述第一膨胀机31的压缩端通过三通阀33分出一股氢气后,通过减压阀34降压,然后通入所述气体轴承。第二返流流股和第一返流流股分别通过第二膨胀机32、第一膨胀机31的压缩端后充分利用了其的轴功,减少了***的压缩机需求量以及减少了整个***的压缩能耗。
本实施例中,对第一净化器11、正仲氢转化器12产生的气态氢,以及产品液氢进行连续抽样分析,分析仪采用色谱仪。
本实施例中,所述第三换热器42对所述压缩机组41进行水冷或空冷散热。
本实施例中,所述氢液化***包含控制装置,所述第一换热器13、第二换热器21和正仲氢转化器12中均分别设置有温度传感器、压力传感器和流量传感器,并且与控制氢气液化工艺流程的控制装置相连接。
本发明利用氢膨胀冷却为氢气提供冷量,并且再用气氢去回收膨胀过程中产生的膨胀功对气氢进行压缩,回收了膨胀功的同时还减少了***的压缩机的用量及体积,在使用本***之后可以减少5%-10%的压缩能耗。
本发明使用气体轴承膨胀机,轴承气为氢气,相比起油轴承,膨胀功回收过程避免了氢液化***受到污染,也无需承担除油所需的成本。
本发明通过设置过冷器,减少了液氢的闪蒸,使液氢蒸发损失小,安全隐患小。
通过对膨胀机参数的设计,所述第一返流流股和第二返流流股离开所述膨胀机的压缩端后,其压力均与离开第一换热器的膨胀流股相同。此时只需要一台压缩机组来加压。减少了压缩机数量,节约用地约20%,节约了***的成本。
第二返流流股和第一返流流股从第二换热器流出后,作为冷流股经过所述第一换热器后,再依次流经所述膨胀机的压缩端,充分利用了这两个流股的冷能,减少冷量浪费。
本发明可用于液氢运输船的再液化,也可用于陆地上的氢液化过程。
尽管本发明的内容已经通过上述优选实施例作了详细介绍,但应当认识到上述的描述不应被认为是对本发明的限制。在本领域技术人员阅读了上述内容后,对于本发明的多种修改和替代都将是显而易见的。因此,本发明的保护范围应由所附的权利要求来限定。
Claims (10)
1.一种回收膨胀功的液氢运输船再液化***,其特征在于,包含:预冷单元,氢液化单元,循环单元;
所述预冷单元包含第一换热器,用于给原料氢流股预冷;
所述氢液化单元包含第二换热器、气液分离器、过冷器;所述原料氢流股离开所述预冷单元,经过所述第二换热器形成气液两相后,到达所述气液分离器,其中气相记为第一返流流股,作为冷流股回流到所述第二换热器;而液相进入过冷器冷却到18K±5K后,分流为产品流股和第二返流流股;所述产品流股通往产品收集容器;所述第二返流流股节流降压后,作为冷流股依次回流至所述过冷器和所述第二换热器;
所述循环单元包含至少1台压缩机组和若干膨胀机;所述膨胀机均包含压缩端,其利用所述膨胀机的膨胀功给气体加压;所述膨胀机选用气体轴承膨胀机;轴承气为氢气,由所述压缩机组或所述膨胀机压缩端的氢气分出一股提供;所述轴承气在进入轴承前,先通过一减压阀减压至0.6~0.8MPa;所述膨胀机包含第一膨胀机和第二膨胀机,所述第一、第二膨胀机数量均为0~4台;所述第一返流流股从所述第二换热器流经所述第一膨胀机的压缩端后,及所述第二返流流股从所述第二换热器流经所述第二膨胀机的压缩端后,均通向所述压缩机组且合并,合并后的流股记为循环氢气流股;
所述循环氢气流股通过所述第一换热器预冷后分为膨胀流股和补充流股,所述补充流股经过所述第二换热器后,到达所述气液分离器;
所述膨胀流股经过所述第二换热器、以及所述膨胀机的膨胀端降温降压后,又作为冷流股依次流向所述第二换热器、第一换热器,最终回到所述压缩机组且并入所述循环氢气流股。
2.如权利要求1所述的回收膨胀功的液氢运输船再液化***,其特征在于,所述氢液化单元还设有第一J-T阀、第二J-T阀、第三J-T阀,用于节流降压;所述原料氢流股经过所述第二换热器后,还经过所述第一J-T阀降温降压,形成气液两相;所述补充流股,经过所述第二换热器后,还经过所述第二J-T阀降温降压,形成气液两相;所述第二返流流股经过所述第三J-T阀降温降压后,作为冷流股依次回流至所述过冷器和所述第二换热器。
3.如权利要求1所述的回收膨胀功的液氢运输船再液化***,其特征在于,所述第二换热器的原料氢通道内设有正仲氢催化剂,用于对所述原料氢进行连续的正仲转化。
4.如权利要求1所述的回收膨胀功的液氢运输船再液化***,其特征在于,所述第二返流流股从所述第二换热器流出后,作为冷流股经过所述第一换热器,再依次流经所述第二膨胀机的压缩端。
5.如权利要求1所述的回收膨胀功的液氢运输船再液化***,其特征在于,所述压缩机组仅包含一台压缩机组,所述第二返流流股、第一返流流股、膨胀流股汇合形成所述循环氢气流股后,再进入所述压缩机组压缩。
6.如权利要求1所述的回收膨胀功的液氢运输船再液化***,其特征在于,所述第一返流流股从所述第二换热器流出后,作为冷流股经过所述第一换热器后,再依次流经所述第一膨胀机的压缩端。
7.如权利要求1所述的回收膨胀功的液氢运输船再液化***,其特征在于,所述膨胀流股交替经过所述第二换热器和所述膨胀机。
8.如权利要求1所述的回收膨胀功的液氢运输船再液化***,其特征在于,所述预冷单元还包含第一净化器和正仲氢转化器;所述原料氢流股经过所述第一换热器预冷;然后依次经过所述第一净化器和正仲氢转化器后,再次经过所述第一换热器,冷却至冷剂设计温区。
9.如权利要求8所述的回收膨胀功的液氢运输船再液化***,其特征在于,还设有第二净化器,所述循环氢气流股通过所述第二净化器除去杂质,所述第一净化器和所述第二净化器用于吸附杂质气体。
10.如权利要求1所述的回收膨胀功的液氢运输船再液化***,其特征在于,所述膨胀机的数量为2-5台。
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