CN101454424A - 氢化方法 - Google Patents
氢化方法 Download PDFInfo
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- CN101454424A CN101454424A CNA2007800192654A CN200780019265A CN101454424A CN 101454424 A CN101454424 A CN 101454424A CN A2007800192654 A CNA2007800192654 A CN A2007800192654A CN 200780019265 A CN200780019265 A CN 200780019265A CN 101454424 A CN101454424 A CN 101454424A
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- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
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- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/50—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids in the presence of hydrogen, hydrogen donors or hydrogen generating compounds
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- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
- C10G3/42—Catalytic treatment
- C10G3/44—Catalytic treatment characterised by the catalyst used
- C10G3/45—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof
- C10G3/46—Catalytic treatment characterised by the catalyst used containing iron group metals or compounds thereof in combination with chromium, molybdenum, tungsten metals or compounds thereof
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- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
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Abstract
用于制备包含源自羧酸和/或羧酸酯的烃的燃料组合物的方法,所述方法包括将氢气和含烃物流进料到第一反应器中以减少所述含烃物流中烯烃和/或含杂原子化合物的含量,和将如此处理的含烃物流和氢气和羧酸和/或羧酸酯一起送入第二反应器中,以制备第二含烃物流,在所述第二含烃物流中至少一些烃源自所述羧酸和/或羧酸酯。
Description
本发明涉及氢化领域,更具体涉及加氢处理羧酸和/或羧酸酯,例如生物衍生的脂肪酸和/或脂肪酸酯,来制备燃料。
燃料例如汽油、柴油和喷气发动机燃料通常通过原油的处理来制备。在原油精炼中,通常通过将来自原油蒸馏装置的直馏馏分和源自来自原油蒸馏装置的较重或较轻馏分的改质的精炼物流混合,来制备燃料前体组合物。通常,这些组合物包含不希望的组分,比如芳香烃、烯烃或含硫化合物,要求进一步处理来使它们适合用作燃料。实现此的一种方式是使它们进行氢化过程比如加氢处理或加氢裂解,以便降低不希望的组分的含量。通常,这类方法必须前体燃料组合物和氢气在升高的温度和压力下,任选在催化剂存在下,进行接触,其中烯烃和芳香烃被氢化成链烷烃,含硫化合物被转化成硫化氢,其可以采用闪蒸容器或分离容器从燃料中去除。
随着对化石燃料衍生的二氧化碳及其对气候变化的潜在影响的日益关注,对减少释放到大气中的二氧化碳净量的燃料的要求日益增加。实现此的一种方式是使用生物质作为燃料源。生物质,无论是源自植物还是源自动物的,最终都是通过大气二氧化碳通过光合作用的固定以及相关的生物化学过程来制备。由于在生物质燃烧时释放的二氧化碳量等同于为了生产它而从大气中汲取的二氧化碳量,所以生物质燃烧是有效的CO2平衡过程。但是,由于适用作燃料比如柴油或汽油的生物衍生材料量通常并不足以满足要求,所以,生物衍生材料和现有矿物衍生燃料的混合正越来越被考虑作为减少燃料对大气CO2影响的有吸引力的选项。
与生物衍生油(比如脂肪酸和/或脂肪酸酯)和现有燃料制剂的混合相关的问题是内燃机可能需要进行修改从而以所述改变的燃料来高效运转。避免需要改变发动机的一种方式是将生物油转变成可以和现有燃料容易混合的烃。这种方法描述在例如US5702722中,其中,生物质原料和氢气反应以生成烃的混合物,其中间蒸馏馏分适于和常规柴油燃料混合。
Baldauf & Balfanz在VDE Reports No 1126(1994)pp153-168中描述了另一种方法,该方法描述了对源自精炼的中间馏出物流和源自生物的油进行共加氢处理以制备柴油燃料。
但是,与源自生物的油(包括脂肪酸和/或脂肪酸酯)和精炼中间馏出物流的共加氢处理相关的问题是,对脂肪酸和/或脂肪酸酯的加氢处理通常是比加氢处理中间馏出物燃料更放热性的和消耗更多的氢。另外,通常制备更多气体副产物比如二氧化碳,这会导致处理装置的腐蚀速度更高。
根据本发明,提出了用于制备燃料组合物的方法,所述燃料组合物包含源自羧酸和/或羧酸酯的烃,所述方法包括如下步骤:
(a)将氢气和第一含烃过程物流送入第一反应器;
(b)在第一反应器内保持足以制备第一含烃产物物流的条件,所述产物物流和第一含烃过程物流相比,具有减低浓度的含杂原子有机化合物和/或烯烃;
(c)从第一反应器中去除第一含烃产物物流;
特征在于所述方法另外包含如下步骤:
(d)将氢气、羧酸和/或羧酸酯、和至少一部分第一含烃产物物流进料至第二反应器;
(e)在第二反应器内保持足以将至少一些羧酸和/或羧酸酯转化成一种或多种烃的条件;
(f)从第二反应器中去除第二含烃产物物流,其中至少一部分烃源自羧酸和/或羧酸酯。
本发明包括两个氢化阶段,其中第一阶段包括将第一含烃过程物流和氢气接触,以降低其中所含的烯烃和/或含杂原子有机化合物的水平,从而制成第一含烃产物物流,第二步骤包括氢化羧酸和/或羧酸酯和至少一部分第一含烃产物物流的组合。这种方法使得羧酸和/或羧酸酯能够以能够很容易适应现有氢化方法(如同例如在原油精炼中进行的那样)的方式进行氢化,这样使得在第二反应器的安装和起动过程中的任何中断或停机时间变得最小。另外,第二反应器中的条件可以保持以使羧酸和/或羧酸酯氢化成为烃的过程得到最优化,所述条件可能和第一反应器中保持的条件不同。本发明特别适于制备其中源自羧酸和/或羧酸酯的组分是少数量的燃料组合物,以使所述分开的氢化能够针对每种原料获得所需燃料的最优产量。优选地,燃料包括0.1-49.9wt%的源自羧酸和/或羧酸酯的组分,比如在2-15wt%范围内。
可以使用多于一种羧酸和/或羧酸酯的混合物。优选选择羧酸和/或羧酸酯、或羧酸和/或羧酸酯的混合物,以使在第二反应器中通过反应产生的所述一种或多种烃和目标燃料中的那些处于相同范围内。例如,柴油燃料通常包含具有10-22个碳原子的烃。因此,产生碳原子数在此范围内的烃的羧酸会是合适的,比如单羧酸或二羧酸,包括正十六烷酸或1,16-二(十六烷酸)和/或其酯。脂肪酸和/或其酯也是合适的,具有通式R1C(O)OH和/或R1C(O)O-R2,其中R1和R2典型的是烃链。根据本发明在柴油燃料制备中适用的脂肪酸和/或酯的示例包括例如月桂酸、肉豆蔻酸、棕榈酸、硬脂酸、亚油酸、亚麻酸、油酸、花生酸和芥子酸和/或其酯,其中R1分别包括11、13、15、17、17、17、17、19和21个碳原子。酯可以以单甘油酯、双甘油酯或三甘油酯形式存在,通式为[R1C(O)O]nC3H5(OH)3-n,其中分别对于单甘油酯、二甘油酯或三甘油酯而言,n=1、2或3。脂肪酸和/或其酯可以具有饱和的或不饱和的烃基团。二甘油酯或三甘油酯可以包含源自相同或不同脂肪酸的烃链。
优选地,羧酸和/或羧酸酯源自生物质,是例如源自植物或动物的油或脂肪的组分。源自生物的羧酸和/或酯的使用确保和纯粹源自矿物源的等同燃料相比,所得到的燃料组合物的大气二氧化碳净排放更低。羧酸和/或羧酸酯的合适生物源包括植物衍生的油,比如油菜籽油、花生油、低芥酸菜子油、向日葵油、妥尔油、玉米油、豆油。动物油或脂肪,比如牛油脂肪或鸡脂肪,也是羧酸和/或羧酸酯的合适来源,废油比如用过的烹调油也是合适的。
生物油或脂肪包含具有碳原子数和柴油燃料中通常所见的烃相当的烃基团的三甘油酯。因此,本发明的方法优选用于制备柴油燃料,其中第二反应器保持在加氢处理条件下,这样和将生物油或脂肪转化成沸点更低燃料(这通常需要更苛刻的加氢裂解条件)比如喷气发动机燃料、汽油或LPG相比,消耗更少的氢,需要更少的能量。
在本发明的方法中,第一含烃过程物流被送入第一反应器中,于其中它和氢气反应。第一含烃过程物流合适的是液体过程物流。它可以源自煤气(gas)或煤,其中液体烃通过方法比如蒸气重整和/或部分氧化结合Fischer Tropsch合成来由其制备。或者,第一含烃过程物流可以源自原油。本发明特别适于源自原油的液体烃过程物流,因为和源自Fischer Tropsch的烃相比,它们通常含有更多的含杂原子的有机化合物。
源自原油精炼的合适过程物流包括石脑油、煤油、或者中间蒸馏馏分。过程物流可以是直接从原油蒸馏装置取出的直馏馏分,或者它可以源自或包含通过其它精炼方法比如裂解、重整、炼焦、脱芳构化和/或烷基化制备的烃。典型地,原油衍生的物流包含组分比如烯烃和/或含杂原子的有机化合物,尤其是有机硫化合物,因此通过方法比如加氢裂解或加氢处理用氢气进行合适地处理。
第一含烃过程物流优选包含中间馏分烃,其通常在150-400℃范围的温度沸腾,并且其中碳原子数典型的是10-22个碳原子。该馏分优选用于制备柴油燃料,虽然它也可以用于制备燃料油和喷气发动机燃料。直馏馏分可以和通过其它精炼方法比如更重原油馏分的蒸气裂解和/或加氢裂解制备的烃混合,所述其它精炼方法得到沸点范围和直馏馏分相似的烃。
第一含烃过程物流包含烷烃、烯烃和/或一种或多种含杂原子的化合物。典型地,含杂原子的化合物是含硫化合物,比如硫醇(mercaptan)或硫醇(thiol)。它们典型地以大于State regulatory authorities(国家管理委员会)许可的在所需燃料中的浓度的浓度存在。因此,第一含烃过程物流的硫含量典型是200ppm或更多,比如0.1wt%或更多,例如范围是0.2-2wt%,以元素硫计算。烯烃可以以至多50wt%的浓度,典型至多20wt%的浓度存在。第一含氢产物物流的其它可能的组分包括芳族化合物,比如环烷烃。优选地,第一含烃产物物流不包含羧酸和/或羧酸酯或源自生物质的成分,因为这些物质优选进料到第二反应器中。
保持第一反应器中的条件以减少第一含烃过程物流中所含的烯烃和/或含杂原子有机化合物的浓度。这可以通过采用典型用于精炼加氢裂解或加氢处理方法中的条件来实现。
加氢处理或加氢裂解通常在250-430℃的温度范围和20-200bara(2-20MPa)的压力范围内进行。条件的严格程度取决于送入反应器的含烃过程物流的本质以及所需燃料产物的本质。例如,当主要关心从适用于汽油燃料的物流中去除含杂原子的有机化合物时,通常使用采用250-350℃范围中的温度和20-40bara(2-4MPa)范围的压力的严格程度低的加氢处理条件。为了从适用于柴油燃料的过程物流中去除含杂原子的有机化合物,那么可以采用严格程度中等的加氢处理条件,温度通常是300-400℃,压力范围是30-70bara(3-7MPa)。对于真空瓦斯油原料而言,可以采用更严格的加氢处理条件,比如温度范围是350-410℃,压力范围是70-150bara(7-15MPa)。在需要对原料进行裂解以制备例如适于汽油和/或柴油燃料的烃混合物时,采用更严格的加氢裂解条件,比如温度范围是350-430℃,压力范围是100-200bara(10-20MPa)。
第一反应器中的氢化反应可以进行催化或不进行催化,优选催化。合适的催化剂包括含有Ni、Co、Mo(其它)中的一种或多种,优选Ni和Mo,或Co和Mo,的那些。催化剂通常负载在载体比如氧化锆、氧化钛或γ-氧化铝上,优选γ-氧化铝上。这种催化剂适于加氢处理(hydrotreating)和加氢裂解(hydrocracking),具体取决于反应条件。
第一反应器中的反应可以是在加氢裂解催化剂存在下的加氢裂解反应、在加氢处理催化剂存在下的加氢处理反应、或者可以加氢裂解和加氢处理反应的组合(任选地在两种或多种催化剂床的存在下)。
第一反应器的产物,也即第一含烃产物物流,和送入第一反应器的第一含烃过程物流相比,含有更低浓度的烯烃和/或含杂原子有机化合物。
在本发明的优选实施方案中,第一含烃产物物流中的硫浓度通常小于200ppm,以元素硫计算。至少一部分第一含烃产物物流被送入第二反应器,任选地并优选地采用例如闪蒸分离器预先去除轻质组分比如硫化氢和未反应的氢气。未反应的氢气可以合适地循环回到第一反应器中,用作第二反应器的原料,或者在其它地方例如在不同的精炼过程中使用。
羧酸和/或羧酸酯以及氢气和来自第一反应器的至少一部分产物物流被送入第二反应器。用已经和氢气反应的第一含烃产物物流稀释在第二反应器中的羧酸和/或羧酸酯的优点在于减少了在第二反应器中的产生的放热。这在提高例如柴油产量方面特别有利,因为减少了更适于汽油或LPG(液化石油气)的轻质烃的生成。也可以通过使催化剂暴露的温度最小化,来延长催化剂的有效寿命。另外,第一含烃产物物流的稀释效果可以通过减少羧酸和/或羧酸酯的不希望的副反应来缓解可能发生的催化剂结焦程度。该稀释效应也可以减少催化剂床中的氢气消耗,从而减少催化剂结焦。针对第二反应器将羧酸和/或羧酸酯和一部分第一产物物流结合起来的另一优点是,可以进一步减少来自第一反应器的第一产物物流中存留的任何残余烯烃和/或含杂原子有机化合物的浓度。
羧酸和/或羧酸酯、氢气和所述部分的第一含烃产物物流可以分别送入到第二反应器中。或者,可以在送入第二反应器之前预先混合任何或所有的所述独立的组分。任选地,除了所述第一含烃产物物流和羧酸和/或羧酸酯以外,另外的烃,例如还没有送入第一反应器的第一含烃过程物流的一部分可以送入到第二反应器中。在该实施方案中,送入第二反应器的任何另外烃的量足够低,以至于用已经氢化的产物物流(第一含烃产物物流)稀释羧酸和/或羧酸酯的优点仍然能够实现。
第二反应器中的条件经保持以使羧酸和/或羧酸酯被转化成一种或多种烃。典型的,在该反应中也生成其它副产物比如二氧化碳、一氧化碳、丙烷和水。在第二反应器中保持如上所述通常用于加氢处理器或加氢裂解器中的条件,这些条件依赖于送入该反应器的羧酸和/或羧酸酯或生物质材料的本质。羧酸和/或羧酸酯消耗的氢气通常大于也送入第二反应器的含烃第一产物物流所消耗的,因此,通常保持加氢处理条件以便防止在过程比如任何进料组分的加氢裂解中利用多于必需的氢气。通常保持200—410℃范围中的温度,优选320-410℃范围内。典型的,使用20-200bara(2-20MPa)范围内的压力,优选在50-200bara(5-20MPa)范围内的压力。在该反应器优选保持条件以使实现羧酸和/或羧酸酯的几乎完全转化,例如大于90wt%转化,优选大约95%转化。
从第二反应器中去除的第二含烃产物物流包含一种或多种源自送入第二反应器的羧酸和/或羧酸酯的烃。任选的和优选的,第二含烃产物物流被处理以去除轻质杂质,比如未反应的氢气或者源自第一含烃产物物流的进一步脱硫的任何硫化氢。这合适地通过例如闪蒸分离器实现。
由于第二反应器优选在加氢处理条件下操作,所以第二反应器中的催化剂优选是至此为止描述的加氢处理催化剂。在本发明的在第二反应器中具有硫化的催化剂的实施方案中,在第一反应器中的脱硫反应产生的硫化氢能够有利地帮助在第二反应器中保持硫化的活性金属。
第一和第二含烃产物物流的一种或两种可以包含太轻或太重而不能用作单一类型燃料的一些烃。因此,所述产物物流之一或两者可以任选地分馏或者蒸馏以使例如轻质烃馏分、汽油馏分、喷气发动机燃料馏分和柴油馏分中的一种或多种可以生产出来。这样使得来自本方法的废物最少,确保了最终燃料掺混物保持通过本发明之外的方式制备的类似燃料的质量和一致性(consistency)。
现在将参考图1举例说明本方法,图1是根据本发明方法的示意概述。
将硫含量为1wt%的直馏中间馏分物流1和氢气2一起送入第一反应器3,所述第一反应器含有硫化的Co-Mo/氧化铝催化剂。第一反应器中的条件是370℃和100bara压力。所述中间馏分在催化剂上的液体时空速度(LHSV)是3hr-1。从该反应器中去除的第一含烃产物物流4(硫含量为75ppm)和脂油原料5结合起来,和氢气6一起送入第二反应器7中。第二反应器保持在350℃和99bara压力,总LHSV(也即,来自第一反应器的产物和生物油的组合LHSV)为4hr-1。从第二反应器中去除的第二含烃产物物流8被送入闪蒸分离器9中,其中挥发性组分10(包括H2S和未反应的氢气)从包含燃料烃的液相11中分离。包含燃料烃的液相被送入在2bara工作的分馏和汽提塔12中,塔底部温度是380℃。含有轻质烃和硫化氢的液相13从塔顶去除,喷气发动机燃料物流4从塔的中间部分去除(在燃料烃物流11送入的位点上方),从塔底部取出柴油燃料物流15。柴油燃料的硫含量小于50ppm。
Claims (11)
1、用于制备包含源自羧酸和/或羧酸酯的烃的燃料组合物的方法,所述方法包括下列步骤:
(a)将氢气和第一含烃过程物流进料到第一反应器中;
(b)在第一反应器中保持足以制备第一含烃产物物流的条件,所述第一含烃产物物流和第一含烃过程物流相比,含杂原子的有机化合物和/或烯烃的浓度减少;
(c)从第一反应器中取出所述第一含烃产物物流;
特征在于所述方法另外包括下列步骤:
(d)将氢气、羧酸和/或羧酸酯、和至少一部分第一含烃产物物流进料至第二反应器;
(e)在第二反应器中保持足以将至少一些所述羧酸和/或羧酸酯转化成一种或多种烃的条件;
(f)从第二反应器中取出第二含烃产物物流,其中至少一部分所述烃源自所述羧酸和/或羧酸酯。
2、权利要求1的方法,其中所述燃料组合物是柴油燃料。
3、权利要求1或2的方法,其中羧酸和/或羧酸酯是脂肪酸和/或脂肪酸酯。
4、权利要求1-3任一的方法,其中所述羧酸和/或羧酸酯源自植物或动物脂肪或油。
5、权利要求1-4任一的方法,其中第一含烃过程物流包含来自原油精炼的中间馏分烃。
6、权利要求5的方法,其中所述烃包含直馏中间馏分烃以及源自其它精炼方法的沸腾范围和所述直馏馏分相似的烃。
7、权利要求1-6任一的方法,其中第一含烃过程物流的硫浓度为200ppm或更多,以元素硫计算。
8、权利要求1-7任一的方法,其中第一含氢产物物流包含小于200ppm的硫,以元素硫计算。
9、权利要求1-8任一的方法,其中第一反应器保持在250-430℃范围内的温度和20-200bara(2-20MPa)范围内的压力。
10、权利要求1-9任一的方法,其中第二反应器保持在200-410℃范围内的温度和20-200bara(2-20MPa)范围内的压力。
11、权利要求1-11任一的方法,其中将另外的烃送料到第二反应器中。
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PCT/GB2007/001841 WO2007138254A1 (en) | 2006-05-25 | 2007-05-18 | Hydrogenation process |
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EP (1) | EP2019854B1 (zh) |
CN (1) | CN101454424B (zh) |
AT (1) | ATE509995T1 (zh) |
AU (1) | AU2007266927B2 (zh) |
BR (1) | BRPI0712612A2 (zh) |
CA (1) | CA2652739C (zh) |
ES (1) | ES2365873T3 (zh) |
MY (1) | MY146604A (zh) |
NZ (1) | NZ572743A (zh) |
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CN103102967A (zh) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | 一种副产柴油的蜡油加氢处理方法 |
CN103102967B (zh) * | 2011-11-10 | 2015-02-18 | 中国石油化工股份有限公司 | 一种副产柴油的蜡油加氢处理方法 |
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EP2019854B1 (en) | 2011-05-18 |
ZA200809793B (en) | 2012-04-24 |
AU2007266927A1 (en) | 2007-12-06 |
AU2007266927B2 (en) | 2011-12-22 |
ES2365873T3 (es) | 2011-10-11 |
WO2007138254A1 (en) | 2007-12-06 |
CA2652739C (en) | 2014-12-02 |
CN101454424B (zh) | 2012-07-04 |
MY146604A (en) | 2012-08-30 |
ATE509995T1 (de) | 2011-06-15 |
BRPI0712612A2 (pt) | 2012-10-23 |
EP2019854A1 (en) | 2009-02-04 |
NZ572743A (en) | 2011-04-29 |
US20090107033A1 (en) | 2009-04-30 |
CA2652739A1 (en) | 2007-12-06 |
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