CN110655950B - 一种用于烷基苯生产的馏分油预处理方法和系统 - Google Patents
一种用于烷基苯生产的馏分油预处理方法和系统 Download PDFInfo
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- 150000004996 alkyl benzenes Chemical class 0.000 title claims abstract description 11
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 10
- 238000002203 pretreatment Methods 0.000 title claims description 7
- 230000007935 neutral effect Effects 0.000 claims abstract description 36
- 238000000605 extraction Methods 0.000 claims abstract description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 30
- 238000001179 sorption measurement Methods 0.000 claims abstract description 26
- 239000000839 emulsion Substances 0.000 claims abstract description 19
- 238000011084 recovery Methods 0.000 claims abstract description 19
- 238000000034 method Methods 0.000 claims abstract description 18
- 150000001875 compounds Chemical class 0.000 claims abstract description 15
- 229910017053 inorganic salt Inorganic materials 0.000 claims abstract description 15
- 239000012266 salt solution Substances 0.000 claims abstract description 14
- 238000005406 washing Methods 0.000 claims abstract description 12
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000001301 oxygen Substances 0.000 claims abstract description 11
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 11
- 239000003513 alkali Substances 0.000 claims abstract description 10
- 239000002585 base Substances 0.000 claims abstract description 10
- 238000006243 chemical reaction Methods 0.000 claims abstract description 10
- 239000000243 solution Substances 0.000 claims abstract description 10
- 239000002798 polar solvent Substances 0.000 claims abstract description 9
- 238000005804 alkylation reaction Methods 0.000 claims abstract description 8
- 239000003463 adsorbent Substances 0.000 claims abstract description 7
- 230000029936 alkylation Effects 0.000 claims abstract description 7
- 238000009835 boiling Methods 0.000 claims abstract description 7
- 238000007599 discharging Methods 0.000 claims abstract description 7
- 238000003756 stirring Methods 0.000 claims abstract description 4
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 9
- 230000008569 process Effects 0.000 claims description 7
- 239000007789 gas Substances 0.000 claims description 6
- 239000002808 molecular sieve Substances 0.000 claims description 5
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 5
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 claims description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 4
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 4
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 claims description 4
- TYJJADVDDVDEDZ-UHFFFAOYSA-M potassium hydrogencarbonate Chemical compound [K+].OC([O-])=O TYJJADVDDVDEDZ-UHFFFAOYSA-M 0.000 claims description 4
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 3
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 claims description 2
- 239000001110 calcium chloride Substances 0.000 claims description 2
- 229910001628 calcium chloride Inorganic materials 0.000 claims description 2
- 239000011736 potassium bicarbonate Substances 0.000 claims description 2
- 235000015497 potassium bicarbonate Nutrition 0.000 claims description 2
- 229910000028 potassium bicarbonate Inorganic materials 0.000 claims description 2
- 229910000027 potassium carbonate Inorganic materials 0.000 claims description 2
- 235000011181 potassium carbonates Nutrition 0.000 claims description 2
- 239000001103 potassium chloride Substances 0.000 claims description 2
- 235000011164 potassium chloride Nutrition 0.000 claims description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 2
- 235000017550 sodium carbonate Nutrition 0.000 claims description 2
- 239000011780 sodium chloride Substances 0.000 claims description 2
- UIIMBOGNXHQVGW-DEQYMQKBSA-M Sodium bicarbonate-14C Chemical compound [Na+].O[14C]([O-])=O UIIMBOGNXHQVGW-DEQYMQKBSA-M 0.000 claims 1
- 230000005684 electric field Effects 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000004062 sedimentation Methods 0.000 abstract description 3
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- 239000012071 phase Substances 0.000 description 24
- 238000006386 neutralization reaction Methods 0.000 description 10
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- 239000003795 chemical substances by application Substances 0.000 description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 239000003208 petroleum Substances 0.000 description 6
- 239000002253 acid Substances 0.000 description 5
- 239000000872 buffer Substances 0.000 description 5
- 238000001816 cooling Methods 0.000 description 5
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- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 238000010992 reflux Methods 0.000 description 4
- 239000011734 sodium Substances 0.000 description 4
- 229910052708 sodium Inorganic materials 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 238000004945 emulsification Methods 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 2
- 125000002947 alkylene group Chemical group 0.000 description 2
- 239000008346 aqueous phase Substances 0.000 description 2
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- 239000007788 liquid Substances 0.000 description 2
- 230000003472 neutralizing effect Effects 0.000 description 2
- 238000005191 phase separation Methods 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 239000003945 anionic surfactant Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000008139 complexing agent Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
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- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000004745 nonwoven fabric Substances 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 1
- 235000017557 sodium bicarbonate Nutrition 0.000 description 1
- 238000005063 solubilization Methods 0.000 description 1
- 230000007928 solubilization Effects 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000002699 waste material Substances 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
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
- C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
- C10G53/12—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one alkaline treatment step
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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
- C10G57/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process
- C10G57/005—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process with alkylation
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- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
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- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
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Abstract
一种用于烷基苯生产的馏分油预处理方法和系统，包括：在反应器中加入馏分油、弱碱溶液和无机盐溶液，充分搅拌，待反应完全后，静置分层；排出产生的乳相和水相，在油相中加入水和无机盐溶液进行水洗以去除多余碱液，静置分层；排出产生的乳相和水相，将中性馏分油输送至萃取装置；在萃取装置中利用高沸点极性溶剂萃取中性馏分油中的含氧化合物，然后将中性馏分油输送到吸附装置，将含有含氧化合物的萃取剂输送至萃取剂回收装置；在吸附装置中利用吸附剂吸附分离中性馏分油中的含氧化合物，然后将中性馏分油输送至烷基化反应器进行反应。本发明利用弱碱中和馏分油，废水易处理；无需高压电场沉降，能耗低；使用高沸点极性萃取剂，选取范围更广。
Description
技术领域
本发明属于化工合成技术领域，具体涉及一种用于烷基苯生产的馏分油预处理方法和系统。
背景技术
费托轻质馏分油因其直链烯烃含量高而可以用作制备烷基苯的原料。但因费托轻质馏分油成分复杂，含氧化物含量高，呈弱酸性，不易直接作为烷基化反应原料，而需要中和、水洗、脱含氧化物等预处理步骤。对于馏分油中和、水洗步骤来说，馏分油碱洗电精制脱酸工艺是含酸原油加工的重要手段。自20世纪30年代以来，它在国内外已得到广泛应用。在现有的碱洗电精制脱酸工艺中，碱大量过剩，在石油酸钠、碱、高温和搅拌混合条件下，氢氧化钠与馏分油中的石油酸发生等摩尔反应，生成的石油酸钠是一种阴离子表面活性剂，对馏分油有乳化和增溶作用，造成了油水乳化严重。这就需要加入馏分油脱酸剂。馏分油脱酸剂是由氢氧化钠、破乳剂、萃取剂、脱油剂等溶剂组成的一种多功能复合剂。其中破乳剂起破乳作用，消除乳化，加速油剂相分离；萃取剂抽提石油酸钠；脱油剂脱出碱渣中的中性油，提高精制油收率。脱酸剂具有与石油酸反应、破乳、抽提石油酸钠和脱油功能。现有的馏分油碱洗电精制脱酸工艺存在以下问题：1.加入强碱氢氧化钠，用碱量大，废液污染环境，不易治理。2.油水易乳化，破乳剂消耗大，难以回收，产品收率低。3.使用高压电场沉降分离，能耗高。
近20年来，人们一直在研究高效、清洁的脱酸方法，但这些方法均不同程度地存在投资较大、操作费用高和不够完善等问题。
发明内容
为了解决现有技术中存在的问题，本发明提出了一种用于烷基苯生产的馏分油预处理方法和系统，尤其适用于预处理用于烷基苯生产的费托轻质馏分油。
为了达到上述目的，一方面，本发明提出了一种用于烷基苯生产的馏分油预处理方法，包括：
在反应器中加入馏分油、弱碱溶液和无机盐溶液，充分搅拌，待反应完全后，静置分层，排出产生的乳相和水相；
在油相中加入水和无机盐溶液进行水洗以去除多余碱液，静置分层，排出产生的乳相和水相；
将中性馏分油输送至萃取单元，利用高沸点极性溶剂萃取中性馏分油中的含氧化合物，然后将中性馏分油输送到吸附单元，将含有含氧化合物的萃取剂输送至萃取剂回收单元；
在吸附单元中利用吸附剂吸附分离中性馏分油中的含氧化合物，然后将中性馏分油输送至烷基化反应器进行反应。
优选地，所述弱碱溶液选自碳酸钾、碳酸钠、碳酸氢钾、碳酸氢钠中的一种或多种。
优选地，所述无机盐溶液选自氯化钾、氯化钠、氯化钙中的一种或多种。
优选地，所述高沸点极性溶剂选自N-甲基吡咯烷酮、乙二醇中的一种或多种。
优选地，在萃取步骤中，中性馏分油在所述萃取单元的中部进料，所述高沸点极性溶剂在所述萃取单元的上部进料。
优选地，在萃取步骤中，冷却从所述萃取单元排出的气体，并回收其中的中性馏分油，优选地，在低压状态下回收其中的中性馏分油。
优选地，在萃取剂回收步骤中，回收的萃取剂输送至所述萃取单元中循环利用。
优选地，在萃取剂回收步骤中，冷却从所述萃取剂回收单元排出的气体，并回收其中的含氧化合物，优选地，在低压状态下回收其中的含氧化合物。
优选地，所述吸附剂选自ZSM-5、3A、4A、5A、10X、13X分子筛中的一种或多种。
优选地，将中性馏分油输送到吸附单元之前，对中性馏分油进行预热处理。
另一方面，本发明提出了一种用于烷基苯生产的馏分油预处理系统，包括依次连接的中和反应单元、萃取单元、萃取剂回收单元和吸附单元，
其中所述中和反应单元设置有馏分油入口、注水口、弱碱溶液入口、无机盐溶液入口、中性馏分油出口以及乳相和水相出口；
所述萃取单元的上部与萃取剂输送管道相连，中部与所述中和反应单元的中性馏分油出口相连，底部与所述萃取剂回收单元的入口相连，顶部与所述吸附单元的入口相连；
所述萃取剂回收单元的顶部与含氧化合物排出管道相连，底部与所述萃取剂输送管道相连；
所述吸附单元的顶部与烷基化反应器相连。
优选地，所述中和反应单元的顶部设置氮封。
优选地，所述萃取单元的顶部设置有冷却单元，用于冷却回收顶部排出气体中的馏分油。
优选地，所述冷却单元通过萃取回流罐与所述吸附单元相连。优选地，所述回流罐通过真空缓冲器与真空泵相连。
优选地，所述萃取单元的底部设置有再沸器。
优选地，所述萃取剂回收单元的顶部设置有冷却单元，用于回收顶部排出气体中的含氧化合物。
优选地，所述冷却单元通过回流罐与含氧化合物排出管道相连。优选地，所述回流罐通过真空缓冲器与真空泵相连。
优选地，所述萃取剂回收单元的底部设置有再沸器。优选地，所述吸附单元内填充有ZSM-5、3A、4A、5A、10X、13X分子筛中的一种或多种。
优选地，所述萃取单元与所述吸附单元之间设置有预热器。
优选地，所述吸附单元与烷基化反应器之间设置有冷凝器。
与现有技术相比，本发明的技术方案具有以下有益效果：
1.本发明的方法使用弱碱中和，废水易处理；
2.本发明的方法加入简单无机盐溶液破乳后，乳相随水相流入后续工段进行处理，油相回收利用，产品收率高；
3.本发明的方法无需高压电场沉降，能耗低；
4.本发明所选取的萃取剂为高沸点极性萃取剂，选取范围更广，操作难度小。
5.本发明选用气态吸附，吸附效果更加显著，可将含氧化物量降到0.1ppm以下。
附图说明
图1为本发明中馏分油预处理方法的流程图；
图2为本发明实施例中馏分油预处理系统的中和单元和乳相水相处理单元示意图；
图3为本发明实施例中馏分油预处理系统的萃取单元和萃取剂回收单元示意图；
图4为本发明实施例中馏分油预处理系统的吸附单元示意图。
具体实施方式
为使本发明的目的、技术方案和优点更加清楚明白，以下结合具体实施例，并参照附图，对本发明作进一步的详细说明。
如图1所示，本发明提出了一种用于烷基苯生产的馏分油预处理方法包括：
(1)馏分油与弱碱溶液中和反应。
在该步骤中，在反应器中加入馏分油、弱碱溶液和无机盐溶液，充分搅拌，待反应完全后，静置分层，排出产生的乳相和水相。
(2)油相水洗。
在该步骤中，在油相中加入水和无机盐溶液进行水洗以去除多余碱液，静置分层，排出产生的乳相和水相。
(3)萃取中性馏分油中的含氧化合物。
在该步骤中，将中性馏分油输送至萃取装置，在萃取装置中利用高沸点极性溶剂萃取中性馏分油中的含氧化合物，然后将中性馏分油输送到吸附装置，将含有含氧化合物的萃取剂输送至萃取剂回收装置。
(4)吸附中性馏分油中的含氧化合物。
在该步骤中，利用吸附剂吸附分离中性馏分油中的含氧化合物，然后将中性馏分油输送至烷基化反应器进行反应。
如图2所示，在一实施例中，原料首先进入中和反应器R-1，反应器顶部分别设有馏分油、水、无机盐破乳剂、碳酸钾溶液管道。反应器顶部设置氮封及分程控制，保持反应器内部压力0.25～0.35MPa。
先将馏分油与适量的碳酸钾溶液、无机盐溶液充分搅拌4小时，待反应完全后，静置分层1小时，将乳相和水相通过底部出口管放出至静置分相罐，然后注水进行水洗，去除多余碱液，水洗时同样加入适量无机盐溶液。
水洗后，静置分层1小时，将乳相和水相放出至静置分相罐，然后将中性馏分油送出装置。
静置分相罐V-1内设置隔油板和浮子界位计，控制乳相和水相的界位使其不高于隔油板的高度，超过隔油板高度的乳相溢流至隔油板的另一侧。分相罐顶部设置氮封及分程控制，保持内部压力0.2～0.3MPa。
静置1小时后(每当前工序中和反应器不送料时，即可认为开始静置)，将水相通过水相泵P-1送至水处理单元；将含水乳液通过乳相泵P-2送至滤油器V-2。
含水乳液通过乳相泵P-2送至滤油器V-2中，控制乳相泵P-2出口压力0.2～3.0Mpa。
滤油器内部设置无纺布滤芯或其它类似滤油材料，顶部设置玻璃界位计。水分子可通过滤芯，在容器底部积存；油分子不可通过滤芯而在其表面集聚成大油滴，上升到容器顶部。
定期通过玻璃界位计观察油位，当油位到达界位计中部时，打开顶部排油阀，将油排至回收油缓冲罐V-3。
回收油缓冲罐顶设置压力表及放空线，保持管内压力恒定为常压。
待回收油缓冲罐V-3内建立液位后，启动回收泵P-4，将回收油送回中和反应器R-1内，完成轻质馏分油回收；也可视工况直接将回收油送出装置。
如图3所示，来自中和反应器R-1的中性馏分油，进入萃取塔(中部进料)，与NMP或乙二醇等高沸点极性溶剂逆向接触(上部进料)，塔顶烷烯混合物去吸附装置进一步脱除含氧化物。塔底为含氧化物及萃取剂的混合物，进入回收塔进行萃取剂的分离，含氧化物自塔顶馏出，萃取剂自塔底馏出，进入萃取塔循环使用。
萃取塔操作温度为塔底0-300℃，塔顶0-200℃。操作压力为1Pa-2.0MPa。优选地，塔底温度为150-260℃，塔顶温度为50-150℃，操作压力为0.5-1kPa。
回收塔操作温度为塔底0-300℃，塔顶0-200℃。操作压力为1Pa-2.0MPa。优选地，塔底温度为150-260℃，塔顶温度为50-160℃，操作压力为0.5-1kPa。
如图4所示，自萃取塔来的中性馏分油(烷烯混合物)进入预热炉，再进入装有分子筛的吸附塔，对含氧化物进行进一步吸附分离。原料加热后，以气态进行吸附，吸附后的烷烯混合物进入烷基化反应器进行反应。
吸附塔内吸附剂可以为ZSM-5、3A、4A、5A、10X、13X等类似各类分子筛。预热炉操作温度为50-300℃，优选为150-300℃，操作压力为0.1MPa-2.0MPa。吸附塔有两种工况，常温吸附和高温解吸，吸附塔操作温度为0-300℃，操作压力为0.1MPa-2.0MPa。
以上所述的具体实施例，对本发明的目的、技术方案和有益效果进行了进一步详细说明，应理解的是，以上所述仅为本发明的具体实施例而已，并不用于限制本发明，凡在本发明的精神和原则之内，所做的任何修改、等同替换、改进等，均应包含在本发明的保护范围之内。
Claims (9)
1.一种用于烷基苯生产的馏分油预处理方法，其特征在于，包括：
在反应器中加入馏分油、弱碱溶液和无机盐溶液，充分搅拌，待反应完全后，静置分层，排出产生的乳相和水相；
在油相中加入水和无机盐溶液进行水洗以去除多余碱液，静置分层，排出产生的乳相和水相；
将中性馏分油输送至萃取单元，利用高沸点极性溶剂萃取中性馏分油中的含氧化合物，然后将中性馏分油输送到吸附单元，将含有含氧化合物的萃取剂输送至萃取剂回收单元；
在吸附单元中利用吸附剂吸附分离中性馏分油中的含氧化合物，然后将中性馏分油输送至烷基化反应器进行反应；
其中，所述弱碱溶液选自碳酸钾、碳酸钠、碳酸氢钾、碳酸氢钠中的一种或多种，所述无机盐溶液选自氯化钾、氯化钠、氯化钙中的一种或多种；所述高沸点极性溶剂选自N-甲基吡咯烷酮、乙二醇中的一种或多种。
2.根据权利要求1所述的馏分油预处理方法，其中，在萃取步骤中，中性馏分油在所述萃取单元的中部进料，所述高沸点极性溶剂在所述萃取单元的上部进料。
3.根据权利要求1所述的馏分油预处理方法，其中，在萃取步骤中，冷却从所述萃取单元排出的气体混合物，并回收其中的中性馏分油。
4.根据权利要求3所述的馏分油预处理方法，其中，在低压状态下回收其中的中性馏分油。
5.根据权利要求1所述的馏分油预处理方法，其中，在萃取剂回收步骤中，回收的萃取剂输送至所述萃取单元中循环利用。
6.根据权利要求1所述的馏分油预处理方法，其中，在萃取剂回收步骤中，冷却从所述萃取剂回收单元排出的气体混合物，并回收其中的含氧化合物。
7.根据权利要求6所述的馏分油预处理方法，其中，在低压状态下回收其中的含氧化合物。
8.根据权利要求1所述的馏分油预处理方法，其中，所述吸附剂选自ZSM-5、3A、4A、5A、10X、13X分子筛中的一种或多种。
9.根据权利要求1所述的馏分油预处理方法，其中，将中性馏分油输送到吸附单元前，对中性馏分油进行预热处理。
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106675625A (zh) * | 2017-01-23 | 2017-05-17 | 洛阳和梦科技有限公司 | 费托合成轻质馏分油精制装置 |
| CN106753546A (zh) * | 2017-01-23 | 2017-05-31 | 洛阳和梦科技有限公司 | 费托合成轻质馏分油精制新工艺 |
| CN208632469U (zh) * | 2018-06-29 | 2019-03-22 | 内蒙古伊泰煤基新材料研究院有限公司 | 一种用于烷基苯生产的馏分油预处理系统 |
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| Publication number | Publication date |
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| WO2020001269A1 (zh) | 2020-01-02 |
| CN110655950A (zh) | 2020-01-07 |
| EP3760695A1 (en) | 2021-01-06 |
| US11306262B2 (en) | 2022-04-19 |
| EP3760695A4 (en) | 2021-11-03 |
| US20210054296A1 (en) | 2021-02-25 |
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