CN106520195B - A kind of method for hydrogen cracking for improving boat coal quality - Google Patents
A kind of method for hydrogen cracking for improving boat coal quality Download PDFInfo
- Publication number
- CN106520195B CN106520195B CN201510578869.9A CN201510578869A CN106520195B CN 106520195 B CN106520195 B CN 106520195B CN 201510578869 A CN201510578869 A CN 201510578869A CN 106520195 B CN106520195 B CN 106520195B
- Authority
- CN
- China
- Prior art keywords
- fraction
- kerosene
- jet
- oil
- hydrocracking
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000000034 method Methods 0.000 title claims abstract description 72
- 229910052739 hydrogen Inorganic materials 0.000 title claims description 28
- 239000001257 hydrogen Substances 0.000 title claims description 28
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims description 25
- 239000003245 coal Substances 0.000 title claims description 25
- 238000005336 cracking Methods 0.000 title claims description 6
- 239000003350 kerosene Substances 0.000 claims abstract description 184
- 238000004517 catalytic hydrocracking Methods 0.000 claims abstract description 80
- 238000006243 chemical reaction Methods 0.000 claims abstract description 77
- 238000007670 refining Methods 0.000 claims abstract description 22
- 239000000047 product Substances 0.000 claims description 74
- 239000003054 catalyst Substances 0.000 claims description 60
- 229910052751 metal Inorganic materials 0.000 claims description 18
- 238000005984 hydrogenation reaction Methods 0.000 claims description 17
- 239000002184 metal Substances 0.000 claims description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 10
- 229910000510 noble metal Inorganic materials 0.000 claims description 10
- 239000002283 diesel fuel Substances 0.000 claims description 7
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- 229910052717 sulfur Inorganic materials 0.000 claims description 5
- 239000011593 sulfur Substances 0.000 claims description 5
- 238000000605 extraction Methods 0.000 claims description 4
- 238000009835 boiling Methods 0.000 claims description 2
- 238000004523 catalytic cracking Methods 0.000 claims description 2
- 239000012263 liquid product Substances 0.000 claims description 2
- 239000010970 precious metal Substances 0.000 claims 2
- 229910021536 Zeolite Inorganic materials 0.000 claims 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims 1
- 239000010457 zeolite Substances 0.000 claims 1
- 239000000446 fuel Substances 0.000 abstract description 74
- 238000005194 fractionation Methods 0.000 abstract description 41
- 239000007791 liquid phase Substances 0.000 abstract description 19
- 239000003921 oil Substances 0.000 description 54
- 239000000779 smoke Substances 0.000 description 26
- 230000000052 comparative effect Effects 0.000 description 14
- 230000008569 process Effects 0.000 description 13
- 239000002994 raw material Substances 0.000 description 10
- 238000000926 separation method Methods 0.000 description 9
- 239000007788 liquid Substances 0.000 description 8
- 238000004821 distillation Methods 0.000 description 7
- 239000007789 gas Substances 0.000 description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- MXRIRQGCELJRSN-UHFFFAOYSA-N O.O.O.[Al] Chemical compound O.O.O.[Al] MXRIRQGCELJRSN-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 2
- 238000005520 cutting process Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000011959 amorphous silica alumina Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000004508 fractional distillation Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 229910052814 silicon oxide Inorganic materials 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
本发明涉及炼油领域，公开了一种改善航煤质量的加氢裂化方法，该方法包括1)将来自加氢裂化反应区的液相产物进行分馏，得到石脑油馏分、煤油馏分、柴油馏分和尾油馏分；2)将步骤1)得到的煤油馏分引入煤油分馏塔进行分馏，得到轻质航煤馏分、中质航煤馏分和重质航煤馏分，抽出至少部分所述中质航煤馏分，以及将轻质航煤馏分、重质航煤馏分和任选的剩余部分的中质航煤馏分作为航煤产品出装置。本发明提供的方法能够经济且灵活地有效提高加氢裂化装置的航煤质量。
The invention relates to the field of oil refining, and discloses a hydrocracking method for improving the quality of jet fuel. The method comprises 1) fractionating liquid phase products from a hydrocracking reaction zone to obtain naphtha fractions, kerosene fractions, and diesel fractions and tail oil fraction; 2) the kerosene fraction obtained in step 1) is introduced into a kerosene fractionation tower for fractionation to obtain a light aviation kerosene fraction, a medium aviation kerosene fraction and a heavy aviation kerosene fraction, and extract at least part of the medium aviation kerosene Distillate, and light jet fuel fraction, heavy jet fuel fraction and the optional remaining part of medium jet fuel fraction are output as jet fuel products. The method provided by the invention can economically and flexibly improve the quality of jet fuel in a hydrocracking unit effectively.
Description
技术领域technical field
本发明涉及炼油领域，具体地，涉及一种改善航煤质量的加氢裂化方法。The invention relates to the field of oil refining, in particular to a hydrocracking method for improving the quality of aviation coal.
背景技术Background technique
我国国民经济的持续发展促进了交通运输能力的迅速提高，近期航空运输燃料的需求量也越来越大。通常航煤馏分的来源途径主要有：经蒸馏装置得到的煤油馏分进行脱硫醇；减压蜡油通过加氢裂化过程生产航煤。经蒸馏装置得到的航煤馏分因受到原油加工能力以及航煤馏分收率的限制，其产量相对固定；而加氢裂化过程可将重质馏分油转化为轻质产品，通过调整操作、改善催化剂的选择性以及工艺流程的改进等手段，航煤收率可实现在较大范围内灵活变化。The continuous development of my country's national economy has promoted the rapid improvement of transportation capacity, and the demand for air transportation fuel is also increasing recently. Usually, the sources of aviation kerosene fractions mainly include: sweetening of kerosene fractions obtained through distillation units; and production of jet kerosene by hydrocracking process of vacuum wax oil. Due to the limitation of the crude oil processing capacity and the yield of jet fuel fraction obtained by the distillation unit, its output is relatively fixed; while the hydrocracking process can convert heavy distillate oil into light products, by adjusting the operation and improving the catalyst The selectivity and the improvement of the technological process and other means, the jet fuel yield can be flexibly changed in a wide range.
加氢裂化过程以减压蜡油、焦化蜡油和FCC轻循环油等劣质原料为进料，可获得石脑油、中间馏分油(包括航煤和柴油)以及尾油等产品，但其航煤质量与进料性质、反应氢分压、转化深度以及装置的运转时间密切相关。The hydrocracking process uses low-quality raw materials such as vacuum gas oil, coker gas oil, and FCC light cycle oil as feed materials, and can obtain products such as naphtha, middle distillates (including aviation kerosene and diesel oil) and tail oil, but its aviation Coal quality is closely related to feed properties, reaction hydrogen partial pressure, conversion depth and operating time of the unit.
通常情况下，原料劣质化、转化深度降低都会导致航煤质量变差，烟点降低，尤其到运转末期，此阶段反应温度偏高，催化剂芳烃饱和性能下降，航煤烟点较初期下降明显。In general, inferior raw materials and reduced conversion depth will lead to poor quality of jet fuel and lower smoke point, especially at the end of operation, when the reaction temperature is relatively high at this stage, the aromatics saturation performance of the catalyst will decrease, and the smoke point of jet fuel will drop significantly compared with the initial stage.
对于已有的加氢裂化装置，其反应氢分压、工艺流程相对固定、转化深度也通常会由于后续分馏系统存在瓶颈难以大幅度调整，在进料性质劣质化趋势明显的大趋势下，如何提高其航煤烟点，尤其是提高运转末期的航煤烟点是一个亟待解决的问题。For the existing hydrocracking unit, the reaction hydrogen partial pressure, the process flow are relatively fixed, and the conversion depth is usually difficult to greatly adjust due to the bottleneck in the subsequent fractionation system. It is an urgent problem to improve the smoke point of aviation fuel, especially the smoke point of aviation fuel at the end of operation.
CN103013559A公开了一种提高加氢裂化航煤产量的方法，该方法包括将重柴油馏分返回到原料油一起进行继续反应，其中循环重柴油馏分占总重柴油馏分的质量百分数为10％～100％。该方法可以在原有基础上增产航煤，但未能提出有效改善现有航煤质量的方案。CN103013559A discloses a method for increasing the output of hydrocracking jet fuel, the method includes returning the heavy diesel oil fraction to the raw material oil to continue the reaction, wherein the mass percentage of the circulating heavy diesel oil fraction in the total heavy diesel oil fraction is 10% to 100% . This method can increase the production of jet fuel on the original basis, but fails to propose an effective solution to improve the quality of the existing jet fuel.
US4172815公开了同时生产喷气燃料和柴油的单段循环加氢裂化方法，原料的初馏点大于500℉(约260℃)。其工艺流程简单描述如下：原料油经过加氢裂化，在压力大于1000psig(约6.9Mpa)的反应条件下反应，反应流出物经过分馏，得到石脑油馏分、喷气燃料馏分、柴油馏分和尾油，喷气燃料馏分全部或部分与尾油混合，送回裂化反应区。该方法在较为缓和的加氢裂化条件下，可达到同时最大量生产喷气燃料和柴油的目的，航煤的质量也得到改善。该方法涉及了循环航煤馏分从而改善航煤质量的构思，但循环航煤馏分一方面会增加能耗，另一方面也会提高反应的总空速，对加氢裂化反应有负面影响；在加氢裂化装置运转末期，其催化剂性能已经低于初期，且反应温度较高，没有大的调整空间，因此循环航煤馏分、提高空速后可能会影响整体加氢裂化效果，不一定适用于现有加氢裂化装置。US4172815 discloses a single-stage circulation hydrocracking method for simultaneously producing jet fuel and diesel oil, and the initial boiling point of the feedstock is greater than 500°F (about 260°C). The process flow is briefly described as follows: the feedstock oil undergoes hydrocracking, reacts under the reaction conditions of a pressure greater than 1000 psig (about 6.9Mpa), and the reaction effluent undergoes fractional distillation to obtain naphtha fraction, jet fuel fraction, diesel fraction and tail oil , jet fuel fractions are mixed with all or part of the tail oil and sent back to the cracking reaction zone. Under relatively moderate hydrocracking conditions, the method can achieve the purpose of simultaneously producing jet fuel and diesel in large quantities, and the quality of jet fuel is also improved. This method involves the idea of recycling jet fuel fractions to improve jet fuel quality, but recycling jet fuel fractions will increase energy consumption on the one hand, and increase the total space velocity of the reaction on the other hand, which has a negative impact on hydrocracking reactions; At the end of the operation of the hydrocracking unit, the catalyst performance is already lower than the initial stage, and the reaction temperature is high, so there is no room for adjustment. Therefore, the circulation of jet fuel fractions and the increase of space velocity may affect the overall hydrocracking effect, which may not be applicable to Existing hydrocracking unit.
CN1224678C公开了一种生产航煤的方法，重质原料先经加氢裂化后，分离加氢裂化反应生产物得到中间馏分油，该中间馏分油与轻质原料经加氢处理，分离加氢处理反应的反应生成物得到目的产物：航煤，新鲜氢气可补充到加氢裂化反应区和/或加氢处理反应区。该发明可在相对低的反应压力下，生产烟点、芳烃含量等指标均合格的航煤，但该工艺方法不能直接在加氢裂化装置上得到合格的航煤，仍需要与直馏煤油混合加氢精制。CN1224678C discloses a method for producing jet fuel. After the heavy raw material is hydrocracked first, the hydrocracking reaction product is separated to obtain middle distillate oil. The middle distillate oil and light raw material are hydrotreated, separated and hydrotreated The reaction product of the reaction is the target product: jet fuel, and fresh hydrogen can be added to the hydrocracking reaction zone and/or the hydroprocessing reaction zone. This invention can produce jet fuel with qualified indicators such as smoke point and aromatics content under relatively low reaction pressure, but this process method cannot directly obtain qualified jet fuel in the hydrocracking unit, and still needs to be mixed with straight-run kerosene Hydrofining.
申请号为00110437.3的现有技术公开了一种中压条件下生产航煤的方案，该中压加氢裂化过程所需的补充氢首先在加氢饱和催化剂及加氢饱和条件下经过一个航煤加氢饱和单元，然后再进入中压加氢裂化单元，所说的航煤加氢饱和的原料来自分馏塔馏出物航煤馏分中的一部分，航煤加氢饱和单元的流出物中，气体作为补充氢继续进入中压加氢裂化单元，液体产物直接进入上述分馏塔。该发明可在中压下，生产烟点、芳烃含量等指标均合格的航煤，但该工艺方法中需要增加一个航煤加氢饱和单元，在压力较高的反应区增加装置相对投资较大。The prior art with application number 00110437.3 discloses a scheme for producing jet fuel under medium pressure conditions. The supplementary hydrogen required for the medium pressure hydrocracking process first passes through a jet fuel under hydrogenation saturation catalyst and hydrogenation saturation conditions. The hydrogenation saturation unit then enters the medium-pressure hydrocracking unit. The raw material for the jet fuel saturation comes from a part of the fractionation tower distillate jet fuel fraction, and in the effluent of the jet coal hydrogenation saturation unit, the gas As make-up hydrogen continues to enter the medium-pressure hydrocracking unit, the liquid product directly enters the above-mentioned fractionation column. This invention can produce jet fuel with qualified indicators such as smoke point and aromatics content under medium pressure, but in this process, it is necessary to add a jet fuel hydrogenation saturation unit, and the relative investment of adding a device in the reaction zone with higher pressure is relatively large .
CN101280221A公开了一种劣质柴油馏分加氢转化方法，其核心内容在于设立了第二个航煤加氢精制反应区，且该区与原有的加氢裂化区域相隔离，对原有加氢裂化得到的航煤馏分进一步加氢精制得到合格产品。该发明可用于加工劣质的柴油馏分得到合格的航煤，但该工艺方法中需要增加一个航煤加氢饱和单元，在较高的反应区增加装置相对较难。CN101280221A discloses a method for hydrogenation conversion of low-quality diesel fractions, the core content of which is to set up a second jet fuel hydrotreating reaction zone, and this zone is isolated from the original hydrocracking zone, and the original hydrocracking The obtained jet fuel fraction is further hydrotreated to obtain qualified products. The invention can be used to process low-quality diesel fractions to obtain qualified jet fuel, but the process requires adding a jet fuel hydrogenation saturation unit, which is relatively difficult to add in a higher reaction zone.
总结目前的技术提高航煤的烟点主要包括以下两点：(1)循环航煤全馏分，对航煤馏分进一步加氢，从而提高航煤烟点；(2)设立第二加氢精制反应区，对航煤全馏分进行饱和精制，从而提高航煤烟点。Summarizing the current technology to improve the smoke point of aviation kerosene mainly includes the following two points: (1) recycle the whole fraction of jet kerosene, and further hydrogenate the fraction of jet kerosene, thereby improving the smoke point of jet kerosene; (2) set up a second hydrogenation refining reaction In the area, saturate and refine the whole distillate of aviation kerosene to increase the smoke point of aviation kerosene.
上述方案可以有效提高航煤质量，但也存在不足之处：(1)对航煤循环操作会增加额外的操作费用；此外，循环航煤将增加总空速，对反应系统有负面影响，尤其是在反应末期，催化剂活性大幅度下降，提高空速会系统影响相对较大；(2)设立第二反应区则需要增加额外的高压反应装置，投资较大。The above scheme can effectively improve the quality of aviation fuel, but there are also shortcomings: (1) additional operating costs will be added to the recycling operation of aviation fuel; in addition, circulating aviation fuel will increase the total airspeed, which will have a negative impact on the reaction system, especially Especially in the final stage of the reaction, the activity of the catalyst is greatly reduced, and increasing the space velocity will have a relatively large impact on the system; (2) the establishment of the second reaction zone requires an additional high-pressure reaction device, which requires a large investment.
发明内容Contents of the invention
本发明的目的是克服现有技术的缺陷，提供一种更经济、更灵活地改善航煤质量的加氢裂化方法。The purpose of the present invention is to overcome the defects of the prior art and provide a more economical and flexible hydrocracking method for improving the quality of jet fuel.
为了实现上述目的，本发明提供一种改善航煤质量的加氢裂化方法，该方法包括：In order to achieve the above object, the present invention provides a method for improving the hydrocracking of jet fuel quality, the method comprising:
1)将来自加氢裂化反应区的液相产物进行分馏，得到石脑油馏分、煤油馏分、柴油馏分和尾油馏分；1) Fractionating the liquid phase product from the hydrocracking reaction zone to obtain naphtha fractions, kerosene fractions, diesel fractions and tail oil fractions;
2)将步骤1)得到的煤油馏分引入煤油分馏塔进行分馏，得到轻质航煤馏分、中质航煤馏分和重质航煤馏分，抽出至少部分所述中质航煤馏分，以及将轻质航煤馏分、重质航煤馏分和任选的剩余部分的中质航煤馏分作为航煤产品出装置。2) introducing the kerosene fraction obtained in step 1) into a kerosene fractionation tower for fractionation to obtain a light jet kerosene fraction, a medium jet kerosene fraction and a heavy jet kerosene fraction, extracting at least part of the middle jet kerosene fraction, and extracting the light jet kerosene fraction The high-quality aviation kerosene fraction, the heavy aviation kerosene fraction and the optional remaining part of the medium-weight aviation kerosene fraction are output from the device as aviation kerosene products.
本发明提供的方法能够有效提高加氢裂化装置的航煤质量。与其它提高加氢裂化装置航煤质量的方法相比，抽出至少部分中质航煤馏分仅需对分馏系统中的航煤气提塔进行改造，改动较小，成本较低；另一方面，该方式操作费用较低，抽出量还可以根据装置的进料及其运转周期进行调整，相对更加灵活。The method provided by the invention can effectively improve the quality of jet fuel in a hydrocracking unit. Compared with other methods of improving the quality of jet fuel in hydrocracking units, extracting at least part of the medium-quality jet fuel fraction only needs to modify the jet fuel stripping tower in the fractionation system, which is less modified and less costly; on the other hand, the The operating cost of the method is low, and the pumping volume can be adjusted according to the feed material of the device and its operation cycle, which is relatively more flexible.
本发明的其它特征和优点将在随后的具体实施方式部分予以详细说明。Other features and advantages of the present invention will be described in detail in the detailed description that follows.
附图说明Description of drawings
附图是用来提供对本发明的进一步理解，并且构成说明书的一部分，与下面的具体实施方式一起用于解释本发明，但并不构成对本发明的限制。图中省略了许多设备，如泵、换热器、压缩机等，但这对本领域普通技术人员是公知的。在附图中：The accompanying drawings are used to provide a further understanding of the present invention, and constitute a part of the description, together with the following specific embodiments, are used to explain the present invention, but do not constitute a limitation to the present invention. Many devices are omitted in the figure, such as pumps, heat exchangers, compressors, etc., but are well known to those skilled in the art. In the attached picture:
图1是根据本发明的方法生产航煤的工艺流程示意图。Fig. 1 is the technological process schematic diagram of producing aviation kerosene according to the method of the present invention.
附图标记说明Explanation of reference signs
1、原料油 2、氢气1. Raw oil 2. Hydrogen
3、加氢裂化反应区 4、高压分离器3. Hydrocracking reaction zone 4. High pressure separator
5、低压分离器 6、第一分馏塔5. Low-pressure separator 6. The first fractionating column
7、石脑油馏分 8、煤油馏分7. Naphtha fraction 8. Kerosene fraction
9、柴油馏分 10、尾油馏分9. Diesel fraction 10. Tail oil fraction
11、煤油分馏塔 12、轻质航煤馏分11. Kerosene fractionation tower 12. Light jet fuel fraction
13、中质航煤馏分 14、重质航煤馏分13. Medium jet fuel fraction 14. Heavy jet fuel fraction
15、管线 16、航煤产品15. Pipeline 16. Jet fuel products
具体实施方式Detailed ways
以下对本发明的具体实施方式进行详细说明。应当理解的是，此处所描述的具体实施方式仅用于说明和解释本发明，并不用于限制本发明。Specific embodiments of the present invention will be described in detail below. It should be understood that the specific embodiments described here are only used to illustrate and explain the present invention, and are not intended to limit the present invention.
本发明提供了一种改善航煤质量的加氢裂化方法，该方法包括：The invention provides a hydrocracking method for improving the quality of aviation coal, the method comprising:
1)将来自加氢裂化反应区的液相产物进行分馏，得到石脑油馏分、煤油馏分、柴油馏分和尾油馏分；1) Fractionating the liquid phase product from the hydrocracking reaction zone to obtain naphtha fractions, kerosene fractions, diesel fractions and tail oil fractions;
2)将步骤1)得到的煤油馏分引入煤油分馏塔进行分馏，得到轻质航煤馏分、中质航煤馏分和重质航煤馏分，抽出至少部分所述中质航煤馏分，以及将轻质航煤馏分、重质航煤馏分和任选的剩余部分的中质航煤馏分作为航煤产品出装置。2) introducing the kerosene fraction obtained in step 1) into a kerosene fractionation tower for fractionation to obtain a light jet kerosene fraction, a medium jet kerosene fraction and a heavy jet kerosene fraction, extracting at least part of the middle jet kerosene fraction, and extracting the light jet kerosene fraction The high-quality aviation kerosene fraction, the heavy aviation kerosene fraction and the optional remaining part of the medium-weight aviation kerosene fraction are output from the device as aviation kerosene products.
在本发明中，所述加氢裂化反应区是指原料油能够在此进行加氢裂化反应的区域，在该区域中原料油与含氢物流发生加氢饱和、脱杂质以及裂化反应。In the present invention, the hydrocracking reaction zone refers to the area where the feedstock oil can undergo hydrocracking reaction, and in this zone, the feedstock oil and the hydrogen-containing stream undergo hydrogenation saturation, impurity removal and cracking reactions.
在本发明中，所述“将轻质航煤馏分、重质航煤馏分和任选的剩余部分的中质航煤馏分作为航煤产品出装置”是指，出装置的航煤产品中可以含有或者不含有所述中质航煤馏分，当抽出的中质航煤馏分为全部的中质航煤馏分时，则剩余部分的中质航煤馏分为零，此时，航煤产品中不含有中质航煤馏分，若抽出的中质航煤馏分为部分的中质航煤馏分时，则航煤产品中含有剩余部分的中质航煤馏分。In the present invention, the "light jet kerosene fraction, heavy jet kerosene fraction and the optional remaining part of the medium jet kerosene fraction are taken out of the device as jet kerosene products" means that the jet kerosene products that go out of the device can be Contain or do not contain the medium jet kerosene fraction, when the extracted medium jet kerosene fraction is all the medium jet kerosene fraction, then the remaining part of the medium jet kerosene fraction is zero, at this time, there is no Contains medium jet kerosene fraction. If the extracted medium jet kerosene fraction is part of the medium jet kerosene fraction, the jet fuel product contains the remaining part of the medium jet kerosene fraction.
本发明提供的上述加氢裂化方法能够显著改善生产得到的航煤的质量。与其它提高加氢裂化装置航煤质量的方法相比，抽出至少部分中质航煤馏分仅需对分馏系统中的航煤气提塔进行改造，改动较小，成本较低；另一方面，该方式操作费用较低，抽出量还可以根据装置的进料及其运转周期进行调整，相对更加灵活。The above hydrocracking method provided by the present invention can significantly improve the quality of the produced jet fuel. Compared with other methods of improving the quality of jet fuel in hydrocracking units, extracting at least part of the medium-quality jet fuel fraction only needs to modify the jet fuel stripping tower in the fractionation system, which is less modified and less costly; on the other hand, the The operating cost of the method is low, and the pumping volume can be adjusted according to the feed material of the device and its operation cycle, which is relatively more flexible.
在本发明中，优选所述轻质航煤馏分和所述中质航煤馏分的切割点为190-210℃，所述中质航煤馏分和所述重质航煤馏分的切割点为230-240℃。更加优选所述轻质航煤馏分和所述中质航煤馏分的切割点为195-205℃，所述中质航煤馏分和所述重质航煤馏分的切割点为232-238℃。In the present invention, preferably, the cut point of the light jet kerosene fraction and the medium jet kerosene fraction is 190-210° C., and the cut point of the medium jet kerosene fraction and the heavy jet kerosene fraction is 230° C. -240°C. More preferably, the cut point of the light jet kerosene fraction and the medium jet kerosene fraction is 195-205°C, and the cut point of the medium jet kerosene fraction and the heavy jet kerosene fraction is 232-238°C.
根据本发明的一种优选的具体实施方式，所述轻质航煤馏分和所述中质航煤馏分的切割点为200℃，所述中质航煤馏分和所述重质航煤馏分的切割点为235℃。According to a preferred embodiment of the present invention, the cut point of the light jet kerosene fraction and the medium jet kerosene fraction is 200°C, and the cut point of the medium jet kerosene fraction and the heavy jet kerosene fraction The cut point is 235°C.
在本发明中，优选所述石脑油馏分和所述煤油馏分的切割点为130℃；所述煤油馏分和所述柴油馏分的切割点为290℃；所述柴油馏分和所述尾油馏分的切割点为320℃。更加优选情况下，在本发明中，所述石脑油馏分和所述煤油馏分的切割点为145℃；所述煤油馏分和所述柴油馏分的切割点为270℃；所述柴油馏分和所述尾油馏分的切割点为320℃。In the present invention, preferably the cut point of the naphtha fraction and the kerosene fraction is 130°C; the cut point of the kerosene fraction and the diesel fraction is 290°C; the diesel fraction and the tail oil fraction The cut point is 320°C. More preferably, in the present invention, the cut point of the naphtha fraction and the kerosene fraction is 145°C; the cut point of the kerosene fraction and the diesel fraction is 270°C; The cut point of the tail oil fraction is 320°C.
本发明所述的方法包括将加氢裂化反应区生成的气液混合物料进行气液分离，得到气相产物和液相产物，所述气相产物经过后续加工后可以引入反应系统中进行循环，所述液相产物进入分馏塔(为了区分，本发明在后文中也称该处的分馏塔为第一分馏塔)中进行分馏，得到石脑油馏分、煤油馏分、柴油馏分和尾油馏分。其中，本发明所述的分离可以在分离器中进行，所述分离器包括高压分离器和/或低压分离器。The method of the present invention includes separating the gas-liquid mixture generated in the hydrocracking reaction zone to obtain gas-phase products and liquid-phase products, and the gas-phase products can be introduced into the reaction system for circulation after subsequent processing. The liquid phase product enters fractionation tower (in order to distinguish, the present invention also claims that the fractionation tower at this place is the first fractionation tower hereinafter) and carries out fractionation, obtains naphtha fraction, kerosene fraction, diesel oil fraction and tail oil fraction. Wherein, the separation described in the present invention can be performed in a separator, and the separator includes a high-pressure separator and/or a low-pressure separator.
在本发明中，对所述高压分离器、低压分离器、第一分馏塔和煤油分馏塔中的操作条件没有特别的限定，本领域技术人员在了解了本发明的技术方案后能够根据本领域内的常规技术手段选择合适的操作条件以进行分离和分馏。本发明在此不再详述。In the present invention, the operating conditions in the high-pressure separator, the low-pressure separator, the first fractionation tower and the kerosene fractionation tower are not particularly limited, and those skilled in the art can understand the technical scheme of the present invention according to the technical scheme of the present invention. Suitable operating conditions are selected for separation and fractionation by conventional technical means within. The present invention will not be described in detail here.
在本发明中，为了更加显著地改善生产得到的航煤的质量，优选所述轻质航煤馏分的馏程为145-200℃，所述中质航煤馏分的馏程为高于200℃且低于235℃，所述重质航煤馏分的馏程为235-270℃。In the present invention, in order to more significantly improve the quality of the jet kerosene produced, preferably the distillation range of the light jet kerosene fraction is 145-200°C, and the distillation range of the medium jet kerosene fraction is higher than 200°C And lower than 235°C, the distillation range of the heavy jet fuel fraction is 235-270°C.
在本发明所述的方法中，优选抽出的所述中质航煤馏分与出装置的航煤产品的重量比为0.1-0.9：1。本发明的发明人发现，当抽出的所述中质航煤馏分与出装置的航煤产品的重量比为0.1-0.9：1时，获得的航煤的烟点高。In the method of the present invention, preferably, the weight ratio of the extracted medium jet fuel fraction to the jet fuel product out of the device is 0.1-0.9:1. The inventors of the present invention found that when the weight ratio of the extracted medium jet kerosene fraction to the jet kerosene product out of the device is 0.1-0.9:1, the smoke point of the jet kerosene obtained is high.
在本发明所述的方法中，特别优选抽出的所述中质航煤馏分与出装置的航煤产品的重量比为0.18-0.44：1。本发明的发明人发现，当抽出的所述中质航煤馏分与出装置的航煤产品的重量比为0.18-0.44：1时，获得的航煤的烟点能够达到最优。In the method of the present invention, it is particularly preferred that the weight ratio of the extracted medium jet fuel fraction to the jet fuel product out of the device is 0.18-0.44:1. The inventors of the present invention found that when the weight ratio of the extracted medium jet kerosene fraction to the jet kerosene product out of the device is 0.18-0.44:1, the smoke point of the jet kerosene obtained can be optimized.
根据本发明，按照反应物流的流向，优选所述加氢裂化反应区中依次设置含有加氢预处理催化剂的加氢预处理单元、含有加氢裂化催化剂的加氢裂化单元和含有后精制催化剂的后精制单元。According to the present invention, according to the flow direction of the reactant stream, preferably, the hydrocracking reaction zone is sequentially provided with a hydrocracking unit containing a hydrocracking catalyst, a hydrocracking unit containing a hydrocracking catalyst, and a post-refining catalyst. post-refining unit.
在本发明中，所述加氢预处理单元、所述加氢裂化单元和所述后精制单元可以是不同的反应器，也可以是同一反应器中的不同床层或同一床层的不同区域。In the present invention, the hydropretreatment unit, the hydrocracking unit and the post-refining unit may be different reactors, or different beds in the same reactor or different regions of the same bed .
在本发明中，优选本发明的该方法包括将原料油和含氢物流引入加氢裂化反应区中依次与所述加氢预处理催化剂、所述加氢裂化催化剂和所述后精制催化剂进行接触反应。In the present invention, it is preferred that the method of the present invention comprises introducing feedstock oil and a hydrogen-containing stream into a hydrocracking reaction zone to successively contact the hydrotreating catalyst, the hydrocracking catalyst and the post-refining catalyst reaction.
在本发明中，所述含氢物流是指能够提供氢气的物流，包括新氢、循环氢、富氢气体和其它能够提供氢气的气相物流以及其它能够提供氢气的液相物流中的任意一种或多种。本领域技术人员在了解了本发明的技术方案之后能够清楚地理解本发明中所述的含氢物流。In the present invention, the hydrogen-containing stream refers to a stream that can provide hydrogen, including any one of new hydrogen, recycled hydrogen, hydrogen-rich gas, other gas-phase streams that can provide hydrogen, and other liquid-phase streams that can provide hydrogen or more. Those skilled in the art can clearly understand the hydrogen-containing stream described in the present invention after understanding the technical solution of the present invention.
根据本发明所述的方法，对所述加氢裂化反应区的反应条件没有特别的限定，本发明的方法适应本领域内常规的各种加氢裂化条件，本领域技术人员在了解了本发明的方案之后能够选择合适的条件来进行本发明的方法。但是本发明的发明人发现，当控制所述加氢裂化反应区的反应条件在如下范围内时，生产得到的航煤的烟点更高。所述加氢裂化反应区的反应条件包括：反应温度为300-450℃，氢分压为2.0-18.0MPa，氢油体积比为300-2000：1，体积空速为0.5-20h-1。According to the method of the present invention, the reaction conditions of the hydrocracking reaction zone are not particularly limited. The method of the present invention is suitable for various conventional hydrocracking conditions in the field. Those skilled in the art will understand the present invention Appropriate conditions can then be selected to carry out the method of the present invention. However, the inventors of the present invention found that when the reaction conditions in the hydrocracking reaction zone are controlled within the following ranges, the smoke point of the produced jet fuel is higher. The reaction conditions of the hydrocracking reaction zone include: a reaction temperature of 300-450°C, a hydrogen partial pressure of 2.0-18.0MPa, a hydrogen-to-oil volume ratio of 300-2000:1, and a volume space velocity of 0.5-20h -1 .
更加优选情况下，在本发明中，所述加氢裂化反应区的反应条件包括：氢分压为10.0-18.0MPa。More preferably, in the present invention, the reaction conditions in the hydrocracking reaction zone include: the hydrogen partial pressure is 10.0-18.0 MPa.
本发明的方法对所述加氢预处理催化剂、加氢裂化催化剂和后精制催化剂的种类以及装填体积比没有特别的限定，本领域技术人员在了解了本发明的技术方案之后能够根据本领域内常规使用的加氢预处理催化剂、加氢裂化催化剂和后精制催化剂的种类以及装填体积比进行选择，采用常规的各种加氢预处理催化剂、加氢裂化催化剂和后精制催化剂就能够实现本发明前述的发明目的。The method of the present invention has no special limitation to the type and loading volume ratio of the hydropretreatment catalyst, hydrocracking catalyst and post-refining catalyst. The conventionally used hydrogenation pretreatment catalyst, hydrocracking catalyst and post-refining catalyst are selected, and the present invention can be realized by adopting conventional various hydroprocessing catalysts, hydrocracking catalysts and post-refining catalysts Aforesaid purpose of the invention.
优选情况下，本发明的发明人发现采用以下加氢裂化催化剂时，获得的航煤的烟点更高，所述加氢裂化催化剂中含有选自氧化铝、无定形硅铝和沸石中的至少一种的载体以及负载在所述载体上的活性组分元素；所述活性组分元素包括贵金属元素和/或非贵金属元素；所述非贵金属元素为VIB族金属元素和/或VIII族金属元素；Preferably, the inventors of the present invention have found that the smoke point of jet fuel obtained is higher when using a hydrocracking catalyst containing at least A carrier and the active component elements loaded on the carrier; the active component elements include noble metal elements and/or non-noble metal elements; the non-noble metal elements are VIB group metal elements and/or VIII group metal elements ;
优选所述VIB族金属元素为Mo和/或W，所述VIII族金属元素为Co和/或Ni；所述贵金属元素为Pt元素和/或Pd元素。Preferably, the VIB group metal element is Mo and/or W, the VIII group metal element is Co and/or Ni; the noble metal element is Pt element and/or Pd element.
在本发明中，所述无定形硅铝包括氧化硅、氧化铝或它们的组合。In the present invention, the amorphous silica-alumina includes silicon oxide, aluminum oxide or a combination thereof.
优选情况下，在本发明中，所述加氢裂化反应区中的后精制催化剂包括载体和负载在所述载体上的活性金属，所述载体包括无定形氧化铝和/或硅铝；所述活性金属包括第VIB族非贵金属和第VIII族非贵金属中的至少一种。根据本发明所述的方法，所述载体可以包括无定形氧化铝和/或硅铝，常用的载体也可以为γ-Al2O3。所述活性金属可以包括第VIB族非贵金属和第VIII族非贵金属中的至少一种，常用的活性金属可以包括Mo、W、Co和Ni中的至少一种。Preferably, in the present invention, the post-refining catalyst in the hydrocracking reaction zone includes a carrier and an active metal supported on the carrier, and the carrier includes amorphous alumina and/or silica-alumina; the The active metal includes at least one of a Group VIB non-noble metal and a Group VIII non-noble metal. According to the method of the present invention, the support may include amorphous alumina and/or silica-alumina, and the commonly used support may also be γ-Al 2 O 3 . The active metal may include at least one of Group VIB non-noble metals and Group VIII non-noble metals, and commonly used active metals may include at least one of Mo, W, Co and Ni.
根据本发明，优选所述加氢预处理催化剂包括载体和负载在所述载体上的活性金属元素，所述载体包括无定形氧化铝和/或硅铝；所述活性金属元素包括第VIB族金属元素和第VIII族金属元素中的至少一种。更加优选情况下，在本发明所述的后精制催化剂中，所述VIB族金属元素为Mo和/或W，所述VIII族金属元素为Co和/或Ni。According to the present invention, it is preferred that the hydrogenation pretreatment catalyst includes a carrier and an active metal element loaded on the carrier, the carrier includes amorphous alumina and/or silica-alumina; the active metal element includes a Group VIB metal element and at least one of a Group VIII metal element. More preferably, in the post-refining catalyst of the present invention, the VIB group metal element is Mo and/or W, and the VIII group metal element is Co and/or Ni.
在本发明中，所述加氢裂化反应区中可以包括一个或多个反应器，每个反应器可以包括一个或多个催化剂床层，各个所述催化剂床层可以装填相同或者不同种类的催化剂。In the present invention, one or more reactors may be included in the hydrocracking reaction zone, and each reactor may include one or more catalyst beds, each of which may be filled with the same or different types of catalysts .
在本发明中，优选所述原料油的馏程为180-635℃；原料油中硫含量≤50000μg/g，氮含量≤5000μg/g。In the present invention, preferably, the distillation range of the raw oil is 180-635° C.; the sulfur content in the raw oil is ≤50000 μg/g, and the nitrogen content is ≤5000 μg/g.
在本发明中，更加优选所述原料油中硫含量≤40000μg/g、氮含量≤2000μg/g。In the present invention, it is more preferable that the sulfur content in the raw oil is ≤40000 μg/g, and the nitrogen content is ≤2000 μg/g.
在本发明中，所述原料油可以包括减压蜡油、焦化蜡油、催化裂化轻循环油、脱沥青油和煤制取油中的至少一种。In the present invention, the raw oil may include at least one of vacuum gas oil, coker gas oil, catalytic cracking light cycle oil, deasphalted oil and coal-derived oil.
根据本发明的一种优选的具体实施方式，本发明的方法在如图1所示的工艺流程示意图中进行，具体地如下：According to a preferred embodiment of the present invention, the method of the present invention is carried out in the schematic process flow diagram as shown in Figure 1, specifically as follows:
来自管线的原料油1与来自管线的氢气2混合后，进入加氢裂化反应区3，在加氢预处理催化剂、加氢裂化催化剂和后精制催化剂的作用下进行反应，其反应流出物进入高压分离器4进行气液分离，高压分离器4底部的液相物流进入低压分离器5，在此进行进一步的气液分离；低压分离器5底部的液相产物进入第一分馏塔6。进入第一分馏塔6的液相产物经分馏后，切割成石脑油馏分7、煤油馏分8、柴油馏分9和尾油馏分10依次经管线抽出。煤油馏分8再进入煤油分馏塔11，分馏得到轻质航煤馏分12、中质航煤馏分13和重质航煤馏分14。至少部分中质航煤馏分经管线15抽出，而轻质航煤馏分、重质航煤馏分和任选的剩余部分的中质航煤馏分混合后形成航煤产品16出装置。After the raw oil 1 from the pipeline is mixed with the hydrogen gas 2 from the pipeline, it enters the hydrocracking reaction zone 3, and reacts under the action of the hydrogenation pretreatment catalyst, hydrocracking catalyst and post-refining catalyst, and the reaction effluent enters the high-pressure Separator 4 performs gas-liquid separation, and the liquid phase stream at the bottom of high-pressure separator 4 enters low-pressure separator 5, where further gas-liquid separation is performed; the liquid-phase product at the bottom of low-pressure separator 5 enters first fractionation tower 6. After being fractionated, the liquid phase product entering the first fractionating tower 6 is cut into a naphtha fraction 7, a kerosene fraction 8, a diesel fraction 9 and a tail oil fraction 10, which are sequentially drawn out through pipelines. The kerosene fraction 8 then enters the kerosene fractionation tower 11 for fractionation to obtain a light aviation kerosene fraction 12 , a medium aviation kerosene fraction 13 and a heavy aviation kerosene fraction 14 . At least part of the medium jet kerosene fraction is extracted through the pipeline 15, and the light jet kerosene fraction, the heavy jet kerosene fraction and the optional remaining part of the medium jet kerosene fraction are mixed to form the jet kerosene product 16 out of the device.
具体地，本发明的所述方法还包括如下具体的优点：Specifically, the method of the present invention also includes the following specific advantages:
1、采用本发明提供的方法，能够在不改动反应系统的条件下有效提高航煤的烟点；1. By adopting the method provided by the invention, the smoke point of jet fuel can be effectively improved without changing the reaction system;
2、与现有技术的增加第二加氢精制反应区从而改善航煤烟点的方式相比，本发明的方法设备投入及操作费用更少；2. Compared with the method of increasing the second hydrorefining reaction zone of the prior art to improve the smoke point of aviation fuel, the method of the present invention has less equipment input and operating costs;
3、与现有技术的循环回炼全馏分航煤从而提高航煤烟点的方式相比，本发明的操作费用更低；3. Compared with the method of circulating and refining the whole distillate jet fuel in the prior art to improve the smoke point of jet fuel, the operating cost of the present invention is lower;
4、本发明的方法能够用于加氢裂化装置末期航煤质量调整，在催化剂活性下降的情况下，通过对煤油馏分的适当切割并选择性抽出中质航煤馏分从而改善航煤质量，达到生产合格航煤的目标。4. The method of the present invention can be used to adjust the quality of jet fuel at the end of the hydrocracking unit. When the catalyst activity decreases, the quality of jet fuel can be improved by properly cutting the kerosene fraction and selectively extracting the mid-quality jet fuel fraction to achieve The goal of producing qualified jet fuel.
以下将通过实施例对本发明进行详细描述。The present invention will be described in detail below by way of examples.
以下实施例和对比例中，在没有特别说明的情况下，所使用的各种原料均来自商购。In the following examples and comparative examples, unless otherwise specified, all raw materials used are commercially available.
在以下实施例和对比例中，所使用的加氢预处理催化剂为RN-32V；加氢裂化催化剂为RHC-3，后精制催化剂为RN-32V，以上催化剂均由中国石化股份有限公司催化剂长岭分公司生产。所使用的原料油其性质如表1所示。In the following examples and comparative examples, the hydrogenation pretreatment catalyst used is RN-32V; the hydrocracking catalyst is RHC-3, and the post-refining catalyst is RN-32V. The above catalysts are all provided by Sinopec Catalyst Director Manufactured by Ridge Company. The properties of the raw oil used are shown in Table 1.
实施例1Example 1
将原料油与氢气引入含有加氢预处理催化剂、加氢裂化催化剂和后精制催化剂的加氢裂化反应区中进行反应，反应条件如表2所示；然后将该加氢裂化反应器的反应流出物依次引入高压分离器和低压分离器进行气液分离，得到液相产物，并且将该液相产物引入第一分馏塔中进行分馏，得到石脑油馏分、煤油馏分、柴油馏分和尾油馏分(所述石脑油馏分和所述煤油馏分的切割点为145℃；所述煤油馏分和所述柴油馏分的切割点为270℃；所述柴油馏分和所述尾油馏分的切割点为320℃，下同)。将获得的煤油馏分引入煤油分馏塔中进行进一步分馏，得到轻质航煤馏分、中质航煤馏分和重质航煤馏分(所述轻质航煤馏分和所述中质航煤馏分的切割点为200℃，所述中质航煤馏分和所述重质航煤馏分的切割点为235℃，下同)，抽出部分中质航煤馏分，而轻质航煤馏分、重质航煤馏分和剩余部分的中质航煤馏分混合后形成航煤产品出装置。其中，抽出部分中质航煤馏分与航煤产品的重量比为0.21：1.0。产品石脑油馏分、产品柴油馏分和产品尾油馏分的收率分别如表3中所示，且航煤产品的性质如表4中所示。Feed oil and hydrogen are introduced into the hydrocracking reaction zone containing hydroprocessing pretreatment catalyst, hydrocracking catalyst and post-refining catalyst to react, the reaction conditions are as shown in Table 2; then the reaction flow out of the hydrocracking reactor The product is sequentially introduced into a high-pressure separator and a low-pressure separator for gas-liquid separation to obtain a liquid phase product, and the liquid phase product is introduced into the first fractionation tower for fractionation to obtain naphtha fraction, kerosene fraction, diesel fraction and tail oil fraction (the cut point of the naphtha fraction and the kerosene fraction is 145° C.; the cut point of the kerosene fraction and the diesel fraction is 270° C.; the cut point of the diesel fraction and the tail oil fraction is 320° C. ℃, the same below). The kerosene fraction obtained is introduced into a kerosene fractionation tower for further fractionation to obtain a light jet kerosene fraction, a medium jet kerosene cut and a heavy jet kerosene cut (cutting of the light jet kerosene fraction and the middle jet kerosene fraction point is 200°C, the cut point of the medium jet kerosene fraction and the heavy jet kerosene fraction is 235°C, the same below), part of the medium jet kerosene fraction is extracted, and the light jet kerosene fraction, heavy jet kerosene fraction After the distillate is mixed with the remaining medium jet fuel distillate, the jet fuel product is output from the device. Among them, the weight ratio of the extracted part of the medium jet kerosene fraction to the jet kerosene product is 0.21:1.0. The yields of the product naphtha fraction, the product diesel fraction and the product tail oil fraction are shown in Table 3, and the properties of the jet fuel product are shown in Table 4.
表1Table 1
表2Table 2
表3table 3
表4Table 4
实施例2Example 2
将原料油与氢气引入含有加氢裂化催化剂和后精制催化剂的加氢裂化反应器中进行反应，反应条件如表2所示；然后将该加氢裂化反应器的反应流出物依次引入高压分离器和低压分离器进行气液分离，得到液相产物，并且将该液相产物引入第一分馏塔中进行分馏，得到石脑油馏分、煤油馏分、柴油馏分和尾油馏分。将获得的煤油馏分引入煤油分馏塔中进行进一步分馏，得到轻质航煤馏分、中质航煤馏分和重质航煤馏分，抽出全部中质航煤馏分，而轻质航煤馏分和重质航煤馏分混合后形成航煤产品出装置。其中，抽出的中质航煤馏分与航煤产品的重量比为0.44：1.0，产品石脑油馏分、产品柴油馏分和产品尾油馏分的收率分别如表3中所示，且航煤产品的性质如表4中所示。The raw oil and hydrogen are introduced into the hydrocracking reactor containing the hydrocracking catalyst and the post-refining catalyst for reaction, and the reaction conditions are shown in Table 2; then the reaction effluent of the hydrocracking reactor is sequentially introduced into the high-pressure separator Perform gas-liquid separation with a low-pressure separator to obtain liquid phase products, and introduce the liquid phase products into the first fractionation tower for fractionation to obtain naphtha fractions, kerosene fractions, diesel fractions and tail oil fractions. The obtained kerosene fraction is introduced into the kerosene fractionation tower for further fractionation to obtain light jet kerosene fraction, medium jet kerosene fraction and heavy jet kerosene fraction. Jet kerosene fractions are mixed to form jet kerosene products out of the device. Among them, the weight ratio of the extracted medium jet kerosene fraction to the jet kerosene product is 0.44:1.0, the yields of the product naphtha fraction, the product diesel fraction and the product tail oil fraction are shown in Table 3, and the jet kerosene product The properties are shown in Table 4.
对比例1Comparative example 1
将原料油与氢气引入含有加氢预处理催化剂、裂化催化剂和后精制催化剂的加氢裂化反应区中进行反应，反应条件与实施例1中相同；然后将该加氢裂化反应器的反应流出物依次引入高压分离器和低压分离器进行气液分离，得到液相产物，并且将该液相产物引入第一分馏塔中进行分馏，得到石脑油馏分、煤油馏分、柴油馏分和尾油馏分。将获得的煤油馏分直接作为航煤产品出装置，产品石脑油馏分、产品柴油馏分和产品尾油馏分的收率分别如表3中所示，航煤产品的性质如表4中所示。The raw oil and hydrogen are introduced into the hydrocracking reaction zone containing the hydroprocessing pretreatment catalyst, the cracking catalyst and the post-refining catalyst for reaction, and the reaction conditions are the same as in Example 1; then the reaction effluent from the hydrocracking reactor is Sequentially introduce a high-pressure separator and a low-pressure separator for gas-liquid separation to obtain liquid phase products, and introduce the liquid phase products into the first fractionation tower for fractionation to obtain naphtha fractions, kerosene fractions, diesel fractions and tail oil fractions. The obtained kerosene fraction is directly taken out of the device as a jet kerosene product. The yields of the product naphtha fraction, product diesel fraction and product tail oil fraction are shown in Table 3, and the properties of the jet kerosene product are shown in Table 4.
对比例2Comparative example 2
将原料油与氢气引入含有加氢预处理催化剂、加氢裂化催化剂和后精制催化剂的加氢裂化反应器中进行反应，反应条件与实施例2中相同(如表2所示)；然后将该加氢裂化反应器的反应流出物依次引入高压分离器和低压分离器进行气液分离，得到液相产物，并且将该液相产物引入第一分馏塔中进行分馏，得到石脑油馏分、煤油馏分、柴油馏分和尾油馏分。将获得的煤油馏分引入煤油分馏塔中进行进一步分馏，得到轻质航煤馏分、中质航煤馏分和重质航煤馏分，抽出全部轻质航煤馏分，而中质航煤馏分和重质航煤馏分混合后形成航煤产品出装置。其中，抽出的轻质航煤馏分与航煤产品的重量比为0.74：1.0，产品石脑油馏分、产品柴油馏分和产品尾油馏分的收率分别如表3中所示，且航煤产品的性质如表4中所示。Feed oil and hydrogen are introduced into the hydrocracking reactor containing hydropretreatment catalyst, hydrocracking catalyst and post-refining catalyst to react, and the reaction conditions are the same as in Example 2 (as shown in Table 2); then the The reaction effluent of the hydrocracking reactor is sequentially introduced into a high-pressure separator and a low-pressure separator for gas-liquid separation to obtain a liquid phase product, and the liquid phase product is introduced into the first fractionation tower for fractionation to obtain naphtha fraction, kerosene fraction Distillate, Diesel Distillate and Tail Oil Distillate. The obtained kerosene fraction is introduced into the kerosene fractionation tower for further fractionation to obtain light jet kerosene fraction, medium jet kerosene fraction and heavy jet kerosene fraction. Jet kerosene fractions are mixed to form jet kerosene products out of the device. Among them, the weight ratio of extracted light aviation kerosene fraction to aviation kerosene product is 0.74:1.0, and the yields of product naphtha fraction, product diesel fraction and product tail oil fraction are shown in Table 3, and aviation kerosene product The properties are shown in Table 4.
对比例3Comparative example 3
将原料油与氢气引入含有加氢预处理催化剂、加氢裂化催化剂和后精制催化剂的加氢裂化反应器中进行反应，反应条件与实施例2相同(如表2所示)；然后将该加氢裂化反应器的反应流出物依次引入高压分离器和低压分离器进行气液分离，得到液相产物，并且将该液相产物引入第一分馏塔中进行分馏，得到石脑油馏分、煤油馏分、柴油馏分和尾油馏分。将获得的煤油馏分引入煤油分馏塔中进行进一步分馏，得到轻质航煤馏分、中质航煤馏分和重质航煤馏分，抽出全部重质航煤馏分，而轻质航煤馏分和中质航煤馏分混合后形成航煤产品出装置。其中，抽出的重质航煤馏分与航煤产品的重量比为0.38：1.0，产品石脑油馏分、产品柴油馏分和产品尾油馏分的收率分别如表3中所示，且航煤产品的性质如表4中所示。Feedstock oil and hydrogen are introduced into the hydrocracking reactor that contains hydrogenation pretreatment catalyst, hydrocracking catalyst and post-refining catalyst to react, and reaction conditions are identical with embodiment 2 (as shown in table 2); The reaction effluent from the hydrocracking reactor is sequentially introduced into a high-pressure separator and a low-pressure separator for gas-liquid separation to obtain a liquid phase product, and the liquid phase product is introduced into the first fractionation tower for fractionation to obtain naphtha fraction and kerosene fraction , diesel fraction and tail oil fraction. The obtained kerosene fraction is introduced into the kerosene fractionation tower for further fractionation to obtain light jet kerosene fraction, medium jet kerosene fraction and heavy jet kerosene fraction, and all heavy jet kerosene fractions are extracted, while light jet kerosene fraction and Jet kerosene fractions are mixed to form jet kerosene products out of the device. Among them, the weight ratio of extracted heavy aviation kerosene fraction to aviation kerosene product is 0.38:1.0, and the yields of product naphtha fraction, product diesel fraction and product tail oil fraction are shown in Table 3, and aviation kerosene product The properties are shown in Table 4.
由实施例1和对比例1的结果可知，在采用相同原料、相同催化剂及相同反应条件下，通过抽出部分中质航煤馏分，剩余航煤馏分作为产品航煤出装置可以有效地提高航煤的烟点。由表2-3的结果可知，与对比例中的全馏分航煤相比，当抽出部分中质航煤馏分与航煤产品的重量比为0.21：1时，产品航煤烟点可以提高一个单位。From the results of Example 1 and Comparative Example 1, it can be seen that under the same raw material, the same catalyst and the same reaction conditions, by extracting part of the middle jet kerosene cut, the remaining jet kerosene cut can effectively increase the jet kerosene output as a product jet kerosene outlet device. smoke point. From the results in Table 2-3, it can be known that, compared with the full-distillation jet kerosene in the comparative example, when the weight ratio of part of the extracted medium jet kerosene fraction to the jet kerosene product is 0.21:1, the smoke point of the product jet kerosene can be increased by one unit.
由实施例2与对比例2的结果可知，在采用相同原料、相同催化剂及相同反应条件下，通过全部抽出中质航煤馏分，而不是抽出轻质航煤馏分，可以有效地提高航煤的烟点。由表2-3可知，与对比例2中的抽出轻质航煤馏分后得到的产品馏分航煤相比，抽出全部中质航煤馏分得到产品航煤馏分的烟点可以提高2.3个单位。From the results of Example 2 and Comparative Example 2, it can be seen that under the same raw material, the same catalyst and the same reaction conditions, by all extracting the medium jet kerosene fraction instead of extracting the light jet kerosene fraction, the jet kerosene can be effectively improved. smoke point. It can be seen from Table 2-3 that, compared with the jet kerosene product fraction obtained after extracting the light jet kerosene fraction in Comparative Example 2, the smoke point of the product jet kerosene fraction obtained by extracting all the medium jet kerosene fractions can be increased by 2.3 units.
由实施例2与对比例3的结果可知，在采用相同原料、相同催化剂及相同反应条件下，通过全部抽出中质航煤馏分，而不是抽出重质航煤馏分，可以有效地提高航煤的烟点。由表2-3可知，与对比例3中的抽出重质航煤馏分后得到的产品馏分航煤相比，抽出全部中质航煤馏分得到产品航煤馏分的烟点可以提高1.6个单位。From the results of Example 2 and Comparative Example 3, it can be seen that under the same raw material, the same catalyst and the same reaction conditions, by all extracting the medium jet kerosene fraction instead of extracting the heavy jet kerosene fraction, the jet kerosene can be effectively improved. smoke point. It can be seen from Table 2-3 that, compared with the jet kerosene product fraction obtained after extracting the heavy jet kerosene fraction in Comparative Example 3, the smoke point of the product jet kerosene fraction obtained by extracting all the medium jet kerosene fractions can be increased by 1.6 units.
另外，对比实施例1和实施例2的结果还可以看出，提高中质航煤的抽出量，可以进一步改善航煤的烟点。由表2-3可知，当抽出中质航煤馏分与航煤产品的重量比由0.21：1提高到0.44：1(此时抽出了全部中质航煤馏分)时，航煤的烟点能进一步增加一个单位。In addition, comparing the results of Example 1 and Example 2, it can also be seen that increasing the extraction amount of medium-quality aviation kerosene can further improve the smoke point of the aviation kerosene. It can be seen from Table 2-3 that when the weight ratio of the extracted medium jet kerosene fraction to the jet kerosene product is increased from 0.21:1 to 0.44:1 (at this time all the medium jet kerosene fraction is extracted), the smoke point energy of jet kerosene Go one more unit further.
通过对比可以看出：本发明的方法能够有效提高航煤的烟点(烟点均大于等于26.0mm)，而且，相对于现有技术，本发明的方法仅需对分馏系统中的航煤气提塔进行改造，改动较小，成本较低；另一方面，该方式操作费用较低，抽出量还可以根据装置的进料及其运转周期进行调整，相对更加灵活。Can find out by comparison: the method of the present invention can effectively improve the smoke point of aviation coal (smoke point is all greater than or equal to 26.0mm), and, with respect to prior art, method of the present invention only needs to lift the aviation coal gas in the fractionation system. The transformation of the tower requires minor changes and lower cost; on the other hand, the operation cost of this method is lower, and the extraction volume can be adjusted according to the feed material of the device and its operation cycle, which is relatively more flexible.
以上详细描述了本发明的优选实施方式，但是，本发明并不限于上述实施方式中的具体细节，在本发明的技术构思范围内，可以对本发明的技术方案进行多种简单变型，这些简单变型均属于本发明的保护范围。The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited to the specific details in the above embodiments. Within the scope of the technical concept of the present invention, various simple modifications can be made to the technical solutions of the present invention. These simple modifications All belong to the protection scope of the present invention.
另外需要说明的是，在上述具体实施方式中所描述的各个具体技术特征，在不矛盾的情况下，可以通过任何合适的方式进行组合，为了避免不必要的重复，本发明对各种可能的组合方式不再另行说明。In addition, it should be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable way if there is no contradiction. The combination method will not be described separately.
此外，本发明的各种不同的实施方式之间也可以进行任意组合，只要其不违背本发明的思想，其同样应当视为本发明所公开的内容。In addition, various combinations of different embodiments of the present invention can also be combined arbitrarily, as long as they do not violate the idea of the present invention, they should also be regarded as the disclosed content of the present invention.
Claims (11)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510578869.9A CN106520195B (en) | 2015-09-11 | 2015-09-11 | A kind of method for hydrogen cracking for improving boat coal quality |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510578869.9A CN106520195B (en) | 2015-09-11 | 2015-09-11 | A kind of method for hydrogen cracking for improving boat coal quality |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106520195A CN106520195A (en) | 2017-03-22 |
| CN106520195B true CN106520195B (en) | 2018-05-18 |
Family
ID=58346563
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510578869.9A Active CN106520195B (en) | 2015-09-11 | 2015-09-11 | A kind of method for hydrogen cracking for improving boat coal quality |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106520195B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109722290B (en) * | 2017-10-27 | 2021-04-06 | 中国石油化工股份有限公司 | Methods to reduce the freezing point of jet fuel at high dry point |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3799869A (en) * | 1972-04-13 | 1974-03-26 | Exxon Research Engineering Co | Method of producing jet fuel by upgrading light catalytic cycle oil |
| US7591940B2 (en) * | 2003-02-04 | 2009-09-22 | Uop Llc | Combination hydrocracking process for the production of ultra low sulfur diesel |
| CN103013559A (en) * | 2011-09-22 | 2013-04-03 | 中国石油化工股份有限公司 | Hydrocracking method for selective increasing of aviation kerosene yield |
| CN103059986A (en) * | 2011-10-24 | 2013-04-24 | 中国石油化工股份有限公司 | Hydrocracking method for producing chemical materials |
| CN103059985A (en) * | 2011-10-24 | 2013-04-24 | 中国石油化工股份有限公司 | Middle-pressure hydrocracking method for producing aviation kerosene and low-freezing point diesel |
-
2015
- 2015-09-11 CN CN201510578869.9A patent/CN106520195B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3799869A (en) * | 1972-04-13 | 1974-03-26 | Exxon Research Engineering Co | Method of producing jet fuel by upgrading light catalytic cycle oil |
| US7591940B2 (en) * | 2003-02-04 | 2009-09-22 | Uop Llc | Combination hydrocracking process for the production of ultra low sulfur diesel |
| CN103013559A (en) * | 2011-09-22 | 2013-04-03 | 中国石油化工股份有限公司 | Hydrocracking method for selective increasing of aviation kerosene yield |
| CN103059986A (en) * | 2011-10-24 | 2013-04-24 | 中国石油化工股份有限公司 | Hydrocracking method for producing chemical materials |
| CN103059985A (en) * | 2011-10-24 | 2013-04-24 | 中国石油化工股份有限公司 | Middle-pressure hydrocracking method for producing aviation kerosene and low-freezing point diesel |
Non-Patent Citations (1)
| Title |
|---|
| 灵活利用加氢裂化装置增产喷气燃料;张芳华;《石油炼制与化工》;20150630;第46卷(第6期);第21-25页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106520195A (en) | 2017-03-22 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103013559B (en) | Hydrocracking method for selective increasing of aviation kerosene yield | |
| CN1952070A (en) | Method for producing cleaning oil from coal-tar oil | |
| CN114437789A (en) | Method for producing jet fuel from diesel oil fraction | |
| CN100558863C (en) | A combined method for producing clean oil from coal tar | |
| CN103059974B (en) | Hydrotreatment method for producing food grade solvent naphtha | |
| CN106520199B (en) | The method for hydrogen cracking of production boat coal under the conditions of a kind of middle pressure | |
| CN103525461B (en) | A kind of method for hydrogen cracking | |
| CN103773480B (en) | A kind of method improving heavy diesel quality | |
| CN112143521B (en) | Hydrogenation method and system for producing catalytic reforming raw material | |
| CN105542851B (en) | Aviation kerosene production method | |
| CN106520196B (en) | A kind of method for hydrogen cracking for producing boat coal | |
| CN106520195B (en) | A kind of method for hydrogen cracking for improving boat coal quality | |
| WO2022007736A1 (en) | Distillate super/subcritical fluid enhanced hydrogenation method | |
| CN106520197B (en) | A kind of method for hydrogen cracking that boat coal is produced by inferior feedstock oil | |
| CN100443572C (en) | A hydrocracking method for producing diesel oil from heavy feed oil with high nitrogen content | |
| CN116042270B (en) | Hydrocracking method for producing heavy naphtha and jet fuel | |
| CN103965961A (en) | Hydrogenization reforming system, hydrogenization reforming process, and aromatic products of coal liquefaction full distillate | |
| CN110835550A (en) | Hydrocracking method for producing chemical raw materials | |
| CN102807893B (en) | Co-current flow type hydrocracking method | |
| CN100594232C (en) | A kind of upgrading method of inferior distillate oil | |
| CN104650972B (en) | Reduce the method for hydrogen cracking of light fraction product sulfur content | |
| CN106520191B (en) | It is a kind of to strengthen the method for hydrogen cracking for adding hydrogen | |
| CN203820722U (en) | Hydroreforming system for full-range coal liquefied oil | |
| CN114736708B (en) | Wax oil liquid phase hydrotreating method | |
| CN103773491A (en) | Method for improving quality of heavy diesel oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |