CN210045217U - Up-down opposite flushing type residual oil hydrogenation fluidized bed micro-interface strengthening reaction device - Google Patents
Up-down opposite flushing type residual oil hydrogenation fluidized bed micro-interface strengthening reaction device Download PDFInfo
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- CN210045217U CN210045217U CN201920156218.4U CN201920156218U CN210045217U CN 210045217 U CN210045217 U CN 210045217U CN 201920156218 U CN201920156218 U CN 201920156218U CN 210045217 U CN210045217 U CN 210045217U
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 27
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 18
- 238000011010 flushing procedure Methods 0.000 title claims abstract description 10
- 238000005728 strengthening Methods 0.000 title claims abstract description 8
- 239000007788 liquid Substances 0.000 claims abstract description 124
- 230000001804 emulsifying effect Effects 0.000 claims abstract description 7
- 238000004080 punching Methods 0.000 claims abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 238000000034 method Methods 0.000 abstract description 3
- 230000005501 phase interface Effects 0.000 abstract description 3
- 230000008569 process Effects 0.000 abstract description 3
- 230000008901 benefit Effects 0.000 abstract description 2
- 230000036632 reaction speed Effects 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 23
- 239000007789 gas Substances 0.000 description 18
- 239000002994 raw material Substances 0.000 description 12
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 239000001257 hydrogen Substances 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- 239000002101 nanobubble Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 239000000839 emulsion Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 239000010771 distillate fuel oil Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004945 emulsification Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000003116 impacting effect Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000007142 ring opening reaction Methods 0.000 description 1
- 229930195734 saturated hydrocarbon Natural products 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
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Abstract
The utility model discloses a micro-interface strengthening reaction device of an up-down opposite flushing type residual oil hydrogenation emulsifying bed, which comprises a reactor main body; the top of the gas-liquid separator is provided with a gas-liquid discharge hole; at least two bubble breakers; are respectively arranged at the upper part and the lower part of the reactor main body and are in an up-down opposite punching shape; the bubble breaker is provided with an air inlet, a liquid inlet and a discharge port, and the discharge port of the upper bubble breaker is connected with the reactor main body through a gas-liquid mixing pipeline; a gas-liquid separator; a gas-liquid discharge port connected with the reactor main body; the top of the gas-liquid separator is provided with an exhaust port, and the bottom of the gas-liquid separator is provided with a liquid outlet; a circulation pump; a liquid outlet connected with the gas-liquid separator; a heat exchanger; an outlet pipeline connected with the circulating pump; and the heat exchanger is provided with a liquid discharge port which is respectively connected with a liquid discharge pipeline and a circulating liquid pipeline. The device of the utility model has the advantages of low operating pressure, large gas-liquid mass transfer phase interface area, high apparent reaction speed, high gas utilization rate, less investment, low energy consumption, flexible process and the like.
Description
Technical Field
The utility model relates to a micro-interface strengthening reaction device of an upper and lower hedging type residual oil hydrogenation and emulsification bed.
Background
The residual oil can be classified into a large number of types according to the differences of crude oil producing areas, oil refining processes and the like, and generally can be classified into two types of atmospheric residual oil and vacuum residual oil. The main components of the residual oil comprise saturated hydrocarbon, aromatic hydrocarbon, colloid, asphaltene and the like. Under the action of high temperature and high pressure and catalyst, residual oil may be deeply hydrogenated to obtain light fuel oil product through ring opening, cracking and other complicated physical and chemical changes.
With the increasing demand of various countries in the world on light oil products and the continuous stricter requirement on environmental protection, people pay more attention to the hydrogenation technology of residual oil. The traditional residual oil hydrogenation generally adopts a suspension bed hydrogenation reactor, and although the reactor has strong adaptability to raw materials and simple operation, the hydrogenation reaction efficiency is lower because the reactor is controlled by mass transfer. The fundamental reason is that the bubble size in the reactor is large (generally 3-10 mm), so the gas-liquid phase boundary mass transfer area is small (generally 100-
2/m
3) Thus limiting mass transfer efficiency. Therefore, engineering has to employ high temperature (470 ℃ or higher) and high pressure (20 MPa or higher) operations to enhance the reaction process by increasing the solubility of hydrogen to increase the mass transfer rate. However, high temperature and high pressure cause a series of side effects: high energy consumption and production cost, high investment intensity, short equipment operation period, more faults, poor intrinsic safety and the like, thereby bringing challenges to industrialized mass production.
Diameter of bubble (Sauter diameter) d
32Is a key parameter for determining the size of the interfacial area and is a core factor for determining the gas-liquid reaction rate. d
32When the volume mass transfer coefficient is gradually increased, the volume mass transfer coefficient is gradually increased; especially when d is
32When the diameter is less than 1mm, the volume mass transfer coefficient is dependent on d
32The decrease in (c) increases rapidly in an exponential-like fashion. Thus, d is
32The reduction to nanometer level can strengthen the gas-liquid reaction greatly. The diameter of the steel wire is less than or equal to 1 mu m
32Bubbles less than 1mm can be called micro bubbles, and the diameter satisfies d is less than or equal to 50nm
32Bubbles < 1 μm may be referred to as nanobubbles. The phase interface formed by the microbubbles and nanobubbles is called a nanointerface. If the system has both nano bubbles and micro bubbles, the system is called a nano-micro interface system. According to Yang-Laplace equation, the internal pressure of the bubble is compared withThe radius is in inverse proportion, so that the nano micro bubbles are also beneficial to improving the internal pressure of the bubbles and improving the solubility of the gas. Therefore, in the gas-liquid reaction process, the nano-micro interface system can strengthen gas-liquid mass transfer, and further accelerate the gas-liquid reaction. The nano-micro-bubbles have the characteristic of rigidity, have good independence and are not easy to coalesce, so that the gas and the liquid of a nano-micro-bubble system are fully mixed, a system containing a large amount of nano-micro-bubbles can be obtained, a higher phase interface area is formed in the reactor, and the reaction rate is further accelerated.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing an upper and lower hedging formula residual oil hydrogenation fluidized bed micro-interface intensification reaction unit utilizes little micron order bubble breaker to transmit the pressure energy of gas and the kinetic energy of liquid for the bubble and finally change bubble surface energy into, and the device forms little micron order bubble through fluid torrent micro-structure and mechanical microstructure combined action to form the micro-interface gas-liquid reaction system.
The utility model discloses specifically adopt following technical scheme to realize above-mentioned technical purpose:
a micro-interface strengthening reaction device of an up-down opposite flushing type residual oil hydrogenation emulsifying bed comprises:
a reactor body; the top of the gas-liquid separator is provided with a gas-liquid discharge hole;
at least two bubble breakers; are respectively arranged at the upper part and the lower part of the reactor main body and are in an up-down opposite punching shape; the bubble breaker is provided with an air inlet, a liquid inlet and a discharge port, and the discharge port of the upper bubble breaker is connected with the reactor main body through a gas-liquid mixing pipeline;
a gas-liquid separator; a gas-liquid discharge port connected with the reactor main body; the top of the gas-liquid separator is provided with an exhaust port, and the bottom of the gas-liquid separator is provided with a liquid outlet;
a circulation pump; a liquid outlet connected with the gas-liquid separator;
a heat exchanger; an outlet pipeline connected with the circulating pump; the heat exchanger is provided with a liquid discharge port, the liquid discharge port is respectively connected with a liquid discharge pipeline and a circulating liquid pipeline, and the circulating liquid pipeline is connected with a liquid inlet of the bubble crusher;
a draft tube; is vertically arranged in the reactor main body.
The bubble breaker of the utility model is divided into a pneumatic type, a hydraulic type and a gas-liquid linkage type according to an energy input mode or a gas-liquid ratio, wherein the pneumatic type bubble breaker is driven by gas, and the input gas amount is far larger than the liquid amount; the hydraulic bubble breaker is driven by liquid, the input gas amount is generally smaller than the liquid amount, and the gas-liquid linkage bubble breaker is driven by gas and liquid together. When a plurality of bubble breakers are adopted, the pneumatic type bubble breaker and the hydraulic type bubble breaker can be connected in series to form a group of bubble breakers. One reaction system may combine a plurality of bubble breakers in series or in parallel.
The utility model discloses a bubble breaker is installed respectively in reactor main part top and bottom, and is the formula of dashing from top to bottom promptly, and the gas-liquid emulsion gets into the reactor main part from below and top respectively. The up-down opposite-flushing arrangement of the bubble breakers is characterized in that the bubble breakers are suitable for reaction systems with large gas volume and high gas-liquid conversion rate requirements, and the guide cylinders in the reactor main body are favorable for macroscopic mass transfer and heat transfer and can accelerate the reaction rate.
As a further improvement of the utility model, the average bubble diameter of the micron-sized bubble system in the bubble breaker is 100nm-500 μm. For a bubble system of 100nm-100 μm, the nano-bubble and the micro-bubble are contained, a nano-micro interface can be formed, and the effect equivalent to that of a micro interface of 10 μm-500 μm can be obtained on the basis of lower air pressure and lower temperature.
The device of the utility model is suitable for a gas-liquid containing reaction system. The bubble size of the gas-liquid system is reduced to 100nm-500 mu m from the traditional 3-10mm by using the bubble breaker, so that the gas content of the system and the mass transfer area of a gas-liquid phase boundary are greatly increased, the heterogeneous reaction process is accelerated, the gas utilization rate is increased, the environmental problem caused by excessive discharge is improved, the problems of high temperature, high pressure, high material consumption and energy consumption, high investment, high risk and the like in the traditional gas-liquid reaction process are solved, and the investment cost and the operating cost of equipment are reduced.
The utility model discloses a reaction system is because the bubble is less than less, and the gas-liquid separation that leads to is slower, so need set up dedicated high-efficient vapour and liquid separator (like the suspension separator) behind the reactor again in order to realize the separation of microbubble and liquid.
The device of the utility model is not only suitable for the hydrogenation of middle and low pressure high airspeed residual oil, but also can be used for the hydrogenation of the mixed oil of middle and low pressure high airspeed residual oil and coal tar, and the hydrogenation reaction of middle and low pressure high airspeed in high-difficulty mixed solid-liquid systems such as buggy-residual oil, buggy-tar, buggy-catalytic slurry oil and so on to prepare light fuel oil or other specific petroleum products.
The utility model discloses compare in traditional gas-liquid reactor's advantage lies in:
1. the energy consumption is low. Conventional fixed bed gas-liquid reactors increase the solubility of the gas feed in the liquid feed by high pressure to enhance mass transfer. The utility model breaks the gas into a 100nm-500 μm small micron-sized bubble system to form an emulsifying bed, which can greatly increase the gas-liquid interface area and strengthen the mass transfer. The pressure can be suitably reduced, thereby reducing energy consumption.
2. The gas-liquid ratio is low. In order to ensure that the liquid raw materials can fully react in the traditional gas-liquid reactor, the gas-liquid ratio is generally controlled at 2000-3000: 1. The device can greatly reduce the gas-liquid ratio due to greatly strengthening mass transfer, thereby not only reducing the material consumption of gas, but also reducing the energy consumption of subsequent gas cyclic compression. The mass transfer and further reaction of the device are enhanced, so that the hydrogen-oil ratio can be greatly reduced, the material consumption of hydrogen is reduced, and the energy consumption of cyclic compression is reduced.
3. Flexible process configuration, high production safety, low ton product cost and strong market competitiveness.
Drawings
FIG. 1 is a schematic structural diagram of a micro-interface enhanced reaction device of an up-down counter flushing type residue oil hydrogenation emulsifying bed in example 1;
FIG. 2 is a schematic structural diagram of a micro-interface enhanced reaction device of an up-down counter-flushing residual oil hydrogenation fluidized bed in example 2;
FIG. 3 is a schematic structural diagram of a micro-interface enhanced reaction device of an up-down counter flushing type residue oil hydrogenation emulsifying bed in example 3;
in the figure: 1 a reactor body; 2, a gas-liquid separator; 3, a circulating pump; 4, a heat exchanger; 1-1 hydraulic breaker; 1-2 pneumatic bubble breaker; 1-3 gas raw material pipelines; 1-4 hydraulic bubble breaker air inlet pipeline; 1-5 primary emulsion lines; 1-6 pneumatic bubble breaker air inlet pipeline; 1-7 liquid raw material pipelines; 1-8 gas-liquid discharge pipelines; 1-9 slag removal pipelines; 1-10 gas-liquid mixing pipelines; 1-11 guide shell; 1-12 gas-liquid linkage type bubble breakers; 2-1 liquid outlet pipeline; 2-2 exhaust lines; 3-1 outlet pipeline; 4-1 liquid discharge pipeline; 4-2 circulating liquid pipelines.
Detailed Description
The following describes in further detail embodiments of the present invention with reference to the accompanying drawings. The following examples are intended to illustrate the invention, but not to limit its scope.
Example 1
The micro-interface strengthening reaction device of the upper and lower opposite flushing type residual oil hydrogenation emulsifying bed shown in figure 1 comprises a reactor main body 1; the top of the gas-liquid discharge port is provided with a gas-liquid discharge port which is connected with gas-liquid discharge pipelines 1-8;
at least two bubble breakers; are respectively arranged at the upper part and the lower part of the reactor main body 1 and are in an up-down opposite punching shape; in the embodiment, the upper bubble breaker is a hydraulic bubble breaker 1-1, the lower bubble breaker is a pneumatic bubble breaker 1-2, and the hydraulic bubble breaker 1-1 is provided with a liquid inlet which is connected with a liquid raw material pipeline 1-7 and a 4-2 circulating liquid pipeline; the air inlet is connected with an air inlet pipeline 1-4 of the hydraulic bubble breaker; the pneumatic bubble breaker 1-2 is provided with an air inlet which is connected with an air inlet pipeline 1-3 of the pneumatic bubble breaker; the liquid inlet is not connected, the liquid inlet can be connected with a liquid raw material pipeline, and static liquid can be filled in the pneumatic bubble crusher in advance without introducing liquid additionally; the discharge port of the upper hydraulic bubble breaker 1-1 is connected with the reactor main body 1 through a gas-liquid mixing pipeline 1-10.
Fresh hydrogen entering from the gas raw material pipeline 1-3 is divided into two paths, one part of the hydrogen enters a pneumatic type crusher 1-2 arranged at the bottom of the reactor main body 1 through a pneumatic type bubble crusher air inlet pipeline 1-6, and the hydrogen rises into the reactor main body 1 after being crushed into micro bubbles. Liquid raw materials enter a hydraulic bubble crusher 1-1 through a hydraulic bubble crusher air inlet pipeline 1-4, the liquid raw materials are crushed into a micron bubble gas-liquid system in the hydraulic bubble crusher 1-1 through circulating liquid sent from a pipeline 4-2 and the liquid raw materials introduced into the hydraulic bubble crusher air inlet pipeline 1-4, and the obtained gas-liquid emulsion enters a reactor main body 1 through a mixing pipeline 1-10 and then rushes into a guide cylinder 1-11. The gas-liquid mixture reaches the bottom of the reactor main body 1 along the guide shell 1-11, and after impacting and mixing oppositely with the micro bubble flow generated by the bubble breaker 1-2 at the bottom of the reactor main body 1, the gas-liquid mixture moves upwards along the wall surface of the reactor main body 1, part of the ascending micro bubble flow is sucked into the guide shell 1-11 at the upper end of the guide shell 1-11 to form a circulating flow, the rest is sent into the gas-liquid separator 2 from the top gas-liquid discharge pipeline 1-8, the separated gas is sent to subsequent treatment through the exhaust pipeline 2-2, and the obtained liquid enters the circulating pump 3 through the pipeline 2-1. After liquid sent by the circulating pump 3 enters the heat exchanger 4 through the pipeline 3-1, a part of the liquid is sent to subsequent treatment through the liquid discharging pipeline 4-1, and the rest of the liquid is used as crushing power and sent to the hydraulic bubble crusher 1-1 through the circulating liquid pipeline 4-2.
Example 2
The apparatus of example 2 is different from example 1 in that the bubble breaker at the upper part is a gas-liquid linkage type bubble breaker 1-12, as shown in fig. 2.
Example 3
The apparatus of example 3 is constructed as shown in FIG. 3, and differs from example 1 in that the upper bubble breaker is composed of a hydraulic bubble breaker 1-1 and a pneumatic bubble breaker 1-2 connected in series. The pneumatic bubble breaker 1-2 is provided with an air inlet which is connected with an air inlet pipeline 1-6 of the pneumatic bubble breaker 1-2; the liquid inlet is connected with a liquid raw material pipeline 1-7; a liquid inlet is arranged on the hydraulic bubble crusher 1-1 and is connected with a circulating liquid pipeline 4-2; the air inlet is connected with an air inlet pipeline 1-4 of the hydraulic bubble breaker; the pneumatic bubble breaker air inlet pipeline 1-6 and the hydraulic bubble breaker air inlet pipeline 1-4 are connected to the gas raw material pipeline 1-3.
Claims (3)
1. A micro-interface strengthening reaction device of an up-down opposite flushing type residual oil hydrogenation emulsifying bed is characterized by comprising:
a reactor body; the top of the gas-liquid separator is provided with a gas-liquid discharge hole;
at least two bubble breakers; are respectively arranged at the upper part and the lower part of the reactor main body and are in an up-down opposite punching shape; the bubble breaker is provided with an air inlet, a liquid inlet and a discharge port, and the discharge port of the upper bubble breaker is connected with the reactor main body through a gas-liquid mixing pipeline;
a gas-liquid separator; a gas-liquid discharge port connected with the reactor main body; the top of the gas-liquid separator is provided with an exhaust port, and the bottom of the gas-liquid separator is provided with a liquid outlet;
a circulation pump; a liquid outlet connected with the gas-liquid separator;
a heat exchanger; an outlet pipeline connected with the circulating pump; the heat exchanger is provided with a liquid discharge port, the liquid discharge port is respectively connected with a liquid discharge pipeline and a circulating liquid pipeline, and the circulating liquid pipeline is connected with a liquid inlet of the bubble crusher;
a draft tube; is vertically arranged in the reactor main body.
2. The device of claim 1, wherein the bubble breaker is a gas-liquid linkage type bubble breaker, a pneumatic type bubble breaker, a hydraulic type bubble breaker or a series combination thereof.
3. The apparatus according to claim 1, wherein the micro-bubble system in the bubble breaker has an average bubble diameter of 100nm to 500 μm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920156218.4U CN210045217U (en) | 2019-01-29 | 2019-01-29 | Up-down opposite flushing type residual oil hydrogenation fluidized bed micro-interface strengthening reaction device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920156218.4U CN210045217U (en) | 2019-01-29 | 2019-01-29 | Up-down opposite flushing type residual oil hydrogenation fluidized bed micro-interface strengthening reaction device |
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| CN111482139A (en) * | 2019-01-29 | 2020-08-04 | 南京大学 | Up-down opposite flushing type residual oil hydrogenation fluidized bed micro-interface strengthening reaction device and method |
| CN111569815A (en) * | 2020-05-14 | 2020-08-25 | 南京延长反应技术研究院有限公司 | Benzene selective hydrogenation reaction system and method |
| WO2021196386A1 (en) * | 2020-03-31 | 2021-10-07 | 南京延长反应技术研究院有限公司 | Built-in micro-interface oxidation system and method for preparing terephthalic acid from p-xylene |
| WO2021208202A1 (en) * | 2020-04-13 | 2021-10-21 | 南京延长反应技术研究院有限公司 | Micro-interface enhanced cyclohexanone ammoximation reaction system and method |
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| RU2808489C1 (en) * | 2020-06-17 | 2023-11-28 | Наньцзин Яньчан Реэкшн Текнолоджи Рисерч Институт Ко., Лтд. | System for carrying out reaction for producing polyethylene with increasing microsurfaces using polymerization in solution |
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| CN111482139A (en) * | 2019-01-29 | 2020-08-04 | 南京大学 | Up-down opposite flushing type residual oil hydrogenation fluidized bed micro-interface strengthening reaction device and method |
| JP2023513384A (en) * | 2020-03-31 | 2023-03-30 | 南京延長反応技術研究院有限公司 | Built-in micro-surface oxidation system and method for producing terephthalic acid from para-xylene |
| WO2021196386A1 (en) * | 2020-03-31 | 2021-10-07 | 南京延长反应技术研究院有限公司 | Built-in micro-interface oxidation system and method for preparing terephthalic acid from p-xylene |
| JP7433584B2 (en) | 2020-03-31 | 2024-02-20 | 南京延長反応技術研究院有限公司 | Built-in micro-interfacial oxidation system and method for producing terephthalic acid from paraxylene |
| WO2021208202A1 (en) * | 2020-04-13 | 2021-10-21 | 南京延长反应技术研究院有限公司 | Micro-interface enhanced cyclohexanone ammoximation reaction system and method |
| CN111569815A (en) * | 2020-05-14 | 2020-08-25 | 南京延长反应技术研究院有限公司 | Benzene selective hydrogenation reaction system and method |
| WO2021227135A1 (en) * | 2020-05-14 | 2021-11-18 | 南京延长反应技术研究院有限公司 | Benzene selective hydrogenation reaction system and method |
| US11370727B1 (en) | 2020-05-14 | 2022-06-28 | Nanjing Yanchang Reaction Technology Research Institute Co., Ltd. | Benzene selective hydrogenation reaction system and method thereof |
| WO2021253311A1 (en) * | 2020-06-17 | 2021-12-23 | 南京延长反应技术研究院有限公司 | Micro-interface strengthened reaction system and method for preparing polyethylene by means of solution method |
| JP7184313B2 (en) | 2020-06-17 | 2022-12-06 | 南京延長反応技術研究院有限公司 | MICROINTERFACE REINFORCED REACTION SYSTEM AND METHOD FOR PRODUCING POLYETHYLENE BY SOLUTION |
| JP2022539481A (en) * | 2020-06-17 | 2022-09-09 | 南京延長反応技術研究院有限公司 | MICROINTERFACE REINFORCED REACTION SYSTEM AND METHOD FOR PRODUCING POLYETHYLENE BY SOLUTION |
| RU2808489C1 (en) * | 2020-06-17 | 2023-11-28 | Наньцзин Яньчан Реэкшн Текнолоджи Рисерч Институт Ко., Лтд. | System for carrying out reaction for producing polyethylene with increasing microsurfaces using polymerization in solution |
| WO2021253312A1 (en) * | 2020-06-17 | 2021-12-23 | 南京延长反应技术研究院有限公司 | Enhanced reaction system and method for preparing polypropylene by means of slurry process |
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