CN1435275A - Multistage circulation reactor - Google Patents
Multistage circulation reactor Download PDFInfo
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- CN1435275A CN1435275A CN 02100451 CN02100451A CN1435275A CN 1435275 A CN1435275 A CN 1435275A CN 02100451 CN02100451 CN 02100451 CN 02100451 A CN02100451 A CN 02100451A CN 1435275 A CN1435275 A CN 1435275A
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- 239000007788 liquid Substances 0.000 claims abstract description 24
- 239000012295 chemical reaction liquid Substances 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 abstract description 32
- 239000007787 solid Substances 0.000 abstract description 21
- 239000012530 fluid Substances 0.000 abstract description 19
- 238000000034 method Methods 0.000 abstract description 8
- 239000002245 particle Substances 0.000 abstract description 6
- 238000005984 hydrogenation reaction Methods 0.000 abstract description 4
- 238000007254 oxidation reaction Methods 0.000 abstract description 4
- 239000010865 sewage Substances 0.000 abstract description 4
- 238000004517 catalytic hydrocracking Methods 0.000 abstract description 3
- 230000000694 effects Effects 0.000 abstract description 3
- 239000010802 sludge Substances 0.000 abstract description 3
- 239000004215 Carbon black (E152) Substances 0.000 abstract description 2
- 238000009825 accumulation Methods 0.000 abstract description 2
- 239000003245 coal Substances 0.000 abstract description 2
- 230000008021 deposition Effects 0.000 abstract description 2
- 238000000855 fermentation Methods 0.000 abstract description 2
- 230000004151 fermentation Effects 0.000 abstract description 2
- 229930195733 hydrocarbon Natural products 0.000 abstract description 2
- 150000002430 hydrocarbons Chemical class 0.000 abstract description 2
- 239000000463 material Substances 0.000 abstract description 2
- 238000004090 dissolution Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 29
- 238000010586 diagram Methods 0.000 description 6
- 230000033001 locomotion Effects 0.000 description 6
- 239000012071 phase Substances 0.000 description 6
- 238000005273 aeration Methods 0.000 description 5
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 230000005587 bubbling Effects 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- JHIVVAPYMSGYDF-UHFFFAOYSA-N cyclohexanone Chemical compound O=C1CCCCC1 JHIVVAPYMSGYDF-UHFFFAOYSA-N 0.000 description 2
- 230000026058 directional locomotion Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000010907 mechanical stirring Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000012495 reaction gas Substances 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- BRLQWZUYTZBJKN-UHFFFAOYSA-N Epichlorohydrin Chemical compound ClCC1CO1 BRLQWZUYTZBJKN-UHFFFAOYSA-N 0.000 description 1
- 159000000021 acetate salts Chemical class 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
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Abstract
A multi-stage circulation reactor for various gas-liquid two-phase and gas-liquid-solid three-phase chemical reactions comprises a tower body 1, a guide cylinder 2 and a gas distributor 3, wherein the guide cylinder 2 is arranged in the tower body 1, and the gas distributor 3 is arranged at the bottom of the guide cylinder 2. Once bubbles are generated at the bottom of the tower, the fluid in the guide shell moves upwards to form a flow state that the large circulation is sleeved with the small circulation; the gas-liquid contact in the reactor is full, the gas content is high, the local gas content is uniformly distributed, the mass transfer rate is high, and the gas dissolution speed is high; for a gas-liquid-solid three-phase reaction system, solid particles are uniformly distributed in the reactor, and local accumulation or deposition cannot occur; the heat transfer effect is good, the heat exchange speed between the fluid and the wall of the reactor is high, the temperature in the reaction system is uniformly distributed due to the full mixing of the materials in the reactor, and the temperature difference of different areas is very small, so that the reactor can be widely applied to various gas-liquid and gas-liquid-solid reaction processes such as an oxidation reaction process, a hydrogenation reaction process, a hydrocracking process, a coal liquefaction hydrogenation process, a fermentation process, a hydrocarbon processing reaction process, an activated sludge sewage treatment process and the like.
Description
Technical Field
A reactor for various gas-liquid two-phase and gas-liquid-solid three-phase chemical reactions belongs to the field of chemical engineering, and particularly relates to a multistage loop reactor.
Background
Gas-liquid or gas-liquid-solid reactors are currently widely used in chemical, petrochemical, and other industrial processes. Generally, a bubble reactor or a stirred tank reactor is used for gas-liquid or gas-liquid-solid reactions. The two traditional reactors have low efficiency and high energy consumption, and the application field is limited by the reaction system. Efficient gas-liquid or gas-liquid-solid mixing, good dispersion of gas and solid particles in the liquid phase, high velocity directional flow of fluids, and high mass transfer rates are important properties of the reactor during these reactions. Particularly for reactions where mass transfer is the overall reaction control step and where liquid or solid phase catalysts are involved, some form of mechanical agitation must be employed to increase the mass transfer rate and the same mixing in order to accelerate the overall reaction process. Mechanical stirring is adopted, so that not only is the energy consumption high, but also the reaction system with high temperature, high pressure and strong corrosion is difficult to realize.
The inner loop reactor developed based on the bubbling reactor is characterized in that a guide shell is introduced into the bubbling reactor, so that fluid generates circulating flow in the reactor, the gas-liquid or gas-liquid-solid mixing effect is enhanced, and the overall mass transfer rate of the reactor is higher than that of the traditional bubbling reactor.
However, the conventional internal loop reactor has a serious drawback that in the annular space region between the guide shell and the inner wall of the reactor, the buoyancy force applied to the larger bubbles is larger than the drag force applied to the larger bubbles, so that the drag force generated by the liquid circulation cannot drag the larger bubbles, resulting in small annular space gas content, low reactor utilization rate and low overall reactor efficiency.
Disclosure of Invention
The invention aims to: a multistage loop reactor was developed and developed on the basis of a conventional bubble reactor. The multistage circulation reactor adopts the multistage guide cylinders and the inner members with different structures, completely overcomes the defects of small gas content of the annular space of the traditional internal circulation reactor and low reaction efficiency, has excellent hydrodynamic property, good gas-liquid or gas-liquid-solid mixing, high total mass transfer rate and uniform temperature distribution in the reactor, and can be widely applied to various gas-liquid or gas-liquid-solid chemical reaction processes.
The invention is realized by the following steps:
comprises a tower body 1, a guide shell 2 and a gas distributor 3, wherein the guide shell 2 is arranged in the tower body 1, and the gas distributor 3 is arranged at the bottom of the guide shell 2.
The invention also adopts the following technical scheme:
the ratio of the total height of the tower body 1 to the inner diameter of the reactor is 3-12, and the ratio of the diameter of the guide shell 2 to the inner diameter of the reactor is 0.3-0.9.
The guide shell 2 is an integral body, and can be a section or more than two sections; the distance between the sections is 5-50 cm, and the sections are connected by rigid ribs; baffle plates are added between the sections, and holes are punched on each section of the guide cylinder 2.
The guide shell 2 is provided with an opening area along the axial direction.
The opening on the guide shell 2 can be one or more than one.
The guide shell 2 is provided with an inner component 4.
The distance between the lower end of the guide shell 2 and the bottom of the reactor is 10-100 cm; the upper end of the guide shell is 10-200 cm away from the liquid level of the reaction liquid.
The reactor is internally provided with a plurality of stages of guide cylinders 2, the guide cylinders at all stages are coaxially fixed with each other, and gaps are reserved between the guide cylinders.
The number of the guide shell 2 can be 1-6, the axes of the guide shell 2 are parallel and are arranged in the reactor, and a gas distributor 3 is arranged below each guide shell 2.
The multistage circulation reactor of the invention is characterized in that:
① the multi-stage loop reactor of the invention is composed of a tower body, a guide shell, an inner member and a gas distributor, wherein the guide shell is single-section or multi-section, and the sections adopt various forms of combination and/or addition of the inner member;
② reaction gas enters the aeration tower through the gas distributor, once bubbles are generated at the bottom of the tower, bubble clusters drive surrounding liquid to move upwards due to the jet force and density difference of the gas, and fast circulation movement is carried out around each section of the guide shell and the guide shell as a whole, thus forming a flow state of large circulation sleeved with small circulation;
③ the gas-liquid-solid three-phase reaction system has high mass transfer rate and high gas dissolving speed because of the full gas-liquid contact, high gas content and uniform distribution of local gas content, and the solid particles are uniformly distributed in the reactor without local accumulation or deposition.
④ has good heat transfer effect, because the fluid makes rapid directional movement in the annular space of the reactor, the heat exchange rate between the fluid and the wall of the reactor is high, and because the materials in the reactor are fully mixed, the temperature in the reaction system is uniformly distributed, and the temperature difference in different areas is very small.
Drawings
FIG. 1 is one of the structural diagrams of the multi-stage circulation aeration tower of the present invention;
FIG. 2 is a second structural view of the multi-stage circulation aeration tower of the present invention;
FIG. 3 is a third structural view of the multi-stage circulation aeration tower of the present invention;
FIG. 4 is a fourth structural view of the multi-stage circulation aeration tower of the present invention;
FIG. 5 is a structural view of an inner member (baffle plate) between guide cylinders according to the present invention;
FIG. 6 is a fluid flow regime diagram for the reactor configuration shown in FIG. 1;
FIG. 7 is a state diagram of fluid flow in the reactor configuration shown in FIG. 2;
FIG. 8 is a state diagram of fluid flow in the reactor configuration shown in FIG. 3;
FIG. 9 is a state diagram of fluid flow in the reactor configuration shown in FIG. 4;
FIG. 10 is a diagram showing the structure and flow state of a multi-stage loop reactor with multiple guide cylinders.
Detailed description of the invention
The invention is described in detail below with reference to the attached drawing figures:
as shown in fig. 1, the tower consists of a tower body 1, a guide shell 2, a gas distributor 3 and the like. The guide shell can be one section, two sections or multiple sections, and the sections are connected by rigid ribs.
As shown in fig. 2: consists of a tower body, a guide shell, an inner component 4 and a gas distributor. The guide shell can be one section, two sections or multiple sections.
As shown in fig. 3: comprises a tower body, a guide shell 2 with an opening, and a gas distributor. One, two or more perforated areas can be arranged along the axial direction of the guide shell.
As shown in fig. 4, the tower consists of a tower body,a guide shell, an inner member and a gas distributor. The guide shell can be one section, two sections or multiple sections, and an opening area is arranged at a certain part of each section of guide shell.
As shown in FIG. 6, the fluid performs rapid directional movement in the tower around each section of guide shell and the whole guide shell, and forms a movement mode of large circulation flow and small circulation flow.
In the multistage loop reactor of the invention, reaction gas enters from the bottom of the multistage loop reactor through the gas distributor 3, and a large amount of bubbles are immediately generated around the gas distributor 3, namely a dilute phase area is formed around the gas distributor 3, the density of the dilute phase area is less than that of surrounding liquid, under the action of density difference and impulse force of the gas entering the reactor, the bubbles and the liquid in the dilute phase area move upwards in the guide shell, and the liquid in an annular gap area between the guide shell 2 and the inner wall of the reactor immediately flows to the gas distributor for supplement, so that rapid circulation movement is formed. When the fluid moves upwards to the top end of the first section of guide cylinder 2, under the action of the baffle plate and/or static pressure difference, a part of the fluid flows to the annular gap from the gap between the first guide cylinder and the second guide cylinder and turns back with the fluid flowing downwards in the annular gap; and a part of fluid still moves upwards to enter the second guide cylinder and continues to move upwards. And continuing to do so until the fluid moves to the top of the last guide cylinder, and then turning back to move downwards along the annular gap.
Obviously, in the above-mentioned flow in the reactor, a plurality of small circular flows are formed along each section of the guide shell 2, and a large circular flow is formed along the whole guide shell, i.e. a flow state that a large circular flow overlaps a small circular flow is formed. Therefore, the turbulence degree at each position in the reactor is not greatly different, the gas content is uniformly distributed, and the bubbles are uniformly distributed along the axial direction of the reactor; for a gas-liquid-solid reaction system, solid particles are uniformly distributed. Because the gas makes multi-stage circular motion in the reactor, although the average residence time is kept unchanged, the path of the gas before the gas escapes from the reactor is longer, and meanwhile, the gas-liquid fully contacts and mixes, so that the solubility of the gas in a liquid phase is high.
The reactor consists of a tower body 1, an inner member 4, a guide cylinder 2 and a bottom gas distributor 3. The reactor of the invention has no mechanical stirring component, the fluid can circulate in the reactor quickly and directionally, the gas-liquid or gas-liquid-solid mixing is good, the reactor has no dead angle, and the mass transfer rate is high; through the action of the guide shell and the inner member, a rapid movement mode of circulation or large circulation sleeved by large circulation is formed in the reactor, bubbles and solid particles are uniformly distributed, the gas content and the solid content are uniform and consistent, and the solid particles cannot be accumulated at any position; because of the rapid circulation movement of the fluid in the reactor, the temperature in the reactor is uniformly distributed, and the heat exchange between the fluid and the wall of the reactor is good. The invention can be widely applied to various gas-liquid and gas-liquid-solid reaction processes such as an oxidation reaction process, a hydrogenation reaction process, a hydrocracking process, a coal liquefaction hydrogenation process, a fermentation process, a hydrocarbon processing reaction process, an activated sludge sewage treatment process and the like.
The multi-stage guide shell can be divided into two stages, three stages or a plurality of stages according to the height of the reactor. The multi-stage guide shell can be in different forms, including: the guide shell is divided into a plurality of sections, and the distance between the sections is 5-50 cm; the guide shell is divided into a plurality of sections, baffle plates are added between the sections, and holes are punched at different positions on each section of guide shell; the guide shell is one section, holes are drilled at different positions, and the opening rate is determined by the total length of the guide shell.
The reactor is internally provided with a gas distributor at the lower part of the guide shell.
Several embodiments of the invention are described below.
Example 1: gas-liquid reaction
A reactor: a first loop reactor; volume: 50 liters of the product
Chemical reaction:
reaction temperature: 170 ℃; reaction pressure: 12 atm; catalyst: KOH solution
Continuous operation, liquid space velocity: 0.25h-1
Example 2: oxidation reaction
A reactor: a secondary loop reactor; volume: 1m3
Chemical reaction:
reaction temperature: 140 ℃; reaction pressure: 5 atm; catalyst: acetate salt
Batch operation, reaction time: 11h example 3: oxidation reaction
A reactor: a secondary loop reactor; volume: 20 liters ofthe product
Chemical reaction:
reaction temperature: 106 ℃; reaction pressure: 5.6atm
Batch operation, reaction time 4h example 4: catalytic hydrocracking of heavy oils
A reactor: a secondary loop reactor; volume of the reactor: 20m3
Reaction temperature: at 450 ℃; reaction pressure: 130atm
Continuous operation, liquid space velocity 1h-1. Example 5: industrial sewage treatment
A reactor: the tower body of the secondary circulation reactor is made of carbon steel; volume: 25m3。
The sewage is petrochemical industry comprehensive wastewater which mainly contains benzene, toluene, styrene, epichlorohydrin, cyclohexanone and the like, COD is 960-1020mg/1, continuous operation is adopted, the environmental temperature is 6-20 ℃, the water temperature in the tower is 18-25 ℃, the retention time of the wastewater in the tower is 6 hours, the daily treatment capacity is 100 tons of wastewater per day, the concentration of activated sludge is 3-6g/l, and the COD of the treated water is reduced to 80-140. The COD removal rate is 86.2-91.6%.
Claims (9)
1. Multistage circulation flow reactor, including body of the tower (1), draft tube (2), gas distributor (3), its characterized in that: a guide shell (2) is arranged in the tower body (1), and a gas distributor (3) is arranged at the bottom of the guide shell (2).
2. The multistage loop reactor of claim 1, characterized in that: the ratio of the total height of the tower body (1) to the inner diameter of the reactor is 3-12, and the ratio of the diameter of the guide cylinder (2) to the inner diameter of the reactor is 0.3-0.9.
3. The multistage loop reactor of claim 1, characterized in that: the guide shell (2) is an integral body, can be one section or more than two sections, the distance between the sections is 5-50 cm, the sections are connected by rigid ribs, baffle plates are added between the sections, and holes can be punched on each section of the guide shell (2).
4. The multistage loop reactor according to claim 1 or 3, characterized in that: the guide shell (2) is provided with an opening area along the axial direction.
5. The multistage loop reactor according to claim 1 or 4, characterized in that: the opening on the guide shell (2) can be one or more than one.
6. The multistage loop reactor of claim 1, characterized in that: the guide shell (2) is provided with an inner component (4).
7. The multistage loop reactor of claim 1, characterized in that: the distance between the lower end of the guide shell (2) and the bottom of the reactor is 10-100 cm; the upper end of the guide shell (2) is 10-200 cm away from the liquid level of the reaction liquid.
8. The multistage loop reactor of claim 1, characterized in that: the device is internally provided with a plurality of stages of guide cylinders (2), and the guide cylinders are coaxially fixed with each other and a gap is reserved between the guide cylinders.
9. The multistage loop reactor of claim 1, characterized in that: the number of the guide cylinders (2) can be 1-6, the axes of the guide cylinders (2) are parallel to each other and are arranged in the reactor, and a gas distributor (3) is arranged below each guide cylinder (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB02100451XA CN1171667C (en) | 2002-02-01 | 2002-02-01 | Multistage circulation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB02100451XA CN1171667C (en) | 2002-02-01 | 2002-02-01 | Multistage circulation reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1435275A true CN1435275A (en) | 2003-08-13 |
| CN1171667C CN1171667C (en) | 2004-10-20 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB02100451XA Expired - Fee Related CN1171667C (en) | 2002-02-01 | 2002-02-01 | Multistage circulation reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1171667C (en) |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2007045132A1 (en) * | 2005-10-18 | 2007-04-26 | Zhejiang Renheng Chemical Co., Ltd | A dissolving unit having a guide shell |
| CN100338179C (en) * | 2005-12-28 | 2007-09-19 | 煤炭科学研究总院 | Magnetic scraper loop reactor for coal direct liquefaction and coal direct liquefaction method thereof |
| CN100427198C (en) * | 2006-09-01 | 2008-10-22 | 清华大学 | Staged reactor |
| CN102137715A (en) * | 2008-08-28 | 2011-07-27 | 赢创奥克森诺有限责任公司 | Parallelized jet loop reactors |
| CN101360553B (en) * | 2006-01-04 | 2012-11-14 | 奇派特石化有限公司 | Oxidation system employing internal structure for enhanced hydrodynamics |
| CN103043847A (en) * | 2011-10-17 | 2013-04-17 | 中国石油天然气股份有限公司 | Air floatation-biochemical treatment method and equipment for super-heavy oil sewage |
| CN103043746A (en) * | 2011-10-17 | 2013-04-17 | 中国石油天然气股份有限公司 | Degreasing method for super heavy oil wastewater |
| CN103880180A (en) * | 2014-03-05 | 2014-06-25 | 大连民族学院 | Intelligent integral treatment device for high-concentration non-degradable wastewater produced in industrial parks |
| CN105727845A (en) * | 2016-02-03 | 2016-07-06 | 浙江大学 | Double-solid-phase suspended bed reactor used for heavy oil hydrocracking and application thereof |
| CN108479646A (en) * | 2018-03-30 | 2018-09-04 | 青岛理工大学 | Pneumatic mixing arrangement of spent acid reduction |
| CN111054278A (en) * | 2019-12-02 | 2020-04-24 | 河南金鹏化工有限公司 | Continuous production process and device for thiodicarb synthesis reaction |
| CN112619566A (en) * | 2021-01-19 | 2021-04-09 | 中国科学院山西煤炭化学研究所 | Multistage jet loop reactor for preparing ethylene by oxidative coupling of methane |
| CN112808181A (en) * | 2021-01-19 | 2021-05-18 | 中国科学院山西煤炭化学研究所 | Jet loop reactor for preparing ethylene by oxidative coupling of methane |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1332748C (en) * | 2005-09-16 | 2007-08-22 | 清华大学 | Self circulated cascade gas lift type internal-loop reactor system |
-
2002
- 2002-02-01 CN CNB02100451XA patent/CN1171667C/en not_active Expired - Fee Related
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2007045132A1 (en) * | 2005-10-18 | 2007-04-26 | Zhejiang Renheng Chemical Co., Ltd | A dissolving unit having a guide shell |
| CN100338179C (en) * | 2005-12-28 | 2007-09-19 | 煤炭科学研究总院 | Magnetic scraper loop reactor for coal direct liquefaction and coal direct liquefaction method thereof |
| CN101360553B (en) * | 2006-01-04 | 2012-11-14 | 奇派特石化有限公司 | Oxidation system employing internal structure for enhanced hydrodynamics |
| CN100427198C (en) * | 2006-09-01 | 2008-10-22 | 清华大学 | Staged reactor |
| CN102137715A (en) * | 2008-08-28 | 2011-07-27 | 赢创奥克森诺有限责任公司 | Parallelized jet loop reactors |
| CN103043847A (en) * | 2011-10-17 | 2013-04-17 | 中国石油天然气股份有限公司 | Air floatation-biochemical treatment method and equipment for super-heavy oil sewage |
| CN103043746A (en) * | 2011-10-17 | 2013-04-17 | 中国石油天然气股份有限公司 | Degreasing method for super heavy oil wastewater |
| CN103043746B (en) * | 2011-10-17 | 2014-02-05 | 中国石油天然气股份有限公司 | Degreasing method for super heavy oil wastewater |
| CN103880180A (en) * | 2014-03-05 | 2014-06-25 | 大连民族学院 | Intelligent integral treatment device for high-concentration non-degradable wastewater produced in industrial parks |
| CN103880180B (en) * | 2014-03-05 | 2016-01-20 | 大连民族学院 | Industrial park high-concentration hardly-degradable waste water intelligent integral treatment unit |
| CN105727845A (en) * | 2016-02-03 | 2016-07-06 | 浙江大学 | Double-solid-phase suspended bed reactor used for heavy oil hydrocracking and application thereof |
| CN105727845B (en) * | 2016-02-03 | 2017-12-19 | 浙江大学 | A kind of double solid suspension bed reactors and its application for hydrocracking heavy oil |
| CN108479646A (en) * | 2018-03-30 | 2018-09-04 | 青岛理工大学 | Pneumatic mixing arrangement of spent acid reduction |
| CN111054278A (en) * | 2019-12-02 | 2020-04-24 | 河南金鹏化工有限公司 | Continuous production process and device for thiodicarb synthesis reaction |
| CN112619566A (en) * | 2021-01-19 | 2021-04-09 | 中国科学院山西煤炭化学研究所 | Multistage jet loop reactor for preparing ethylene by oxidative coupling of methane |
| CN112808181A (en) * | 2021-01-19 | 2021-05-18 | 中国科学院山西煤炭化学研究所 | Jet loop reactor for preparing ethylene by oxidative coupling of methane |
| CN112808181B (en) * | 2021-01-19 | 2022-04-08 | 山西潞安化工有限公司 | Jet loop reactor for preparing ethylene by oxidative coupling of methane |
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| Publication number | Publication date |
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| CN1171667C (en) | 2004-10-20 |
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