CN110237778A - A kind of isothermal reactor and its process of convenient changing catalyst - Google Patents
A kind of isothermal reactor and its process of convenient changing catalyst Download PDFInfo
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- B01J8/0407—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds
- B01J8/0411—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds the beds being concentric
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- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
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- B01J8/0415—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal through two or more cylindrical annular shaped beds the beds being superimposed one above the other
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- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
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- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
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- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00212—Plates; Jackets; Cylinders
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- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00884—Means for supporting the bed of particles, e.g. grids, bars, perforated plates
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Abstract
A kind of isothermal reactor and its process of convenient changing catalyst are related to a kind of reactor and its process, and reactor of the present invention is constructed using concentric circles, and every layer of concentric circles collet is relatively independent.Catalyst is filled into circular screen outside reactor, and sieve is integrally loaded into isothermal reactor collet, convenient handling.Unstripped gas is by concentric circles reactor internals surrounding radially into reactor, the refrigerant for making the most strongly exothermic amount corresponding temperature of initial reaction stage minimum in this way, concentric circles periphery loaded catalyst maximum corresponds to maximum heat exchange area, then from gas collecting tube discharge in the middle part of reactor after the convergence of product gas.The reactor of design can ideally realize the stability contorting of reaction bed temperature gradient Yu non-equal field of flow.For strong exothermal reactions such as typical methanol-fueled CLC, preparing methane by synthetic gas and oxidation or nitration reactions, reactor outer layer catalyst bed and internal layer catalyst bed are substantially without the temperature difference.
Description
Technical field
The present invention relates to a kind of reactor and its processes, anti-more particularly to a kind of isothermal of convenient changing catalyst
Answer device and its process.
Background technique
With human society continuous development and people's living standard it is constantly improve, the requirement to chemical industry gradually mentions
Height, trend is safe and environment-friendly, efficient, energy saving and sustainable development, as far as possible by reaction raw materials under the premise of essential safety
It is completely converted into target product, realizes production process zero-emission, shortens reaction process, improves production efficiency.
Since C-H, C-O and H-O key bond energy typical in compound is significantly different, lead to reaction raw materials and target product
Standard molar formation enthalpy difference it is larger, thus chemical reaction process usually just with heat absorption and heat release carry out.
In the synthesis process of most of energetic materials, such as: methanol-fueled CLC, preparing methane by synthetic gas, oxidation reaction, nitrification are anti-
It answers and chlorination or fluorination reaction etc., is frequently accompanied by violent exothermic reaction.If reaction heat can not be in time from anti-
It answers the interior removal of device to will lead to reaction heat largely to accumulate, reaction temperature is difficult to control, and causes reaction bed overtemperature, temperature runaway, or even draw
Play the serious consequences such as explosion.
For the strong exothermal reaction for having catalyst to participate in, high temperature will lead to catalyst overheating sintering and a large amount of carbon deposits in surface,
Significantly reduce catalytic efficiency and catalyst service life.Surface high dispersive, high activity catalyst often it is resistance to sintering and anti-product
Charcoal ability is poor.Meanwhile being limited by thermodynamical equilibrium, the equilibrium conversion of strong exothermal reaction is increased with reaction temperature and is gradually dropped
It is low, reaction need to be controlled as far as possible to be carried out at low temperature.Therefore, exploitation has the enlarged reaction unit gesture of strong heat exchange function must
Row！
By taking synthesis gas methanation reaction as an example, shown in key reaction such as equation (1-3), it is seen that
CO + 3H2→ CH4 + H2O ΔH=-206.1 KJ/mol ..............................(1)
CO2 + 4H2→ CH4 + 2H2O ΔH =-165.0 KJ/mol ...........................(2)
2CO + 2H2→ CH4 + CO2 ΔH =-247.3 KJ/mol ............................(3)
Methanation reaction is strong exothermal reaction, while the surface fast reaction of the reaction or volume reduction.Currently, world wide
Inside realized synthesis gas methanation production mature technology mainly include Luigi company design the neat methanation process in Shandong,
The TREMP methanation process and DAVY methanation process of Topsoe.Above-mentioned three kinds of technics comparings are similar, are using 3-5 sections
Fixed bed adiabatic methanator, first segment and second segment reactor use series and parallel structure, are high-temperature reactor, mixing
Near 650 DEG C, the reaction that CO is converted into CH4 mainly carries out in the two reactors gas outlet temperature, is a large amount of methanations
Reactor.Third and fourth section of reactor is low-temp reaction device, converts CH4 for unreacted CO in preceding two reactor, makes
The methane content of synthetic natural gas reaches the level of needs, to supplement methane reactor.Whole process is steamed by by-product high pressure saturation
Vapour recycles the heat that methanation reaction generates.
It is insulated multistage methanation reaction process and removes methanation reaction process using the means that segmentation conversion and segmentation move heat
In a large amount of heat, this is allowed for, and reaction system is complicated, equipment investment is big, energy consumption is high, operating difficulties, cannot achieve short route methane
Chemical industry skill.
The units such as Institutes Of Technology Of Taiyuan develop a kind of slurry bed system methanation device and technique (CN101979475B,
CN101979476B, CN102952596B), catalyst is dispersed in inert fluid, and bed is close to isothermal operation.Slurry bed system
Heat exchange efficiency is high, bed temperature is average, reaction condition temperature, overcome fixed bed reaction depth and it is strongly exothermic between contradiction.But
Slurry bed system is limited by mass transfer between gas-liquid-solid three-phase, and combined coefficient is low, and slurry bed system methanation process cannot achieve continuously
Operation, back-mixing is serious, and solid catalyst separates difficulty with atent solvent.
Process institute, the Chinese Academy of Sciences, Tsinghua University and Beijing low-carbon etc. exploitation based on conveying bed and fluidized bed methane chemical industry
Skill (CN1960954A, CN101817716A, CN102040441A, CN101774876A, CN102180757A).Convey bed and stream
Changing bed reaction has efficient gas solid transfer and heat transfer efficiency, and temperature and particle are uniformly distributed in reaction bed, can effectively be inhibited
Bed overtemperature and temperature runaway phenomenon.But exploitation is suitable for high intensity, high-wearing feature catalyst and the catalyst carry-over loss of fluidized bed
The problems such as there are no intact solutions.
The exploitation such as Beijing Hua Fu, Shanghai Chinese Xing Nengyuan and China Petroleum isothermal tubulation methanation process (CN102010284B,
CN207362166U, CN103373887B).Catalyst loads in shell-and-tube reactor, and shell is cold by conduction oil or vapor etc.
Matchmaker moves heat, is a major advantage that heat exchange area is big, but device fabrication is difficult, and equipment dependability is low.For methanation reaction, column
There is thermal balance hardly possible in pipe reactor, be embodied in CO and CO2 concentration highest in the reactant for initially enter reaction unit,
The reaction of catalyst bed upper layer is more violent, and heat release is the most serious, but conventional shell-and-tube reactor is uniform heat exchange, can not solution by no means
The problem of homogeneous temperature field and field of flow are mutually matched.
Summary of the invention
The purpose of the present invention is to provide the isothermal reactor and its process of a kind of convenient changing catalyst, the present invention
It can not solve the problems, such as that non-uniform temperature field and field of flow are mutually matched shell-and-tube reactor, start a kind of be suitable for by force
Exothermic reaction, catalyst can convenient handling isothermal reactor and its process design method, the present invention can realize ideally instead
Answer the stability contorting of bed temperature field gradient Yu non-equal field of flow.
The purpose of the present invention is what is be achieved through the following technical solutions:
A kind of isothermal reactor of convenient changing catalyst, the reactor use concentric design；Catalyst packing is in annular
In sieve, sieve is integrally loaded into concentric circles reactor, catalyst integral disassembly, assembly；Unstripped gas is from concentric circles reactor surrounding edge
Radially into the minimum refrigerant of the most strongly exothermic amount corresponding temperature of initial reaction stage, concentric circles periphery loaded catalyst maximum corresponds to
Maximum heat exchange area；The reactor includes pressure-bearing shell, high pressure resistant collet and closed circuit water route；Reactor pressure-bearing shell and
High pressure resistant collet is pressure-resistant material, and the pressure-resistant upper limit is 30MPa；The Catalyst packing that reactor uses is into circular screen；Annular
Sieve orifice diameter 0.5-5.0mm, mesh widths can freely regulate and control, and load convenient for catalyst radial direction single-layer or multi-layer；Reactor
It is the catalyst of single-layer or multi-layer filling in collet, is refrigerant collet outside collet.
A kind of isothermal reactor of convenient changing catalyst, the reactor jacket open equally distributed circle
Hole, square hole, strip-shaped hole or irregular hole, interior collet is refrigerant.
A kind of isothermal reactor of convenient changing catalyst, the reactor refrigerant chuck layer are mutually communicated,
Radial width is freely adjustable, and collet is supported by fixing bracket.
A kind of isothermal reactor process of convenient changing catalyst, the method includes be suitable for strong exothermal reaction,
The isothermal reactor process of convenient changing catalyst；The strong exothermal reaction, including but not limited to synthesis, hydrogenation reaction,
Such as synthesize ammonia, methanation, methanol-fueled CLC, oxidation or nitration reaction；Reactor liquid phase or gas phase heating agent include water, vapor,
Conduction oil, dense dissolved salt etc. are organic or inorganic can to pass hot medium.
A kind of isothermal reactor process of convenient changing catalyst, the methanol synthesis reaction, full bed
The layer temperature difference is lower than 3 DEG C.
A kind of isothermal reactor process of convenient changing catalyst, the methanation reaction, full bed
The temperature difference is lower than 3 DEG C.
The advantages and effects of the present invention are:
1. the present invention can not solve the problems, such as that non-uniform temperature field and field of flow are mutually matched shell-and-tube reactor, start
It is a kind of suitable for strong exothermal reaction, catalyst can convenient handling isothermal reactor design method, which can be ideally
Realize the stability contorting of reaction bed temperature gradient and non-equal field of flow.
2. the isothermal reaction device of the convenient changing catalyst of design method initiative of the present invention is not only applicable to common intensity
Process of absorption or liberation of heat reaction, be particularly suitable for strong exothermal reaction, such as: methanol-fueled CLC, preparing methane by synthetic gas and oxidation or nitration reaction
Deng can remove a large amount of reaction heat of generation in time, overtemperature and temperature runaway phenomenon is avoided to lead to sintering of catalyst and surface area
Charcoal.
3. the convenient disassembly of concentric circles isothermal reaction device catalyst of design method initiative of the present invention, Catalyst packing time
Foreshorten to a hour order of magnitude.
4. the isothermal reactor of the convenient changing catalyst of design method initiative of the present invention can replace original process complicated
The integrated reaction system of multistage insulation fixed bed reactor, significantly reduce equipment investment cost, save energy consumption.
Detailed description of the invention
Fig. 1 is isothermal reactor Catalyst packing sectional view of the present invention；
Fig. 2 is Catalyst packing state diagram in sieve of the present invention；
Fig. 3 is isothermal reactor unstripped gas of the present invention and refrigerant flow profile figure；
Fig. 4 is isothermal reactor collet aperture design drawing of the present invention.
Specific embodiment
The following describes the present invention in detail with reference to examples.
Reactor of the present invention is constructed using concentric circles, and every layer of concentric circles collet is relatively independent.The collet wall of annular has uniformly
The air hole of distribution, as reaction gas mass transfer path.Catalyst packing is then whole to be seated in collet into circular screen
Between, chuck layer is the refrigerants such as vapor or conduction oil.Reactor feed gas by concentric circles reactor internals surrounding radially into
In reactor, so that the minimum refrigerant of the most strongly exothermic amount corresponding temperature of initial reaction stage, concentric circles periphery loaded catalyst
The corresponding maximum heat exchange area of maximum, each chuck layer can regard relatively independent reaction compartment as, then after the convergence of product gas
Gas collecting tube discharge in the middle part of from reactor.
The isothermal reactor design and its method of a kind of convenient changing catalyst include 1) reactor set using concentric circles
Meter；2) in circular screen, sieve is integrally loaded into concentric circles reactor Catalyst packing, catalyst integral disassembly, assembly, convenient
Fast；3) unstripped gas is from concentric circles reactor surrounding radially into minimum cold of, the most strongly exothermic amount corresponding temperature of initial reaction stage
Matchmaker, concentric circles periphery loaded catalyst maximum correspond to maximum heat exchange area.
The concentric circles isothermal reactor includes pressure-bearing shell, high pressure resistant collet and closed circuit water route.
The concentric circles isothermal reactor pressure-bearing shell and high pressure resistant collet are pressure-resistant material, and the pressure-resistant upper limit is 30MPa.
The Catalyst packing that the concentric circles isothermal reactor uses is into circular screen.
The circular screen orifice diameter 0.5-5.0mm, mesh widths can freely regulate and control, and be convenient for catalyst radial direction single layer
Or multilayer filling.
The concentric circles isothermal reactor collet opens equally distributed round hole, square hole, strip-shaped hole or irregular hole,
It is refrigerant in collet.
The liquid phase or gas phase refrigerant includes: that water, vapor, conduction oil, dense dissolved salt etc. are organic or inorganic can
Pass hot medium.
The concentric circles isothermal reactor refrigerant chuck layer is mutually communicated, and radial width is freely adjustable, collet by
Fixed bracket support.
The concentric circles isothermal reactor includes but is not limited to various synthesis, hydrogenation reaction, such as synthesize ammonia, methanation,
Methanol-fueled CLC, oxidation or nitration reaction etc..
The specific design scheme of reactor:
The isothermal reactor of convenient changing catalyst is that have shell of reactor and internals to constitute, the cross section of internals such as Fig. 1 institute
Show, catalyst bed is alternately present with refrigerant bed, it is ensured that solid catalyst bed is completely encapsulated in refrigerant bed, catalyst
Radial bed can be loaded with single layer and also be loaded with multilayer.State of the Catalyst packing in sieve is as shown in Fig. 2, filling catalysis
The section of the circular screen of agent can be diameter not equal annular, and a certain section be also possible in annular, sieve is together with catalysis
Agent is integrally successively installed in concentric circles reactor.Unstripped gas and refrigerant enter mode such as Fig. 3 institute of reactor internals chuck layer
Show, unstripped gas from concentric circles reactor surrounding even into inside reactor internals, along radial by passing through catalyst bed
After layer, reactor is left after the collection of central gas collecting tube.Catalyst radial direction thickness of bed layer can be adjusted freely in sieve, if often
Layer catalyst is single layer filling, then the corresponding heat exchange area of the catalyst for being equivalent to unit volume is approximately equal.If urged
Agent Multi-layers distributing, for strong exothermal reaction, design principle be closer to reactor wall catalyst bed it is thinner, closer to anti-
Answer the catalyst bed at device center thicker.The effect reached is the corresponding heat-transfer surface of reactor radial outer per volume of catalyst
Product is consistent with internal layer catalyst.The catalyst bed being isolated in sieve can be 2 layers, is also possible to multilayer, at most can achieve
20 individual catalytic beds.Catalyst can uniformly be mixed with inert solid fillers and be filled out in reactor outermost layer sieve, and inertia is filled out
The effect of material is heat transfer carrier, quickly the heat that catalyst surface is enriched with can be distributed on inert carrier, with refrigerant collet
Contact promotes heat transfer efficiency, increases heat exchange area.
Isothermal reactor collet aperture mode as shown in figure 4, hole shape can be round hole, square hole, strip-shaped hole or
Irregular hole.Be passed through the heating agents such as water or conduction oil in collet, heating agent the type of flow can be upper entering and lower leaving, under being also possible to
Into it is upper go out.Heating agent is injected by pressure liquid pump, outlet connects drum, maximum 25 MPa of pressure-bearing, and after carrying out gas-liquid separation, steam can be with
It is directly used in power generation or driving steam turbine, steam pressure range is 4.0-20.0MPa, and liquid is after heat exchange is cooling through high pressure
In pump circulation to reactor.Once occur overheating problem in reactor, directly reduction drum outlet pressure, or even emptying drum,
Gasify rapidly by heating agent and take away excessive heat in reactor, reaches the equally distributed purpose of temperature of reactor.
Embodiment 1
By taking synthesising gas systeming carbinol as an example, unstripped gas group becomes 69.92%H2,29.26%CO, 3.11%CO2,0.13%CH4,0.57%
N2,0.004% methanol, 240 DEG C of reaction temperature, reaction pressure 6.0MPa, unstripped gas air speed 7500h-1, reaction gas recycle ratio is
3.86.Using the isothermal reactor of convenient changing catalyst, 20 kilograms of loaded catalyst, catalyst radial multilayer is filled in sieve
(radial layer 2-3) is filled out, low temperature, the low pressure methanol synthesis catalyst commercially produced using Shenyang University of Chemical Technology, isothermal reactor
The catalyst bed of outer layer and the reaction bed temperature of central gas collection inner tube layer are substantially without the temperature difference.According to real-time testing knot
Fruit, when and outer layer catalyst bed temperature is high, when and internal layer catalyst bed temperature is high, temperature difference is less than 3 DEG C.
Embodiment 2
By taking coke-stove gas methane as an example, unstripped gas group becomes 26.3%CH4,57.1%H2,7.7%CO, 2.7%CO2,3.2%N2,
0.5%O2,0.75%C2H6,1.75%C2H4,400 DEG C of reaction temperature, reaction pressure 1.5MPa, unstripped gas air speed 5500h-1, instead
Should gas recycle ratio be 1.75.Using the isothermal reactor of convenient changing catalyst, 20 kilograms of loaded catalyst, catalyst is radial
Multilayer loads (radial layer 2-3), the Catalyst for Low-Temperature Methanation that filling Chinese Academy of Sciences's process is commercially produced；Outside isothermal reactor
The catalyst bed of layer and the reaction bed temperature of central gas collection inner tube layer are substantially without the temperature difference.According to real-time testing as a result,
When and outer layer catalyst bed temperature is high, when and internal layer catalyst bed temperature is high, temperature difference is less than 3 DEG C.
The above is only several embodiments of the application, not does any type of limitation to the application, although this Shen
Please disclosed as above with preferred embodiment, however not to limit the application, any person skilled in the art is not taking off
In the range of technical scheme, a little variation or modification are made using the technology contents of the disclosure above and is equal to
Case study on implementation is imitated, is belonged in technical proposal scope.
Claims (6)
1. a kind of isothermal reactor of convenient changing catalyst, which is characterized in that the reactor uses concentric design；Catalysis
Agent is seated in circular screen, and sieve is integrally loaded into concentric circles reactor, catalyst integral disassembly, assembly；Unstripped gas is from concentric circles
Reactor surrounding is radially into the minimum refrigerant of the most strongly exothermic amount corresponding temperature of initial reaction stage, concentric circles periphery catalyst fills
The amount of filling out maximum corresponds to maximum heat exchange area；The reactor includes pressure-bearing shell, high pressure resistant collet and closed circuit water route；Reaction
Device pressure-bearing shell and high pressure resistant collet are pressure-resistant material, and the pressure-resistant upper limit is 30MPa；The Catalyst packing that reactor uses to annular
In sieve；Circular screen orifice diameter 0.5-5.0mm, mesh widths can freely regulate and control, and be convenient for catalyst radial direction single-layer or multi-layer
Filling；It is the catalyst of single-layer or multi-layer filling in reactor jacket, is refrigerant collet outside collet.
2. a kind of isothermal reactor of convenient changing catalyst according to claim 1, which is characterized in that the reactor
Collet opens equally distributed round hole, square hole, strip-shaped hole or irregular hole, is refrigerant in collet.
3. a kind of isothermal reactor of convenient changing catalyst according to claim 1, which is characterized in that the reactor
Refrigerant chuck layer is mutually communicated, and radial width is freely adjustable, and collet is supported by fixing bracket.
4. a kind of isothermal reactor process of convenient changing catalyst, which is characterized in that strong the method includes being suitable for
Exothermic reaction, convenient changing catalyst isothermal reactor process；The strong exothermal reaction, including but not limited to synthesis,
Hydrogenation reaction such as synthesizes ammonia, methanation, methanol-fueled CLC, oxidation or nitration reaction；Reactor liquid phase or gas phase heating agent include
Water, vapor, conduction oil, dense dissolved salt etc. are organic or inorganic can to pass hot medium.
5. a kind of isothermal reactor process of convenient changing catalyst according to claim 4, which is characterized in that institute
Methanol synthesis reaction is stated, the full bed temperature difference is lower than 3 DEG C.
6. a kind of isothermal reactor process of convenient changing catalyst according to claim 4, which is characterized in that institute
Methanation reaction is stated, the full bed temperature difference is lower than 3 DEG C.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113930266A (en) * | 2021-11-11 | 2022-01-14 | 曲靖市麒麟气体能源有限公司 | Improved methanation process |
| CN115414872A (en) * | 2022-08-11 | 2022-12-02 | 安徽润衍科技有限公司 | Tubular isothermal reactor and process for producing 1,2-pentanediol from 1, 2-cyclopentane oxide |
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| CN108554321A (en) * | 2018-05-04 | 2018-09-21 | 沈阳化工大学 | A kind of catalytic reactor reduced suitable for strongly exothermic volume |
| WO2018204338A1 (en) * | 2017-05-01 | 2018-11-08 | Chevron Phillips Chemical Company Lp | Selective poisoning of aromatization catalysts to increase catalyst activity and selectivity |
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| CN201200884Y (en) * | 2008-05-30 | 2009-03-04 | 吕仲明 | Axial flow plate-shell type isothermal reactor |
| CN103435006A (en) * | 2013-08-20 | 2013-12-11 | 湖南安淳高新技术有限公司 | High-CO high-conversion-rate isothermal shift reactor |
| CN105413592A (en) * | 2015-12-17 | 2016-03-23 | 北京烨晶科技有限公司 | Combined type fixed bed reactor and device formed thereby |
| CN105854736A (en) * | 2016-03-31 | 2016-08-17 | 湖南安淳高新技术有限公司 | An isothermal reactor |
| CN207025289U (en) * | 2016-12-14 | 2018-02-23 | 山东迅达化工集团有限公司 | Radial reactor with height self limiting temperature area |
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| CN207237941U (en) * | 2017-09-19 | 2018-04-17 | 江苏康博新材料科技有限公司 | A kind of rectifying column catalyst carrier arrangement |
| CN108554321A (en) * | 2018-05-04 | 2018-09-21 | 沈阳化工大学 | A kind of catalytic reactor reduced suitable for strongly exothermic volume |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113930266A (en) * | 2021-11-11 | 2022-01-14 | 曲靖市麒麟气体能源有限公司 | Improved methanation process |
| CN115414872A (en) * | 2022-08-11 | 2022-12-02 | 安徽润衍科技有限公司 | Tubular isothermal reactor and process for producing 1,2-pentanediol from 1, 2-cyclopentane oxide |
| CN115414872B (en) * | 2022-08-11 | 2023-11-03 | 安徽润衍科技有限公司 | Tubular isothermal reactor and method for producing 1,2-pentanediol from 1, 2-epoxypentane |
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