CN108607475A - A kind of preparing ethylene glycol by using dimethyl oxalate plus hydrogen reactor - Google Patents
A kind of preparing ethylene glycol by using dimethyl oxalate plus hydrogen reactor Download PDFInfo
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- CN108607475A CN108607475A CN201810402374.4A CN201810402374A CN108607475A CN 108607475 A CN108607475 A CN 108607475A CN 201810402374 A CN201810402374 A CN 201810402374A CN 108607475 A CN108607475 A CN 108607475A
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- blind pipe
- ethylene glycol
- dimethyl oxalate
- plus hydrogen
- preparing ethylene
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- 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
- B01J8/06—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 in tube reactors; the solid particles being arranged in tubes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
- C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
- C07C29/147—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof
- C07C29/149—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of carboxylic acids or derivatives thereof with hydrogen or hydrogen-containing gases
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00938—Flow distribution elements
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The present invention relates to a kind of preparing ethylene glycol by using dimethyl oxalate plus hydrogen reactor, including more reaction tubes, blind pipe (1) is equipped at the position for needing augmentation of heat transfer in the reaction tube.Compared with prior art, the present invention, which has, enhances heat transfer, avoids overreaction, design simply, optimize reactor bed axially and radially temperature the advantages that.
Description
Technical field
The present invention relates to a kind of reactors, more particularly, to a kind of preparing ethylene glycol by using dimethyl oxalate plus hydrogen reactor.
Background technology
Hydrogenation of Dimethyl Oxalate exothermic heat of reaction has stronger fuel factor.The reaction is more sensitive to temperature：If reaction temperature
Spend not high enough, raw material and intermediate product methyl glycollate are excessive in product, show as plus hydrogen is insufficient；And temperature is excessively high, then crosses and add
Hydrogen product ethanol and 1,2- butanediol contents rise.To be energy-saving, operation conditions optimization is needed in production, especially to temperature
Control, while improving feed stock conversion, also to control intermediate product and cross hydrogenation products concentration；To make list simultaneously
The production capacity of position bed volume is high as much as possible.Efficiently to remove reaction heat, existing Hydrogenation of Dimethyl Oxalate fixed bed device
Heat is generally moved using shell and tube reactor and steam jacket, there are two types of representative reaction pipe sizes at present：One is extra heavy pipe,
Internal diameter is 70mm；One is tubule, internal diameter is 38mm.
For cylindrical reaction tubes, heat-conducting area and the reaction tube diameter of unit bed volume are inversely proportional.Therefore, with it is thin
Reaction tube is compared, and the shifting thermal efficiency of crude reaction pipe (internal diameter 70mm) is lower, is limited by rate of heat transfer, and unit bed volume is most
Big production capacity is lower；Simultaneously as crude reaction pipe has bigger thermal resistance, radial symmetry gradient more notable.Cause in practical life
Extra heavy pipe reactor produce load is lower in production, and action pane is narrower.The especially unit bed volume of high activated catalyst
Thermal discharge higher, if using crude reaction pipe, the Wen Shenghui of center is excessively high, causes to go out in the region close to reactor outlet
Existing reaction tube center is crossed plus hydrogen, and the phenomenon that marginal zone adds hydrogen still insufficient.Consequence is that occur in final product, add hydrogen deficiency and
The worst operating mode for adding the excessive product of hydrogen excessively high.
On the other hand, it looks up from reactor bed axis, ideal bed temperature distribution should be that the front is high and the back is low：In entrance
Duan Fanying is still insufficient, and bed Wen Sheng caused by reaction heat is conducive to improve catalytic activity at this time, and bed can be improved in few heat of moving
Conversion ratio will not also cause to add hydrogen side reaction；And in reactor outlet section, terminate since main reaction is close, excessively high of temperature
It can accelerate the side reaction for adding hydrogen, should shorten the residence time at this time, while accelerate to move heat.Therefore, reactor design should needle
The characteristics of reaction, is optimized, section has different shifting thermal energy powers before and after making reactor, reaches and improves reaction conversion ratio, suppression
The effect of side reaction processed.
For ready-made factory, if replacement its cost of reactor and difficulty of construction are larger, and can be continuous if catalyst
It improves, active higher, selectivity and stability are also more preferable.But the superior function of raw catelyst tends not to and original reactor knot
Structure and size matching, cause the efficiency of raw catelyst to be difficult to play.
Invention content
It is an object of the present invention to overcome the above-mentioned drawbacks of the prior art and provide a kind of dimethyl oxalates to add
Hydrogen preparing ethylene glycol reactor.
The purpose of the present invention can be achieved through the following technical solutions：A kind of preparing ethylene glycol by using dimethyl oxalate plus hydrogen use is anti-
It answers device, including more reaction tubes, blind pipe is equipped at the position for needing augmentation of heat transfer in the reaction tube.
Further, the blind pipe occupies thermal resistance maximum, temperature in reaction tube and rises highest reaction zone, has and lowers bed heat
Resistance is homogenized the effect of bed radial temperature.
The blind pipe setting is in reaction tube center, and blind pipe is reducing blind pipe, and diameter needs to move with corresponding position
The amount of heat is proportional.Blind pipe diameter can be according to shifting heat request and catalyst filler particles size variation.Such as activity higher is urged
Agent, the volume that center blind pipe occupies is also bigger, but to consider the remaining ring-like gap of reaction tube and catalyst particle size phase
Matching.Catalyst particle size and shape are then according to factors such as catalytic activity, side reaction, diffusion limitation, pressure drop, manufacturing costs
It is determined after considering.Secondly, according to reaction characteristics, blind elbow length can be shortened, or in different height position using different
Outer diameter.For example, to leading portion need heat up back segment need move heat oxalate hydrogenation, can reaction tube entrance not
Dress uses the thinner blind pipe of caliber, and section and back segment in the reactor, the outer diameter substep of blind pipe amplify.If reaction is in leading portion
It is excessively fierce, and disappear in back segment fuel factor, reaction is not enough, and will then need reverse design at this time, i.e., outside the blind pipe of entrance
Diameter is maximum, and stage casing and back segment attenuate, or even cancels blind pipe in back segment.
Further, the structure of the blind pipe includes up-small and down-big reducing blind pipe or up big and down small reducing blind pipe.
Further, the up-small and down-big reducing blind pipe includes in up-small and down-big cone-like structure；Or by multiple
The different cylinder of internal diameter is sequentially increased according to internal diameter from top to bottom to be connected and composed；Or by multiple internal diameter difference cones and circle
Internal diameter is sequentially increased combination and connects and composes cylinder from top to bottom；The up big and down small reducing blind pipe includes being fallen in up big and down small
Cone-like structure；Or the different cylinder of multiple internal diameters is sequentially reduced according to internal diameter from top to bottom and connects and composes；Or by multiple
Internal diameter difference cone and cylinder are sequentially reduced combination according to internal diameter from top to bottom and connect and compose.
The blind pipe is mounted at the top of reaction tube or bottom.Blind pipe both ends are carried out by locating detent a and locating detent b respectively
Supports support can be also arranged in radial limit, blind pipe bottom, and support element can be spring, supporting rack, support column etc..
Further, it is equipped with cross supporting frame at the top of the blind pipe, connects at the top of the central point and blind pipe of cross supporting frame
It connects, four endpoints are fixed on reaction tube, and cross supporting frame provides axial upward pulling force for blind pipe.
Tapered cap is equipped at the top of the blind pipe so that catalyst is evenly dispersed when filling.
To mitigate weight, blind pipe inner hollow, wall thickness can be designed according to reaction pressure, between generally 1.5-3mm, port
Place's sealing is welded sealing；Blind pipe is hollow structure or the full heat-resisting inert substance of filling, high-purity fine sand, carbonization such as pickling
Silicon etc., or installation inner support frame, to resist external pressure.
The tube inner diameter d1=60~80mm, reaction tube usually larger to internal diameter add blind pipe.
The blind pipe use material identical with reaction tube or use chemical inert material for reduce make blind pipe at
Blind pipe of the closed aluminium alloy extrusions as filling can also be used under the premise of harmless to reaction result in this.
Compared with prior art, the present invention provides a kind of methods being transformed to existing crude reaction pipe, existing
Every reaction tube center install a blind pipe, before being changed without reactor, not reducing production capacity and deterioration reaction index
It puts, gives full play to the efficiency of high activated catalyst, greatly improve the economy of the reaction process；The outer diameter of blind pipe, length, peace
Holding position can need to optimize according to adjusting thermic load, select appropriate area to install blind pipe, can reduce the region catalyst
Loading and bed sectional area so that flow velocity of the material in the region increases, shorter residence time；It is occupied in reaction tube with blind pipe
Thermal resistance is maximum, temperature rises highest reaction zone, has and lowers bed thermal resistance, the effect of bed radial temperature is homogenized, in augmentation of heat transfer
Meanwhile reducing response intensity, avoid overreaction；The reactor design is simple, but can reach while optimize reactor
The effect of bed axially and radially Temperature Distribution, even if reaction effect can be obviously improved if being changed without catalyst and obtain bigger
Operating flexibility, the catalyst better to activity, it is more apparent to promote effect.
Description of the drawings
Fig. 1 is the structural schematic diagram of reaction tube in the present invention；
Fig. 2 is the reaction tube structural schematic diagram of the distribution of locating detent in the present invention；
Fig. 3 is to be equipped in the present invention by the reaction tube structural schematic diagram of thin thicker two-part blind pipe；
Fig. 4 is to be equipped in the present invention by the reaction tube structural schematic diagram of thin thicker three-stage blind pipe；
Fig. 5 is the reaction tube structural schematic diagram for being equipped with upper end in the present invention and having the blind pipe of shadoof；
Fig. 6 is the reaction tube structural schematic diagram that two-part blind pipe from the coarse to fine is equipped in the present invention；
Fig. 7 is the reaction tube structural schematic diagram that blind pipe is locally equipped in the present invention；
Fig. 8 is a kind of structural schematic diagram of reaction tube upper end in the present invention；
Fig. 9 is another structural schematic diagram of reaction tube upper end in the present invention.
In figure：1, blind pipe, 2, locating detent a, 3, locating detent b, 4, spring, 5, tapered cap, 6, cross supporting frame, 7, shadoof.
Specific implementation mode
The present invention is described in detail with specific embodiment below in conjunction with the accompanying drawings.
Embodiment 1
A kind of preparing ethylene glycol by using dimethyl oxalate plus hydrogen reactor, including more reaction tubes are needing to strengthen in reaction tube
The position of heat transfer is equipped with blind pipe 1.Blind pipe 1 occupies thermal resistance maximum, temperature in reaction tube and rises highest reaction zone, has and lowers bed heat
Resistance is homogenized the effect of bed radial temperature.Such as Fig. 1, for the setting of blind pipe 1 in reaction tube center, blind pipe 1 is in cylindrical shape,
Top is equipped with tapered cap 5 so that catalyst is evenly dispersed when filling.1 inner hollow of blind pipe, wall thickness can be set according to reaction pressure
It counts, is sealed between generally 1.5-3mm, at port and be welded sealing；Blind pipe 1 is using material identical with reaction tube or using chemistry
Inert material is that closed aluminium alloy type can also be used under the premise of harmless to reaction result in the cost of reduction making blind pipe 1
Blind pipe of the material as filling.
1 both ends of blind pipe carry out radial limit, locating detent a 2 and locating detent b by locating detent a 2 and locating detent b 3 respectively
3 structures are identical, including three mutual stabilizer blades in 120 degree of angles, as shown in Figure 2.1 bottom of blind pipe is supported by spring 4, is made
Blind pipe 1 occupies thermal resistance maximum, temperature in reaction tube and rises highest reaction zone, has and lowers bed thermal resistance, homogenizing bed radial temperature
Effect.
The latent active of catalyst of new generation doubles than raw catalyst and controls, and catalyst particle size is that 3.6mm is contour
Cylinder.In view of mass transfer and limit, when particle is made, the activity of industrial catalyst is about 1.5 times of former particle.Admission space can be with
It is designed as original 2/3, then the 1/3 of center blind pipe volumetric reaction pipe volume, corresponding a diameter of 40mm of blind pipe or so, blind pipe height
Degree is contour with reactor, as shown in Figure 1.Effect at this time is mainly reduction of radial symmetry gradient, expands action pane, can
To be operated under bigger temperature, pressure, hydrogen ester ratio, flow velocity, the selectivity without influencing purpose product and ethylene glycol.Reduce and urges
Agent dosage 1/3, but inventory and conversion ratio are constant, and ethylene glycol yield improves 1-2%.Center maximum temperature reduces by 10
℃。
Embodiment 2
Preparing ethylene glycol by using dimethyl oxalate plus hydrogen is exothermic reaction under the conditions of current Catalytic processes, and reactor uses shell and tube
Reactor, tube inner diameter d1=60~80mm.Reaction tube leading portion carries out moving hot back segment needs shifting heat at this time, works as leading portion
Shifting heat demand it is smaller when, leading portion uses the thinner blind pipe 1 of caliber, and section and back segment in the reactor, the outer diameter point of blind pipe 1
Step amplification, as shown in figure 3, blind pipe 1 is constituted by two different cylinders of diameter are setting up and down, under the diameter of upper cylinder is less than
The diameter of cylinder, the connecting tube of two cylinder transition region setting taper types, the edge slope of the taper and the gradient of Wen Sheng
It is corresponding.The final center temperature that reduces rises 5-10 DEG C, reduces intermediate product 20-40%, reduced hydrogenation products 10-50%, and led
The yield of purpose product is caused to improve 1-2%, and catalyst space velocities can improve 50%-100%.Since catalyst efficiency is carried
It rises, original two one group of concatenated reactors can be made into two groups of reactors in parallel, reach original with a reactor
The effect of two reactors, or reduce 20% catalyst amount.
Embodiment 3
When needing to carry out the shifting heat operation of multistage difference, multistage reducing blind pipe can be set, there are 2~3 kinds of diameters, such as schemed
Shown in 4,1 top of multistage reducing blind pipe is most thin, and bottom is most thick.The outer diameter of epimere 30% is 10mm, and stage casing 30% is 20mm, hypomere
40% is 40mm, and transition region is the taper draw between section.Result is optimal at this time.Catalyst amount reduces 20% or so, space-time production
Rate improves 1 times, from 0.3kg ethylene glycol/kg cat/h, is increased to 0.6kg ethylene glycol/kg cat/h or more, yield is carried from 96%
For height to 98%, maximum temperature point reduces 5 DEG C.
Embodiment 4
Be different from embodiment 2, when preparing ethylene glycol by using dimethyl oxalate plus hydrogen reaction leading portion using activity it is relatively low, selectivity compared with
When high catalyst, demand of the leading portion to heat is larger, therefore need not carry out moving heat, can change the thinner blind pipe of leading portion caliber 1
For shadoof 7, as shown in Figure 5 so that the heat that leading portion obtains increases, catalytic reaction activity enhancing.
Embodiment 5
It is different from embodiment 2, reaction is excessively fierce in leading portion, and disappears in back segment fuel factor, and reaction is not enough, at this time
Reverse design, i.e. 1 largest outside diameter of blind pipe of entrance, stage casing and back segment will be then needed to attenuate, i.e., by the different round columns of multiple internal diameters
Body is sequentially reduced combination according to internal diameter from top to bottom and connects and composes, as shown in fig. 6, can to shorten blind elbow length as shown in Figure 7.
Embodiment 6
When blind pipe is heavier, cross supporting frame 6, as shown in figs. 8 and 9, the center of cross supporting frame 6 is arranged in 1 top of blind pipe
Point is connect with 1 top of blind pipe, and four endpoints are fixed on reaction tube, and cross supporting frame is that blind pipe 1 provides axial pull up
Power.
Embodiment 7
To being partly equipped with the reaction tube of fixed multipoint temperature monitor test tube in reactor, do not have to separately add blind pipe, it is only necessary to
The outer diameter thermometer test tube consistent with blind pipe is installed.
Embodiment 8
When reaction pressure is higher, the hollow structure of blind pipe 1 is packed into heat-resisting inert substance, it is high-purity such as pickling
Fine sand, silicon carbide etc., or installation inner support frame are spent, to resist external pressure.
The structure of blind pipe 1 can be up-small and down-big reducing blind pipe or up big and down small reducing blind pipe；Up-small and down-big reducing blind pipe
Include in up-small and down-big cone-like structure；Or it is sequentially increased according to internal diameter from top to bottom by the different cylinder of multiple internal diameters
It connects and composes；Or by multiple internal diameter difference cones and cylinder from top to bottom internal diameter be sequentially increased combination connect and compose etc. it is more
Kind different structure, the outer diameter of blind pipe, length, installation site can need to optimize according to adjusting thermic load.Its objective is
Thermal resistance maximum, temperature in reaction tube are occupied with blind pipe and rises highest reaction zone, are had and are lowered bed thermal resistance, homogenizing bed radial temperature
Effect.Secondly, it selects appropriate area that blind pipe is installed, the region catalyst loading and bed sectional area can be reduced, lead to material
Flow velocity in the region increases, shorter residence time；While augmentation of heat transfer, reduce response intensity.Its effect is to inhibit
The fuel factor in the region avoids overreaction.The design is simple, but can reach while optimize reactor bed axial direction and diameter
To the effect of Temperature Distribution.Even if reaction effect can be obviously improved if being changed without catalyst and obtain bigger operating flexibility, and its
Another advantage is that the catalyst better to activity, it is more apparent to promote effect.
Claims (10)
1. a kind of preparing ethylene glycol by using dimethyl oxalate plus hydrogen reactor, including more reaction tubes, which is characterized in that the reaction
In pipe blind pipe (1) is equipped at the position for needing augmentation of heat transfer.
2. a kind of preparing ethylene glycol by using dimethyl oxalate plus hydrogen reactor according to claim 1, which is characterized in that described
Blind pipe (1) occupies thermal resistance maximum, temperature in reaction tube and rises highest reaction zone, has and lowers bed thermal resistance, is homogenized bed radial temperature
Effect.
3. a kind of preparing ethylene glycol by using dimethyl oxalate plus hydrogen reactor according to claim 1, which is characterized in that described
In reaction tube center, blind pipe (1) is reducing blind pipe for blind pipe (1) setting, and the amount that diameter needs shifting hot with corresponding position is in
Direct ratio.
4. a kind of preparing ethylene glycol by using dimethyl oxalate plus hydrogen reactor according to claim 1 or 2 or 3, which is characterized in that
The structure of the blind pipe (1) includes up-small and down-big reducing blind pipe or up big and down small reducing blind pipe.
5. a kind of preparing ethylene glycol by using dimethyl oxalate plus hydrogen reactor according to claim 4, which is characterized in that described
Up-small and down-big reducing blind pipe includes in up-small and down-big cone-like structure；Or by the different cylinder of multiple internal diameters according to from upper
It is sequentially increased and connects and composes to lower internal diameter；Or increased successively according to internal diameter from top to bottom by multiple internal diameter difference cones and cylinder
Big combination connects and composes；
The up big and down small reducing blind pipe includes in up big and down small reverse taper shape structure；Or the cylinder that multiple internal diameters are different
Body is sequentially reduced according to internal diameter from top to bottom and connects and composes；Or by multiple internal diameter difference cones and cylinder internal diameter from top to bottom
Combination is sequentially reduced to connect and compose.
6. a kind of preparing ethylene glycol by using dimethyl oxalate plus hydrogen reactor according to claim 1, which is characterized in that described
Blind pipe (1) is mounted at the top of reaction tube or bottom.
7. a kind of preparing ethylene glycol by using dimethyl oxalate plus hydrogen reactor according to claim 6, which is characterized in that described
Blind pipe (1) both ends carry out radial limit by locating detent a (2) and locating detent b (3) respectively, and support can be also arranged in blind pipe (1) bottom
Part.
8. a kind of preparing ethylene glycol by using dimethyl oxalate plus hydrogen reactor according to claim 6, which is characterized in that described
It is equipped with cross supporting frame (6) at the top of blind pipe (1), is connect at the top of the central point and blind pipe (1) of cross supporting frame (6), four ends
Point is fixed on reaction tube, and cross supporting frame is that blind pipe (1) provides axial upward pulling force.
9. a kind of preparing ethylene glycol by using dimethyl oxalate plus hydrogen reactor according to claim 1, which is characterized in that described
Tapered cap (5) is equipped at the top of blind pipe (1) so that catalyst is evenly dispersed when filling.
10. a kind of preparing ethylene glycol by using dimethyl oxalate plus hydrogen reactor according to claim 2, which is characterized in that described
Blind pipe (1) be hollow structure or the full heat-resisting inert substance of filling, blind pipe (1) wall thickness is 1.5-3mm, is sealed at port；
The tube inner diameter d1=60~80mm；
The blind pipe (1) is using material identical with reaction tube or uses chemical inert material.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201810402374.4A CN108607475A (en) | 2018-04-28 | 2018-04-28 | A kind of preparing ethylene glycol by using dimethyl oxalate plus hydrogen reactor |
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6154229A (en) * | 1984-08-24 | 1986-03-18 | Mitsubishi Heavy Ind Ltd | Reactor |
| CN1531458A (en) * | 2001-08-02 | 2004-09-22 | Bp | Flow reactors for chemical conversions with hetergeneous catalysts |
| CN101351527A (en) * | 2005-12-19 | 2009-01-21 | 英国石油勘探动作有限公司 | Process for producing condensed-phase product from one or more gas-phase reactants |
| CN102649697A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for preparing ethylene glycol through oxalate gas phase hydrogenation |
| CN102741379A (en) * | 2010-02-01 | 2012-10-17 | 英弗勒科技有限公司 | Process for producing synthetic liquid hydrocarbons and reactor for fischer-tropsch synthesis |
| CN103209760A (en) * | 2011-10-12 | 2013-07-17 | 曼柴油机和涡轮机欧洲股份公司 | Shell-and-tube reactor for carrying out catalytic gas phase reactions |
| CN105705229A (en) * | 2013-11-07 | 2016-06-22 | 株式会社日本触媒 | Packing for reaction tube, reaction tube, and reaction method using same |
| CN208591817U (en) * | 2018-04-28 | 2019-03-12 | 上海奕玛化工科技有限公司 | Preparing ethylene glycol by using dimethyl oxalate plus hydrogen reactor |
-
2018
- 2018-04-28 CN CN201810402374.4A patent/CN108607475A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6154229A (en) * | 1984-08-24 | 1986-03-18 | Mitsubishi Heavy Ind Ltd | Reactor |
| CN1531458A (en) * | 2001-08-02 | 2004-09-22 | Bp | Flow reactors for chemical conversions with hetergeneous catalysts |
| CN101351527A (en) * | 2005-12-19 | 2009-01-21 | 英国石油勘探动作有限公司 | Process for producing condensed-phase product from one or more gas-phase reactants |
| CN102741379A (en) * | 2010-02-01 | 2012-10-17 | 英弗勒科技有限公司 | Process for producing synthetic liquid hydrocarbons and reactor for fischer-tropsch synthesis |
| CN102649697A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for preparing ethylene glycol through oxalate gas phase hydrogenation |
| CN103209760A (en) * | 2011-10-12 | 2013-07-17 | 曼柴油机和涡轮机欧洲股份公司 | Shell-and-tube reactor for carrying out catalytic gas phase reactions |
| CN105705229A (en) * | 2013-11-07 | 2016-06-22 | 株式会社日本触媒 | Packing for reaction tube, reaction tube, and reaction method using same |
| CN208591817U (en) * | 2018-04-28 | 2019-03-12 | 上海奕玛化工科技有限公司 | Preparing ethylene glycol by using dimethyl oxalate plus hydrogen reactor |
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