CN105903414A - Slurry-bed reactor for preparing ethylene - Google Patents
Slurry-bed reactor for preparing ethylene Download PDFInfo
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- CN105903414A CN105903414A CN201610417615.3A CN201610417615A CN105903414A CN 105903414 A CN105903414 A CN 105903414A CN 201610417615 A CN201610417615 A CN 201610417615A CN 105903414 A CN105903414 A CN 105903414A
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- reactor
- liquid
- sieve plate
- gas
- downflow weir
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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
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
- B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
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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
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/08—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds
- C07C5/09—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds to carbon-to-carbon double bonds
-
- 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
- B01J2208/00823—Mixing elements
- B01J2208/00831—Stationary elements
- B01J2208/0084—Stationary elements inside the bed, e.g. baffles
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention relates to a slurry-bed reactor for preparing ethylene. The slurry-bed reactor comprises a shell, a heater and sieve plates, and the lower portion of the shell is provided with a reaction gas inlet, a liquid solvent inlet and a liquid outlet; the upper portion of the shell is provided with a gas outlet and a liquid inlet; the heater is arranged on the lower portion in the shell, and the sieve plates are located in the shell, fixed on the inner wall of the shell and located below the liquid inlet and above the reaction gas inlet and the liquid solvent inlet. According to the slurry-bed reactor for preparing ethylene by means of selective hydrogenation of acetylene, a gas phase and a liquid phase of the slurry-bed reactor are in the reverse-flow direction integrally, and mass transfer and heat transfer effects are improved. Due to the fact that multiple layers of the sieve plates are arranged in the reactor, the contact area of sufficient contact among the gas phase, the liquid phase and a solid phase is increased, gas-liquid flow field distribution is improved, a flow-direction short circuit of a fluid is avoided, turbulent motion and gas-liquid mass transfer can be strengthened, and the fluidization quality in the reactor is improved.
Description
Technical field
Present invention relates generally to paste state bed reactor, be specifically related to a kind of slurry bed system preparing ethylene anti-
Answer device.
Background technology
Ethylene is a kind of important basic material in modern industry, is also the chemistry of world wide production maximum
One of product, its product is widely used in the fields such as national economy, people's lives, national defence, is " to have
The mother of machine synthesis ".In the face of the shortage of petroleum resources and riseing of international oil price, raw material sources become
The bottleneck of development ethylene industry, is also to put the problem that must solve in face of people.Therefore, research
Develop a kind of new Technology to prepare ethylene, to be allowed to petroleum replacing as industrial raw materials,
The modern industry dependency to oil can be alleviated.
In coal chemical technology, with coal for raw material by carbide technique, or lead to natural gas for raw material
Cross non-catalytic partial oxidation technique and produce acetylene, it has also become maturation process.Again with acetylene as raw material,
Under the effect of selective hydrocatalyst, obtain ethylene product by hydrogenation process, can be further
Expand Coal Chemical Industry Route.Therefore, the novel technique of exploitation producing ethylene with acetylene hydrogenation, have wide
Application prospect.
Low concentration acetylene gas solid catalysis hydrogen addition technology is the most highly developed, mainly uses
Removing acetylene impurities in ethylene, the reactor of use is fixed bed reactors, fills in the reactor
Fill out solid-phase catalyst and carry out gas-solid phase reaction.But owing to ethyne reactive is high, hydrogenation reaction thermal discharge is big,
Even there is a small amount of acetylene in cracking gas, traditional gas-solid fixes bed hydroprocessing reactor and still suffers from
The serious problems such as green oil generating amount is big, catalyst cycle period is short, reactor easily " temperature runaway ".
Prior art one is fluidized-bed process and the device of a kind of producing ethylene with acetylene hydrogenation.This technique bag
Include following steps: in fluidized-bed reactor, add catalyst and diluent；Catalyst is risen
Temperature reduction；Acetylene and hydrogen mixture are passed through fluidized-bed reactor；Selective hydrogenation of acetylene generates
Ethylene；Cooling medium is passed through reactor heat exchange component to remove reaction heat；Isolated ethylene produces
Product.This Technology has the disadvantage in that
Preparing ethylene by selective hydrogenation of acetylene is strong exothermal reaction, although cooling medium is used in the process
The substantial amounts of heat released during to remove reaction, but still it is difficult to be completely eliminated local when reacting
The hidden danger that gas temperature is too high；
The fluid bed used because of this technique, is just difficult to avoid that the mutual sharp impacts of catalyst particles intergranular,
This can bring the loss of catalyst, increase the difficulty of dedusting, increase heat exchange component and the mill of reactor
The problems such as damage.
Prior art two is continuously separated production line, including oxygen hydrogenation reactor, cracking for a kind of ethylene
Gas the second exsiccator, removal of mercaptans/cos reactor, dearsenization reactor, acetylene hydrogenation reactor.
The reactor that its acetylene hydrogenation reactor used is used is fixed bed reactors.It is merely able to process
The acetylene of low concentration, and treating capacity is smaller；If acetylene content increase, can generate a large amount of green oil,
Cause the problem that catalyst cycle period shortens, even there will be reactor " temperature runaway ".
Therefore, so that reactor adapts to larger amount of reaction acetylene gas, do not have anti-
The problem answering device " temperature runaway ", fundamentally improves gas-liquid flow field distribution, and strengthening turbulence passes with gas-liquid
Matter, the quality fluidized in improving reactor, it is necessary to propose a kind of new reactor preparing ethylene.
Summary of the invention
It is an object of the invention to provide a kind of paste state bed reactor preparing ethylene, existing to solve
Technology employing fixed bed reactors or fluidized-bed reactor are prepared ethylene and are made internal heat be difficult to pass
The problem gone out.
The invention provides a kind of paste state bed reactor preparing ethylene.Described paste state bed reactor includes
Housing, heater and sieve plate, the bottom of described housing be provided with reaction gas inlet, liquid flux entrance,
Liquid outlet；The top of described housing is provided with gas outlet and liquid inlet；Described heater is arranged on
Bottom in described housing；Described sieve plate is positioned at described housing, is fixed in described inner walls,
It is positioned under described liquid inlet, on described reaction gas inlet, described liquid flux entrance.
Above-mentioned reactor, described inside reactor is dispersed with the sieve plate that multilamellar is parallel to each other, adjacent layer
Sieve plate between spaced, the interval of each layer sieve plate is equal.
Above-mentioned system, every layer of described sieve plate includes seal pot, bubbling area, downflow weir and downspout；
Wherein, the part edge of described sieve plate is fixed with described inner walls, described fixing part edge with
The part that described downflow weir fences up is seal pot, for holding the liquid flowed down from downspout described in upper strata
Body；The centre of described seal pot is distributed sieve aperture, forms bubbling area, and described bubbling area is gas-liquid
The main region of reaction；Described downflow weir is located at revocable edge of described sieve plate, described downflow weir
Higher than the seal pot of place layer, for keeping the height of liquid on every layer of described sieve plate；Described downspout
For making liquid flow to the seal pot of sieve plate described in lower floor from the downflow weir of sieve plate described in upper strata, it is positioned at institute
State the side of downflow weir.
Further, the described downspout of above-mentioned reactor is by the downflow weir of described sieve plate and described reaction
The gap of device inwall is formed.
Further, described sieve aperture is equally distributed circular aperture, and the centre-to-centre spacing of described aperture is hole
1-5 times of footpath, a diameter of 5-20mm of described aperture.
Above-mentioned reactor, the sieve aperture of described sieve plate can be provided with float valve or bubble-cap.
Above-mentioned reactor, the bottom of the downspout of sieve plate described in upper strata is not higher than sieve plate described in lower floor and overflows
The height on stream weir.
Further, the described downspout of described reactor adjacent layer is in the side being perpendicular to described seal pot
Being projected on circumferential angle upwards is staggeredly arranged.
Above-mentioned reactor, described heater be electric heater, steam heater, flue gas heater or
Hotline heater.
The beneficial effects of the present invention is, it is anti-that the present invention proposes a kind of new slurry bed system preparing ethylene
Answer device, this paste state bed reactor simple in construction, owing to reactor having multiple sieve plate, increase gas
The contact area that liquid-solid three-phase is fully contacted, improves gas-liquid flow field distribution, it is to avoid fluid flows to short circuit,
But also turbulence and gas-liquid mass transfer can be strengthened, the quality fluidized in improving reactor.Make to utilize
Paste state bed reactor carries out high concentration selective hydrogenation of acetylene and becomes the life of a kind of important alkene processed
Product approach.
Accompanying drawing explanation
Fig. 1 is the structural representation that technical solution of the present invention prepares the paste state bed reactor of ethylene；
Fig. 2 is the plan structure schematic diagram of sieve plate in technical solution of the present invention；
Wherein: 1, reaction gas inlet；2, liquid outlet；3, gas outlet；4, liquid enters
Mouthful；5, sieve plate；6, downspout；7, heater；8, solvent liquid entrance.
Detailed description of the invention
Below in conjunction with drawings and Examples, the detailed description of the invention of the present invention is carried out more detailed
Explanation, so as to the advantage being more fully understood that the solution of the present invention and its various aspects.But,
Specific embodiments described below and embodiment are only descriptive purposes rather than to the present invention
Limit.
If Fig. 1 is the structure chart of the paste state bed reactor in the present invention.The principle of paste state bed reactor
Be gas with bubbling form by being suspended with liquid (serosity) layer of solid fine grain, contrary to realize gas-liquid-solid
Answer the reactor of process.
The present invention is for the paste state bed reactor of preparing ethylene by selective hydrogenation of acetylene, and described slurry bed system is anti-
Device is answered to include reactor shell, heater 7 and sieve plate 5.
Reactor shell bottom is provided with reaction gas inlet 1, solvent liquid entrance 8 and liquid discharge
Mouth 2, gas outlet 3 is arranged at reactor shell top.
At the bottom having heaters 7 of reactor, it penetrates in reactor enclosure body.Wherein, heater
7 can make solvent evaporate, it is provided that the steam air-flow risen continuously, provide for whole reactor simultaneously
Thermal source.
Described sieve plate 5 is positioned at described housing, is fixed in described inner walls, is positioned at described liquid
Under entrance 4, on described reaction gas inlet 1, described liquid flux entrance 8.
Middle part in reactor enclosure body, is evenly distributed sieve plate 5.Every layer of sieve plate 5 has
Seal pot, downflow weir, downspout 6 and bubbling area.The part edge of sieve plate is fixed with inner walls,
Revocable edge is provided with downflow weir.The part that fixing part edge and described downflow weir fence up is
Seal pot, for holding the liquid flowed down from upper strata downspout.
The top view of sieve plate 5 is as shown in Figure 2.Effect at the downflow weir of one end of sieve plate 5 is to protect
Hold the liquid having certain altitude on every layer of sieve plate.It is next to downspout 6 at downflow weir.Specifically,
Downspout 6 can be formed by the gap of the downflow weir of described sieve plate Yu described reactor wall.Certainly descending liquid
It is such as pipeline configuration that pipe 6 may also be other structure.The effect of downspout 6 is to allow liquid from upper sieve
The seal pot of lower floor's sieve plate it is flow at the downflow weir of plate.The bottom of the downspout 6 of upper strata sieve plate 5 is not
Height higher than adjacent lower sieve plate 5 downflow weir.So design is to realize fluid-tight, i.e. prevents
Gas rises at downspout 6 causes each layer gas to connect and short-circuit.Central region on sieve plate 5
For bubbling area, it is uniform-distribution with circular aperture.Aperture is the main thoroughfare that gas rises, energy
Enough make gas and liquid uniform contact.
Described downspout 6 being projected on the direction being perpendicular to described seal pot of reactor adjacent layer
It is staggeredly arranged on circumferential angle.The most conveniently realize the liquid that upper strata sieve plate 5 flows down be stored in adjacent under
Layer sieve plate 5 upper certain time, until liquid exceeds the downflow weir of this lower floor and flows out to the sieve of lower floor again
Plate 5.
Aperture can keep pitching row's state with the flow direction of liquid, and the arrangement mode of aperture can be positive triangle
Formula.Small hole center is away from for 1-5 times of aperture, and the centre-to-centre spacing between preferred hole is 1.5 times；Hole
A diameter of 10mm in the preferred hole of a diameter of 5-20mm.
The sieve aperture of sieve plate also can be provided with float valve or bubble-cap.Float valve can float on sieve plate, with
The change of gas flow and change its open degree.Riser is had, at bubble-cap and riser in bubble-cap
Between formed rotary space.Riser is fixed on sieve plate, and gas phase enters revolution sky by riser
Between, sprayed by slot with certain spouting velocity, form bubbling with the liquid on sieve plate and contact.
When preparing ethylene, the gaseous mixture of acetylene and hydrogen is by the reaction gas bottom paste state bed reactor
Body entrance 1 enters in reactor；Reacting gas passes through inside reactor together along with solvent vapo(u)r
Sieve plate on aperture enter among liquid phase.Wherein solvent vapo(u)r is by the heater of reactor bottom
7 liquid flux heating evaporations and generate.Catalyst and the liquid on carrier solvent autoreactor top
Entrance 4 flows into.Because aperture is equally distributed on sieve plate 5, so reacting gas is the most therewith
Evenly spread in the middle of liquid.In a liquid, reacting gas catalyst in being suspended in liquid
React under catalytic action.Reacted gas departs from this layer of sieve plate 5, then by upper strata sieve plate
The aperture of 5 enters in the middle of supernatant liquid.The most repeatedly until passing through reactor sieve plate topmost
5, go out from the gas outlet 3 of reactor top.
In the reactor, gas be to lower and on the flow direction, liquid is the flow direction from top to down, gas
Present the direction of adverse current mutually with liquid phase entirety, increase the effect of mass transfer and heat transfer.Due to reaction
Device has multiple sieve plate, namely means reactor also exists multiple little slurry reactor
Device, increases the contact area that gas-liquid-solid three-phase is fully contacted, and improves gas-liquid flow field distribution, keeps away
Exempt from short circuit, but also turbulence and gas-liquid mass transfer can be strengthened, the quality fluidized in improving reactor.
From reactor top reaction gas out, more i.e. can get product ethylene by condensation, separation.
After the solvent of reactor bottom carries out reclaiming filtration by liquid outlet 2, can be by catalyst
Filter out from solvent.Solvent after filtration is recycling.
In the present embodiment, the solvent of use is distilled water (electrical conductivity ＜ 5 μm/cm).From instead
Answering the steam of rising bottom device is the thermal source of whole reactor, keeps the most stable of system temperature.
When starting selective hydrogenation of acetylene reaction, the substantial amounts of heat of releasing, can be by the evaporation of solvent
Shift, it is to avoid local temperature is too high.
The heater of reactor of the present invention can be electric heater, steam heater, flue gas heater or lead
Hot oil.
Compared with the technology of acetylene hydrogenation a small amount of with current ethylene, this technology can realize by high concentration
Preparing ethylene by selective hydrogenation of acetylene, expands the technology path of Coal Chemical Industry further.
Further, in the reactor of technical solution of the present invention, gas be to lower and on the flow direction,
Liquid is the flow direction from top to down, and gas phase and liquid phase entirety present the direction of adverse current, increase biography
Matter and the effect of heat transfer.
Further, the reactor of technical scheme there is multiple sieve plate, namely means
And reactor also exists multiple little paste state bed reactor, increase gas-liquid-solid three-phase and be fully contacted
Contact area, improve gas-liquid flow field distribution, short circuit can be avoided, but also turbulence can be strengthened
With gas-liquid mass transfer, the quality fluidized in improving reactor.
Technical scheme utilize liquid phase solvent sensible heat (sensible heat refer to when this heat add or
After removing, the change of mass temperature can be caused, and do not undergo phase transition), heat-sinking capability significantly improves,
The heat produced because selective hydrogenation of acetylene generates ethylene can be quickly moved out, reduce reaction bed
Temperature, improves conversion ratio and the selectivity of ethylene of acetylene.
It addition, the reactor heating system of the technical program is simple, only rely on adding of reactor bottom
Hot device 7 can be realized as heat supply.
In a word, the present invention provide paste state bed reactor, carry out selective hydrogenation of acetylene reaction time,
The catalyst that can cause because of exothermic reaction during preferably suppressing preparation of ethylene through selective hydrogenation of acetylene
The appearance of focus in bed, and then avoid catalysqt deactivation, improve the stability of catalyst.This
It is easy that the equipment of bright proposition solves reactor in preparing ethylene by selective hydrogenation of acetylene reacts well
The problem of " temperature runaway ", and due to the mutual sharp impacts of catalyst particles intergranular in fluid bed, and cause
The loss of catalyst, the difficulty of dedusting and the corrasion due to solid particle, cause heat exchange component
Problem with the serious wear of reactor.
Last it is noted that obvious, above-described embodiment is only for clearly demonstrating institute of the present invention
The citing made, and not restriction to embodiment.Those of ordinary skill in the field are come
Say, can also make other changes in different forms on the basis of the above description.Here
Without also cannot all of embodiment be given exhaustive.And thus amplified out obvious
Change or change among still in protection scope of the present invention.
Claims (9)
1. the paste state bed reactor preparing ethylene, it is characterised in that described paste state bed reactor bag
Include housing, heater and sieve plate,
The bottom of described housing is provided with reaction gas inlet, liquid flux entrance, liquid outlet；Described
The top of housing is provided with gas outlet and liquid inlet；
Described heater is arranged on the bottom in described housing；
Described sieve plate is positioned at described housing, is fixed in described inner walls, is positioned at described liquid and enters
Under Kou, on described reaction gas inlet, described liquid flux entrance.
Reactor the most according to claim 1, it is characterised in that described inside reactor is distributed
The sieve plate that multilamellar is parallel to each other, spaced between the sieve plate of adjacent layer, the interval of each layer sieve plate is equal.
Reactor the most according to claim 1, it is characterised in that every layer of described sieve plate includes being subject to
Liquid dish, bubbling area, downflow weir and downspout；Wherein, the part edge of described sieve plate and described housing
Inwall is fixed；
The part that described fixing part edge and described downflow weir fence up is seal pot, is used for holding
The liquid flowed down from downspout described in upper strata；
The centre of described seal pot is distributed sieve aperture, forms bubbling area, and described bubbling area is gas-liquid
The main region of reaction；
Described downflow weir is located at revocable edge of described sieve plate, and described downflow weir is higher than place layer
Seal pot；Described downflow weir is for keeping the height of liquid on every layer of described sieve plate；
Described downspout is for making liquid flow to sieve plate described in lower floor from the downflow weir of sieve plate described in upper strata
Seal pot, is positioned at the side of described downflow weir.
Reactor the most according to claim 3, it is characterised in that described downspout is by described sieve
The downflow weir of plate is formed with the gap of described reactor wall.
Reactor the most according to claim 3, it is characterised in that described sieve aperture is for being uniformly distributed
Circular aperture, the centre-to-centre spacing of described aperture is 1-5 times of aperture, a diameter of 5-20mm of described aperture.
Reactor the most according to claim 3, it is characterised in that the sieve aperture of described sieve plate is provided with
Float valve or bubble-cap.
Reactor the most according to claim 3, it is characterised in that the descending liquid of sieve plate described in upper strata
The bottom of pipe is not higher than the height of sieve plate downflow weir described in lower floor.
Reactor the most according to claim 3, it is characterised in that the described downspout of adjacent layer
Being projected on circumferential angle on the direction being perpendicular to described seal pot is staggeredly arranged.
Reactor the most according to claim 1, it is characterised in that described heater is electrical heating
Device, steam heater, flue gas heater or hotline heater.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610417615.3A CN105903414A (en) | 2016-06-14 | 2016-06-14 | Slurry-bed reactor for preparing ethylene |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610417615.3A CN105903414A (en) | 2016-06-14 | 2016-06-14 | Slurry-bed reactor for preparing ethylene |
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|---|---|---|---|---|
| US20020198430A1 (en) * | 2000-07-12 | 2002-12-26 | Technip-Coflexip | Process and installation for recovery and purification of ethylene produced by pyrolysis of hydrocarbons, and gases obtained by this process |
| US20090234167A1 (en) * | 2008-03-14 | 2009-09-17 | Catalytic Distillation Technologies | Process for converting methane to ethylene |
| CN102489255A (en) * | 2011-11-24 | 2012-06-13 | 济南大学 | Preparation method for metal wire solid-phase micro-extraction fiber of noble metal nanometer material-ionic liquid composite functional coating |
| CN103044179A (en) * | 2012-12-19 | 2013-04-17 | 清华大学 | Method for preparing ethylene through liquid-phase selective hydrogenation of acetylene in slurry reactor |
| CN104826558A (en) * | 2015-05-15 | 2015-08-12 | 北京神雾环境能源科技集团股份有限公司 | Slurry bed reactor and reaction system for producing ethylene by using acetylene selective hydrogenation |
| CN105175208A (en) * | 2015-08-07 | 2015-12-23 | 北京神雾环境能源科技集团股份有限公司 | Method for preparation of ethylene from hydrogenation of acetylene and reaction tower for the method |
| CN205700485U (en) * | 2016-06-14 | 2016-11-23 | 北京神雾环境能源科技集团股份有限公司 | A kind of paste state bed reactor preparing ethylene |
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2016
- 2016-06-14 CN CN201610417615.3A patent/CN105903414A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20020198430A1 (en) * | 2000-07-12 | 2002-12-26 | Technip-Coflexip | Process and installation for recovery and purification of ethylene produced by pyrolysis of hydrocarbons, and gases obtained by this process |
| US20090234167A1 (en) * | 2008-03-14 | 2009-09-17 | Catalytic Distillation Technologies | Process for converting methane to ethylene |
| CN102489255A (en) * | 2011-11-24 | 2012-06-13 | 济南大学 | Preparation method for metal wire solid-phase micro-extraction fiber of noble metal nanometer material-ionic liquid composite functional coating |
| CN103044179A (en) * | 2012-12-19 | 2013-04-17 | 清华大学 | Method for preparing ethylene through liquid-phase selective hydrogenation of acetylene in slurry reactor |
| CN104826558A (en) * | 2015-05-15 | 2015-08-12 | 北京神雾环境能源科技集团股份有限公司 | Slurry bed reactor and reaction system for producing ethylene by using acetylene selective hydrogenation |
| CN105175208A (en) * | 2015-08-07 | 2015-12-23 | 北京神雾环境能源科技集团股份有限公司 | Method for preparation of ethylene from hydrogenation of acetylene and reaction tower for the method |
| CN205700485U (en) * | 2016-06-14 | 2016-11-23 | 北京神雾环境能源科技集团股份有限公司 | A kind of paste state bed reactor preparing ethylene |
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| CB02 | Change of applicant information | ||
| CB02 | Change of applicant information |
Address after: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Applicant after: Shenwu science and technology group Limited by Share Ltd Address before: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Applicant before: Beijing Shenwu Environment Energy Technology Group Co., Ltd. |