CN104826558A - Slurry bed reactor and reaction system for producing ethylene by using acetylene selective hydrogenation - Google Patents
Slurry bed reactor and reaction system for producing ethylene by using acetylene selective hydrogenation Download PDFInfo
- Publication number
- CN104826558A CN104826558A CN201510251280.8A CN201510251280A CN104826558A CN 104826558 A CN104826558 A CN 104826558A CN 201510251280 A CN201510251280 A CN 201510251280A CN 104826558 A CN104826558 A CN 104826558A
- Authority
- CN
- China
- Prior art keywords
- bed reactor
- gas distributor
- paste state
- state bed
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Abstract
The invention belongs to the field of chemical engineering and provides a slurry bed reactor for producing ethylene by using acetylene selective hydrogenation. A gas distributor is arranged below the slurry bed reactor and is connected with a gas inlet; multiple groups of finger tubes are arranged above the gas distributor and are perpendicular to the horizontal surface; each group of finger tubes comprises multiple heat exchange tubes of which the tops are connected with one another, and the spacing between every two heat exchange tubes is equal; a gas-liquid separator is arranged below the gas outlet of the slurry bed reactor; and a condenser is arranged below the gas-liquid separator. The invention also provides a system by applying the slurry bed reactor. According to the equipment provided by the invention, the problems that the production amount of green oil is large, the cycle period of catalysts is short and temperature runaway of the reactor is easily caused in the fixed bed reactor in the ethylene production reaction based on acetylene selective hydrogenation are well solved, and the problems that loss of catalysts and difficulty in dust removal are caused due to violent collisions among the catalyst particles and that the heat exchange mechanism and the reactor are severely worn due to abrasive actions of solid particles are also solved.
Description
Technical field
The invention belongs to chemical field, be specifically related to a kind of paste state bed reactor and apply the system of described paste state bed reactor.
Background technology
Low concentration acetylene gas solid catalysis hydrogen addition technology is very ripe in the oil industry, be mainly used in removing acetylene impurities in ethene but due to ethyne reactive high, hydrogenation reaction thermal discharge is large, even there is a small amount of acetylene in cracking gas, traditional gas-solid fixes bed hydroprocessing reactor and still there are the serious problems such as green oil generating amount is large, the catalyst circulation cycle is short, reactor easy " temperature runaway ".Therefore the solid phase fixed bed catalytic hydrogenation process of traditional gas is also not suitable for the preparing ethylene by selective hydrogenation of acetylene of high concentration; Paste state bed reactor structure is simple, and be easy to move heat, reaction bed homogeneous temperature, the ethylene product of generation is of many uses, and therefore utilizing paste state bed reactor to carry out high concentration selective hydrogenation of acetylene becomes an important alkene production line processed.
The easy inactivation of catalyst, reaction bed local run aways are normal produced problem in prior art.Design based on reactor improves reaction efficiency and stability, is reasonable and effective solution.
Summary of the invention
For the deficiencies in the prior art part, the object of the invention is for heat release in high-load preparing ethylene by selective hydrogenation of acetylene process fast and thermal discharge disaster removes heat, easy generation green oil, catalysqt deactivation, the shortcoming of the aspects such as the low conversion rate of acetylene, provides a kind of paste state bed reactor for preparing ethylene by selective hydrogenation of acetylene.
The present invention also proposes the system of the preparing ethylene by selective hydrogenation of acetylene of the band solvent reclamation applying described paste state bed reactor.
Realizing the object of the invention technical scheme is:
For a paste state bed reactor for preparing ethylene by selective hydrogenation of acetylene, described paste state bed reactor comprises reactor shell, is surrounded by heating jacket outside housing, and being provided with gas access, top bottom paste state bed reactor has gas vent;
Be provided with gas distributor below described paste state bed reactor, gas distributor is connected with described gas access;
Arrange above gas distributor and organize dactylethrae more, dactylethrae is arranged perpendicular to horizontal plane, and often organize dactylethrae and comprise that many tops are connected, bottom lock and mutual disjunct heat exchanger tube, each heat exchanger tube spacing is equal; Be provided with gas-liquid separator below described paste state bed reactor gas vent, below described gas-liquid separator, be provided with condenser.
Wherein, described gas distributor comprises the multiple concentric annular gas distributor pipe being in same level, described annular gas distributor pipe bottom opening, described multiple concentric annular gas distributor pipe is communicated with the gas distributor tube connector below annular gas distributor pipe, and described gas distributor tube connector is connected with the central airway perpendicular to annular gas distributor pipe place plane; Central airway is connected with gas access.
The design that the present invention proposes, gas central airway entered is distributed to around each annular gas distributor pipe by gas distributor tube connector, realizes distribution of gas each position to the surrounding of gas distributor, thus enters slurry bed system.
Wherein, have the hole (preferred 3mm) of 2 ~ 6mm on bottom each annular gas distributor pipe, total percent opening of all annular gas distributor pipes is 10% ~ 15%.
Preferably, have the hole of 3mm on bottom each annular gas distributor pipe, total percent opening of all annular gas distributor pipes is 12%.
Wherein, described multiple concentric annular gas distributor pipe forms multiple concentric circles, and from the center of circle outwards, concentric circles diameter progressively increases, and the tube hub spacing of neighboring concentric circle is 60 ~ 90mm, and annular gas distributor pipe diameter is 40 ~ 70mm, is preferably 50mm.
Preferably, the tube hub spacing of neighboring concentric circle is 70mm, and annular gas distributor pipe diameter is 50mm.
Wherein, described heat exchanger tube diameter is 50 ~ 70mm, and heat exchanger tube spacing is 1 ~ 5 times of heat exchanger tube diameter.Described heat exchanger tube spacing is preferably 1.5 times of heat exchanger tube diameter.
The dactylethrae of heat exchange is evenly distributed in reactor cross section and forms vertical interior component, major diameter reactor is divided into many minor diameter reactors equably, correspondingly reduce the diameter of reactor, reduce the impact in a footpath, inhibit growing up and promoting breaking of bubble of bubble, limit the radial motion of gas and particle, particle axially-movable is freer, reduce the change of ratio of height to diameter, what solve linear gas velocity in slurries is uniformly distributed problem, improves the quality of fluidisation in reactor.
Further, the quantity of described dactylethrae is 12 ~ 30 groups, often organizes dactylethrae and comprises 3 ~ 20 heat exchanger tubes
Described paste state bed reactor, also comprises liquid-level auto-control device, and liquid-level auto-control device is between described condenser and described dactylethrae.
For a system for preparing ethylene by selective hydrogenation of acetylene, the paste state bed reactor that application the present invention proposes, described system also comprises regenerator, slurry tank;
Described paste state bed reactor lower housing portion is provided with serum outlet, and described serum outlet is connected with catalyst filter, and described catalyst filter connects described regenerator;
Described regenerator is provided with overhead condenser, and the condensate outlet of described overhead condenser connects slurry tank, and described slurry tank is also connected with catalyst storage tank; Described slurry tank is connected described paste state bed reactor by pump with pipeline.
Wherein, heater is provided with in described regenerator; Regenerator tower top is provided with condenser.
Wherein, described slurry tank is with agitating device; Described catalyst storage tank is with automatic discharge apparatus.
Preferably, described catalyst filter is two cluster type full-automatic filters in parallel, and filtering accuracy reaches 0.5 μm, and two cluster type full-automatic filters are used alternatingly and regenerate.
Heater is provided with in regenerator.Heater is by the liquid phase solvent gasification in slurry bed system, and the green-oil deposition in liquid phase is discharged bottom regenerator; The liquid phase solvent gasified in regenerator cools down and enters slurry tank by regenerator overhead condenser.
Preferably, described slurry tank, with agitating device, makes liquid phase solvent and catalyst fully mix.Described slurry tank has catalyst feeds, liquid phase solvent entrance and serum outlet.
Described catalyst storage tank, with automatic discharge apparatus, maintains the solid holdup of slurries about 5% by controlling load.
Beneficial effect of the present invention is:
1. compared with the technology of acetylene hydrogenation a small amount of in current ethene, this technology can realize by high concentration preparing ethylene by selective hydrogenation of acetylene, expands the technology path of Coal Chemical Industry further;
2. the dactylethrae of heat exchange reduces the diameter of reactor, reduce the impact in a footpath, not only can suppress too high local velocity, improve Flow Field Distribution, avoid short circuit, but also turbulence and gas-liquid mass transfer can be strengthened, what solve linear gas velocity in slurries is uniformly distributed problem, improves the quality of fluidisation in reactor;
3. slurries are extracted out from paste state bed reactor bottom, separation regeneration after catalyst filtration, and liquid phase solvent to mix with fresh catalyst and returns paste state bed reactor after regeneration, establishes the counter-current flow of catalyst and reaction gas, enhances the back-mixing of catalyst;
4. utilize the sensible heat of liquid phase solvent, remove heat energy power and significantly improve, the heat that selective hydrogenation of acetylene generates ethene generation can be shifted out fast, reduce the temperature of reaction bed, improve the conversion ratio of acetylene and the selective of ethene;
5. slurry reactor equipment of the present invention can realize catalyst change or regeneration, thus realizes the long period operation of paste state bed reactor, greatly improves process efficiency and reduces operating cost.
The slurry reactor equipment of band solvent reclamation provided by the invention, carry out selective hydrogenation of acetylene reaction, suppress the appearance of focus in the beds that in preparation of ethylene through selective hydrogenation of acetylene process, exothermic reaction causes better, avoid catalysqt deactivation, improve the stability of catalyst.The equipment that the present invention proposes solves that green oil generating amount in preparing ethylene by selective hydrogenation of acetylene reaction in fixed bed reactors is large, the catalyst circulation cycle is short well, the problem of reactor easily " temperature runaway ", due to the mutual sharp impacts of catalyst particles intergranular in fluid bed, cause the loss of catalyst, the difficulty of dedusting and the corrasion due to solid particle, the problem of the serious wear of heat exchange component and reactor.
Accompanying drawing explanation
Fig. 1: for the system diagram of preparing ethylene by selective hydrogenation of acetylene.
Fig. 2: schematic diagram arranged by gas distributor.
Fig. 3: dactylethrae structure chart.
Component names and being numbered in figure: chuck 1, serum outlet 2, gas access 3, gas distributor 4, dactylethrae 5, injection point 6, liquid-level auto-control device 7, condenser 8, gas-liquid separator 9, gas vent 10, catalyst filter 11, regenerator 12, overhead condenser 16, slurry tank 17, circulating pump 18, catalyst storage tank 19, catalyst feeds 20, liquid phase solvent entrance 21, serum outlet 22, paste state bed reactor cylindrical shell 23, annular gas distributor pipe 24, central airway 25, gas distributor tube connector 26.
Detailed description of the invention
Now with following most preferred embodiment, the present invention is described, but is not used for limiting the scope of the invention.
Embodiment 1:
See Fig. 1, a kind of paste state bed reactor for preparing ethylene by selective hydrogenation of acetylene, comprises paste state bed reactor cylindrical shell 23, is surrounded by chuck 1 outside cylindrical shell, and chuck is annular, passes into heat medium, heat paste state bed reactor in chuck.Be provided with gas access 3 bottom paste state bed reactor, gas vent 10 is arranged at top;
Be provided with gas distributor (Fig. 2) below described paste state bed reactor, be connected with gas access 3; Gas distributor comprises the concentric annular gas distributor pipe 24 of three of being in same level, and the tube hub spacing of neighboring concentric circle is 70mm, and annular gas distributor pipe diameter is 50mm.Have the hole that aperture is 3mm bottom annular gas distributor pipe 24, the total percent opening on annular gas distributor pipe is 12%; Annular gas distributor pipe and gas distributor tube connector 26 UNICOM below it, gas distributor tube connector 26 is connected with the central airway 25 perpendicular to annular gas distributor pipe place plane, central airway 25 is connected with gas access 3, the gas that central airway enters is distributed to around each annular gas distributor pipe 24 by gas distributor tube connector, realize distribution of gas each position to the surrounding of gas distributor, thus enter slurry bed system.
Be provided with 15 groups of dactylethraes above gas distributor, often organize dactylethrae and comprise 12 heat exchanger tubes, each heat exchanger tube spacing above gas distributor is equal, and each heat exchanger tube top is connected, bottom lock and be not connected (Fig. 3) mutually; Heat exchanger tube diameter is 57mm, and heat exchanger tube spacing is 1.5 times of heat exchanger tube diameter.Dactylethrae is arranged perpendicular to horizontal plane, and point two sections are independently installed, and two sections are connected with paste state bed reactor cylindrical shell respectively.
Be provided with gas-liquid separator 9 below paste state bed reactor gas vent 10, below gas-liquid separator, be provided with condenser 8.Gas-liquid separator is wire mesh demister.Wherein, described condenser take water as the condenser of cooling medium.
Embodiment 2
For a paste state bed reactor for preparing ethylene by selective hydrogenation of acetylene, comprise reactor shell, be surrounded by chuck outside housing, chuck is annular, passes into heat medium, heat paste state bed reactor in chuck.Be provided with gas access, top bottom paste state bed reactor and have gas vent;
Be provided with gas distributor below paste state bed reactor, be connected with gas access; Gas distributor comprises the concentric annular gas distributor pipe of 5 of being in same level, annular gas distributor pipe bottom opening, aperture 5mm, total percent opening of annular gas distributor pipe is 10%, the tube hub spacing of adjacent annular gas distribution tube is 60mm, and annular gas distributor pipe diameter is 50mm.Annular gas distributor pipe and the gas distributor tube connector UNICOM below it, gas distributor tube connector is connected with the central airway perpendicular to annular gas distributor pipe place plane, and central airway is connected with gas access.
Be provided with 15 groups of dactylethraes above gas distributor, often organize dactylethrae and comprise 12 heat exchanger tubes, each heat exchanger tube spacing above gas distributor is equal; Heat exchanger tube diameter is 57mm, and heat exchanger tube spacing is 2.0 times of heat exchanger tube diameter.
Be provided with gas-liquid separator below paste state bed reactor gas vent, below gas-liquid separator, be provided with condenser.Gas-liquid separator is the material 316ss of porous sintered metal, sintering metal.Condenser is Air-cooled Condenser.
Other parts of paste state bed reactor same embodiment 1 is set.
Embodiment 3
Adopt embodiment 1 paste state bed reactor for preparing ethylene by selective hydrogenation of acetylene system (Fig. 1): comprise paste state bed reactor, regenerator 12, slurry tank 17;
The serum outlet 2 of paste state bed reactor cylindrical shell bottom connects catalyst filter 11, and this catalyst filter is two cluster type full-automatic filters in parallel, and filtering accuracy reaches 0.5 μm, and two cluster type full-automatic filters are used alternatingly and regenerate.
Catalyst filter 11 connects regenerator 12; Heater is provided with in regenerator.Heater is by the liquid phase solvent gasification in slurry bed system, and the green-oil deposition in liquid phase is discharged bottom regenerator.
Regenerator tower top is provided with overhead condenser 16, and the condensate outlet of overhead condenser 16 connects the liquid phase solvent entrance 21 of slurry tank 17, and the liquid phase solvent gasified in regenerator cools down and enters slurry tank by regenerator overhead condenser.The catalyst feeds 20 of slurry tank 17 is connected with catalyst storage tank 19.The serum outlet 22 of slurry tank is connected paste state bed reactor by circulating pump 18 with pipeline.There is agitating device in this slurry tank 17, liquid phase solvent and catalyst are fully mixed.Catalyst storage tank 19, with automatic discharge apparatus, maintains the solid holdup of slurries about 5% by controlling load.
The operation of the present embodiment preparing ethylene by selective hydrogenation of acetylene system is as follows:
Heat medium is passed in the chuck of paste state bed reactor, to be temperature the be conduction oil of 200 DEG C, slurries in slurry bed system are heated to 160 DEG C, use indifferent gas nitrogen by after complete for the air displacement in paste state bed reactor again, hydrogen and acetylene enter gas distributor 4 from gas access 3, the gas entered is distributed, gas inlet distributor 4 pressure drop is not higher than 0.02MPa, thus gas is evenly entered in paste state bed reactor, afterwards by controlling the flow of the circular flow of conduction oil and the cooling medium water of dactylethrae 5 in chuck 1, the temperature of reaction is controlled at about 160 DEG C.
Preparing ethylene by selective hydrogenation of acetylene reaction is exothermic reaction, slurries enter the gaseous mixture counter current contacting with acetylene and hydrogen from paste state bed reactor top, the focus of course of reaction local is withdrawn by the sensible heat of liquid phase solvent, the heat that reaction produces is removed by dactylethrae 5 heat-exchanger rig, and reaction temperature is controlled at about 160 DEG C.
The liquid-level auto-control device 9 of paste state bed reactor, by the flow velocity of the outlet liquid of controlled circulation pump 18, maintains constant liquid level in slurry bed system.
At the condenser 8 on slurry bed system top, by the liquid phase solvent condensation of evaporation, the liquid phase solvent of condensation is back in slurry bed system; There is certain gas-liquid separation space at the top of paste state bed reactor from the gas access of gas-liquid separator 9, after gas enters gas-liquid separator 9, the liquid phase solvent of carry secretly in gas 99%, fall in backfill tower, gas goes out paste state bed reactor from reactor head gas vent 10.
Slurries bottom slurry bed system are after catalyst filter 11 is by catalyst filtration, liquid phase solvent enters regenerator 12, after regeneration, enter regenerator overhead condenser 16, liquid phase solvent enters after slurry tank 17 mixes with fresh catalyst and enters paste state bed reactor through circulating pump 18 after condensation; Catalyst after filtration sends into catalyst storage tank 19 after regeneration.
The green oil be dissolved in liquid phase solvent is regularly isolated bottom the regenerator of regenerating unit.
In paste state bed reactor, the granularity of catalyst is 20 ~ 100 μm, rate of wear≤2.5% of catalyst, catalyst bulk density≤1g/ml, and the temperature of operation is 160 DEG C, and operating pressure is 0.5MPa.The operating temperature of regenerating unit is 250 DEG C, and operating pressure is 50KPa.
The technique effect of the present embodiment consersion unit is as follows:
Continuous operation three months, the stable temperature control of reaction bed is at 160 DEG C ± 5 DEG C;
Liquid-level auto-control device stable operation;
Dactylethrae heat-exchange system is reasonable in design, easy to adjust when fluctuating appears in the temperature of reaction;
Built-in gas-liquid separation device is effective, and the gas liquid content after parting liquid phase solvent is little, and separative efficiency reaches more than 99%, reduces the load of later separation;
Preparing ethylene by selective hydrogenation of acetylene reaction effect in paste state bed reactor is good, and the conversion ratio of acetylene remains on 100%, and the selective of ethene is not less than 80%.
Embodiment 4
Adopt embodiment 2 paste state bed reactor for preparing ethylene by selective hydrogenation of acetylene system, reactor operating pressure is 0.2MPa, reaction temperature 150 DEG C, other operating conditions of slurry bed system and configuration aspects identical with embodiment 3.
The present embodiment effect is as follows:
Continuous operation two months, reactor operation freely, does not occur that gas is by the excessive situation of porous sintered metal pressure reduction;
Adopt the first condensation of Air-cooled Condenser and the combination be separated after built-in porous sintered metal, gas-liquid separation effect reaches requirement, and after parting liquid phase solvent, in gas, liquid hold-up is less than 1%;
Other performance of reactor is consistent with embodiment 1.
Those skilled in the art in the art will be appreciated that, above-described embodiment is only used to the present invention is described, and be not used as limitation of the invention, as long as in spirit of the present invention, the conversion of above-described embodiment, modification all will be dropped in the scope of the claims in the present invention.
Claims (10)
1. for a paste state bed reactor for preparing ethylene by selective hydrogenation of acetylene, described paste state bed reactor comprises reactor shell, is surrounded by heating jacket outside housing, and being provided with gas access, top bottom paste state bed reactor has gas vent; It is characterized in that,
Be provided with gas distributor below described paste state bed reactor, gas distributor is connected with described gas access;
Arrange above gas distributor and organize dactylethrae more, dactylethrae is arranged perpendicular to horizontal plane, and often organize dactylethrae and comprise that many tops are connected, bottom lock and mutual disjunct heat exchanger tube, each heat exchanger tube spacing is equal;
Be provided with gas-liquid separator below described paste state bed reactor gas vent, below described gas-liquid separator, be provided with condenser.
2. paste state bed reactor according to claim 1, it is characterized in that, described gas distributor comprises the multiple concentric annular gas distributor pipe being in same level, described annular gas distributor pipe bottom opening, described multiple concentric annular gas distributor pipe is communicated with the gas distributor tube connector below annular gas distributor pipe, and described gas distributor tube connector is connected with the central airway perpendicular to annular gas distributor pipe place plane; Central airway is connected with gas access.
3. paste state bed reactor according to claim 2, is characterized in that, has the hole of 2 ~ 6mm on bottom each annular gas distributor pipe, and total percent opening of all annular gas distributor pipes is 10% ~ 15%.
4. paste state bed reactor according to claim 2, it is characterized in that, described multiple concentric annular gas distributor pipe forms multiple concentric circles, outside from the center of circle, concentric circles diameter progressively increases, the tube hub spacing of neighboring concentric circle is 60 ~ 90mm, and annular gas distributor pipe diameter is 40 ~ 70mm.
5. paste state bed reactor according to claim 1, is characterized in that, described heat exchanger tube diameter is 50 ~ 70mm, and heat exchanger tube spacing is 1 ~ 5 times of heat exchanger tube diameter.
6. paste state bed reactor according to claim 1, is characterized in that, the quantity of described dactylethrae is 12 ~ 30 groups, often organizes dactylethrae and comprises 3 ~ 20 heat exchanger tubes.
7., according to the arbitrary described paste state bed reactor of claim 1 ~ 6, it is characterized in that, also comprise liquid-level auto-control device, liquid-level auto-control device is between described condenser and described dactylethrae.
8. for a system for preparing ethylene by selective hydrogenation of acetylene, it is characterized in that, application rights requires 1 ~ 7 arbitrary described paste state bed reactor, and described system also comprises regenerator, slurry tank;
Described paste state bed reactor lower housing portion is provided with serum outlet, and described serum outlet is connected with catalyst filter, and described catalyst filter connects described regenerator;
Described regenerator is provided with overhead condenser, and the condensate outlet of described overhead condenser connects slurry tank, and described slurry tank is also connected with catalyst storage tank; Described slurry tank is connected described paste state bed reactor by pump with pipeline.
9. system according to claim 8, is characterized in that, is provided with heater in described regenerator; Regenerator tower top is provided with condenser.
10. system according to claim 8 or claim 9, it is characterized in that, described slurry tank is with agitating device; Described catalyst storage tank is with automatic discharge apparatus.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510251280.8A CN104826558B (en) | 2015-05-15 | 2015-05-15 | Paste state bed reactor and response system for preparing ethylene by selective hydrogenation of acetylene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510251280.8A CN104826558B (en) | 2015-05-15 | 2015-05-15 | Paste state bed reactor and response system for preparing ethylene by selective hydrogenation of acetylene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104826558A true CN104826558A (en) | 2015-08-12 |
| CN104826558B CN104826558B (en) | 2016-10-12 |
Family
ID=53804969
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510251280.8A Active CN104826558B (en) | 2015-05-15 | 2015-05-15 | Paste state bed reactor and response system for preparing ethylene by selective hydrogenation of acetylene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104826558B (en) |
Cited By (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105859497A (en) * | 2016-06-08 | 2016-08-17 | 北京神雾环境能源科技集团股份有限公司 | Reaction system and method for producing ethylene through pressure swing adsorption |
| CN105859501A (en) * | 2016-06-08 | 2016-08-17 | 北京神雾环境能源科技集团股份有限公司 | Reaction system and method for preparing ethylene by means of solvent reclamation |
| CN105859499A (en) * | 2016-06-08 | 2016-08-17 | 北京神雾环境能源科技集团股份有限公司 | Reaction system and method for preparing ethylene through hydrogenation of acetylene |
| CN105859500A (en) * | 2016-06-08 | 2016-08-17 | 北京神雾环境能源科技集团股份有限公司 | Ethylene preparation reaction system and method with vacuum solvent regeneration |
| CN105859505A (en) * | 2016-06-14 | 2016-08-17 | 北京神雾环境能源科技集团股份有限公司 | Reaction system and method for removing green oil to prepare ethylene and method |
| CN105859502A (en) * | 2016-06-14 | 2016-08-17 | 北京神雾环境能源科技集团股份有限公司 | Reaction system and method for preparing ethylene |
| CN105859498A (en) * | 2016-06-08 | 2016-08-17 | 北京神雾环境能源科技集团股份有限公司 | Reaction system and method for producing ethylene through catalyst regeneration |
| CN105879792A (en) * | 2016-06-14 | 2016-08-24 | 北京神雾环境能源科技集团股份有限公司 | Reaction system and method for preparing ethylene by means of slurry bed reactor |
| CN105903414A (en) * | 2016-06-14 | 2016-08-31 | 北京神雾环境能源科技集团股份有限公司 | Slurry-bed reactor for preparing ethylene |
| CN105906468A (en) * | 2016-06-08 | 2016-08-31 | 北京神雾环境能源科技集团股份有限公司 | Reaction system and method for preparing ethylene through regeneration of super gravity solvent |
| CN105906469A (en) * | 2016-06-14 | 2016-08-31 | 北京神雾环境能源科技集团股份有限公司 | External heating reaction system and method for preparing ethylene |
| CN105906470A (en) * | 2016-06-14 | 2016-08-31 | 北京神雾环境能源科技集团股份有限公司 | Reaction system for preparing ethylene by inputting gas at different heights and method |
| CN105944627A (en) * | 2016-07-06 | 2016-09-21 | 北京神雾环境能源科技集团股份有限公司 | Device for preparing ethylene from acetylene through selective hydrogenation |
| CN105967969A (en) * | 2016-06-14 | 2016-09-28 | 北京神雾环境能源科技集团股份有限公司 | Catalyst regeneration type reaction system and method for preparing ethylene |
| CN106045809A (en) * | 2016-07-21 | 2016-10-26 | 北京华福工程有限公司 | Reaction system and method for preparing ethylene by using slurry bed reactor |
| CN106083511A (en) * | 2016-07-21 | 2016-11-09 | 北京华福工程有限公司 | A kind of response system preparing ethylene and method |
| CN107252615A (en) * | 2017-07-19 | 2017-10-17 | 铜陵泰富特种材料有限公司 | Gas distributor and adsorption tower |
| CN110923004A (en) * | 2019-11-12 | 2020-03-27 | 韩慧颖 | Catalytic method capable of improving reaction rate for slurry bed residual oil hydroconversion technology |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1328485A (en) * | 1998-11-26 | 2001-12-26 | Basf公司 | Reactor for carrying out gas-liquid, liquid-liquid or gas-liquid-solid chemical reactions |
| CN1923351A (en) * | 2006-09-01 | 2007-03-07 | 清华大学 | Staged reactor |
| WO2007086610A1 (en) * | 2006-01-30 | 2007-08-02 | Nippon Steel Engineering Co., Ltd. | Bubble column type hydrocarbon synthesis reactor |
| CN101480595A (en) * | 2009-01-08 | 2009-07-15 | 浙江大学 | Slurry bubble column reactor with needle type fin column tube bundle |
| CN104130216A (en) * | 2014-08-11 | 2014-11-05 | 河南骏化发展股份有限公司 | Process for continuously producing epoxy propane through propylene and propane mixed gas directly oxidized by hydrogen peroxide |
| CN204522947U (en) * | 2015-05-15 | 2015-08-05 | 北京神雾环境能源科技集团股份有限公司 | For paste state bed reactor and the reaction system of preparing ethylene by selective hydrogenation of acetylene |
-
2015
- 2015-05-15 CN CN201510251280.8A patent/CN104826558B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1328485A (en) * | 1998-11-26 | 2001-12-26 | Basf公司 | Reactor for carrying out gas-liquid, liquid-liquid or gas-liquid-solid chemical reactions |
| WO2007086610A1 (en) * | 2006-01-30 | 2007-08-02 | Nippon Steel Engineering Co., Ltd. | Bubble column type hydrocarbon synthesis reactor |
| CN1923351A (en) * | 2006-09-01 | 2007-03-07 | 清华大学 | Staged reactor |
| CN101480595A (en) * | 2009-01-08 | 2009-07-15 | 浙江大学 | Slurry bubble column reactor with needle type fin column tube bundle |
| CN104130216A (en) * | 2014-08-11 | 2014-11-05 | 河南骏化发展股份有限公司 | Process for continuously producing epoxy propane through propylene and propane mixed gas directly oxidized by hydrogen peroxide |
| CN204522947U (en) * | 2015-05-15 | 2015-08-05 | 北京神雾环境能源科技集团股份有限公司 | For paste state bed reactor and the reaction system of preparing ethylene by selective hydrogenation of acetylene |
Cited By (25)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105906468A (en) * | 2016-06-08 | 2016-08-31 | 北京神雾环境能源科技集团股份有限公司 | Reaction system and method for preparing ethylene through regeneration of super gravity solvent |
| CN105859501A (en) * | 2016-06-08 | 2016-08-17 | 北京神雾环境能源科技集团股份有限公司 | Reaction system and method for preparing ethylene by means of solvent reclamation |
| CN105859499A (en) * | 2016-06-08 | 2016-08-17 | 北京神雾环境能源科技集团股份有限公司 | Reaction system and method for preparing ethylene through hydrogenation of acetylene |
| CN105859500A (en) * | 2016-06-08 | 2016-08-17 | 北京神雾环境能源科技集团股份有限公司 | Ethylene preparation reaction system and method with vacuum solvent regeneration |
| CN105859499B (en) * | 2016-06-08 | 2019-02-12 | 霍尔果斯道科特环能科技有限公司 | A kind of reaction system and method for producing ethylene with acetylene hydrogenation |
| CN105906468B (en) * | 2016-06-08 | 2019-02-12 | 霍尔果斯道科特环能科技有限公司 | A kind of reaction system and method for the ethylene processed of hypergravity solvent reclamation |
| CN105859498A (en) * | 2016-06-08 | 2016-08-17 | 北京神雾环境能源科技集团股份有限公司 | Reaction system and method for producing ethylene through catalyst regeneration |
| CN105859497A (en) * | 2016-06-08 | 2016-08-17 | 北京神雾环境能源科技集团股份有限公司 | Reaction system and method for producing ethylene through pressure swing adsorption |
| CN105859505B (en) * | 2016-06-14 | 2018-09-07 | 神雾科技集团股份有限公司 | A kind of reaction system and method for preparing ethylene of removing green oil |
| CN105859502B (en) * | 2016-06-14 | 2018-09-07 | 神雾科技集团股份有限公司 | A kind of reaction system and method preparing ethylene |
| CN105906469A (en) * | 2016-06-14 | 2016-08-31 | 北京神雾环境能源科技集团股份有限公司 | External heating reaction system and method for preparing ethylene |
| CN105906470A (en) * | 2016-06-14 | 2016-08-31 | 北京神雾环境能源科技集团股份有限公司 | Reaction system for preparing ethylene by inputting gas at different heights and method |
| CN105859505A (en) * | 2016-06-14 | 2016-08-17 | 北京神雾环境能源科技集团股份有限公司 | Reaction system and method for removing green oil to prepare ethylene and method |
| CN105967969A (en) * | 2016-06-14 | 2016-09-28 | 北京神雾环境能源科技集团股份有限公司 | Catalyst regeneration type reaction system and method for preparing ethylene |
| CN105859502A (en) * | 2016-06-14 | 2016-08-17 | 北京神雾环境能源科技集团股份有限公司 | Reaction system and method for preparing ethylene |
| CN105879792A (en) * | 2016-06-14 | 2016-08-24 | 北京神雾环境能源科技集团股份有限公司 | Reaction system and method for preparing ethylene by means of slurry bed reactor |
| CN105903414A (en) * | 2016-06-14 | 2016-08-31 | 北京神雾环境能源科技集团股份有限公司 | Slurry-bed reactor for preparing ethylene |
| CN105944627A (en) * | 2016-07-06 | 2016-09-21 | 北京神雾环境能源科技集团股份有限公司 | Device for preparing ethylene from acetylene through selective hydrogenation |
| CN106083511A (en) * | 2016-07-21 | 2016-11-09 | 北京华福工程有限公司 | A kind of response system preparing ethylene and method |
| CN106045809A (en) * | 2016-07-21 | 2016-10-26 | 北京华福工程有限公司 | Reaction system and method for preparing ethylene by using slurry bed reactor |
| CN106045809B (en) * | 2016-07-21 | 2019-05-28 | 北京华福工程有限公司 | It is a kind of using prepared in slurry bed reactor for the reaction system and method for ethylene |
| CN106083511B (en) * | 2016-07-21 | 2019-05-28 | 北京华福工程有限公司 | A kind of reaction system preparing ethylene and method |
| CN107252615A (en) * | 2017-07-19 | 2017-10-17 | 铜陵泰富特种材料有限公司 | Gas distributor and adsorption tower |
| CN107252615B (en) * | 2017-07-19 | 2020-12-22 | 铜陵泰富特种材料有限公司 | Gas distributor and adsorption tower |
| CN110923004A (en) * | 2019-11-12 | 2020-03-27 | 韩慧颖 | Catalytic method capable of improving reaction rate for slurry bed residual oil hydroconversion technology |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104826558B (en) | 2016-10-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104826558A (en) | Slurry bed reactor and reaction system for producing ethylene by using acetylene selective hydrogenation | |
| CN105175208A (en) | Method for preparation of ethylene from hydrogenation of acetylene and reaction tower for the method | |
| CN204973827U (en) | A reaction tower for acetylene hydrogenation makes ethylene | |
| CN102659498B (en) | Device and method for converting methanol into low-carbon olefins | |
| CN102850183B (en) | Methanol synthesis system and method | |
| CN204522947U (en) | For paste state bed reactor and the reaction system of preparing ethylene by selective hydrogenation of acetylene | |
| CN107930540A (en) | A kind of controlling temp type multilayer FCC reactor | |
| CN105859502B (en) | A kind of reaction system and method preparing ethylene | |
| CN103341341A (en) | Fluidized bed reactor for preparing butadiene | |
| CN204454563U (en) | High-concentration carbon monoxide isothermal transformation system | |
| CN202808648U (en) | Methanol synthetic system | |
| CN104945211A (en) | Heat extraction and catalyst circulation method in catalytic reaction for preparing hydrocarbons from methanol | |
| CN105859505B (en) | A kind of reaction system and method for preparing ethylene of removing green oil | |
| CN206045989U (en) | A kind of response system of utilization prepared in slurry bed reactor for ethylene | |
| CN206519141U (en) | Shell and tube paste state bed reactor and reaction system | |
| CN206051888U (en) | A kind of response system for preparing ethylene | |
| CN205710506U (en) | A kind of response system preparing ethylene removing green oil | |
| CN101711962B (en) | Catalytic conversion stripper | |
| CN106045809B (en) | It is a kind of using prepared in slurry bed reactor for the reaction system and method for ethylene | |
| CN205893121U (en) | Utilize reaction system of thick liquid attitude bed reactor preparation ethylene | |
| CN106540637A (en) | A kind of circulation flow reactor and application process | |
| CN205700485U (en) | A kind of paste state bed reactor preparing ethylene | |
| CN205893120U (en) | Reaction system of preparation ethylene | |
| CN113522371A (en) | Stripping cooling equipment and method for regenerated catalyst | |
| CN205974315U (en) | Reaction system of gaseous preparation ethylene is not imported to co -altitude |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| EXSB | Decision made by sipo to initiate substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20160928 Address after: 102200 Beijing City, Changping District science and Technology Park Fukang Road No. 18 Patentee after: Beijing Huafu Engineering Co., Ltd. Address before: 102200 Beijing city Changping District Machi Town cow Road No. 18 Patentee before: Beijing Shenwu Environment Energy Technology Group Co., Ltd. |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20200521 Address after: 100121 1105, floor 1, building 1, yard 18, Shuangqiao East Road, Chaoyang District, Beijing Patentee after: Beijing Jintai Chengrui Technology Development Co., Ltd Address before: 102200 No. 18 Fukang Road, Changping District science and Technology Park, Beijing Patentee before: BEIJING HUAFU ENGINEERING Co.,Ltd. |
|
| TR01 | Transfer of patent right |