CN205886829U - Device of acetylene selective hydrogenation system ethylene - Google Patents

Device of acetylene selective hydrogenation system ethylene Download PDF

Info

Publication number
CN205886829U
CN205886829U CN201620710002.4U CN201620710002U CN205886829U CN 205886829 U CN205886829 U CN 205886829U CN 201620710002 U CN201620710002 U CN 201620710002U CN 205886829 U CN205886829 U CN 205886829U
Authority
CN
China
Prior art keywords
liquid
gas
catalyst
filler
attached
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.)
Active
Application number
CN201620710002.4U
Other languages
Chinese (zh)
Inventor
史雪君
苏二强
余海鹏
刘周恩
吴黎阳
吴道洪
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Beijing Huafu Engineering Co Ltd
Original Assignee
Beijing Huafu Engineering Co Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Beijing Huafu Engineering Co Ltd filed Critical Beijing Huafu Engineering Co Ltd
Priority to CN201620710002.4U priority Critical patent/CN205886829U/en
Application granted granted Critical
Publication of CN205886829U publication Critical patent/CN205886829U/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/50Improvements relating to the production of bulk chemicals
    • Y02P20/52Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Abstract

The utility model relates to a device of acetylene selective hydrogenation system ethylene, include the casing, be located vapour and liquid separator in gas feed, gas outlet, liquid import, liquid outlet and the casing on the casing still includes: adhere to the filler that has the catalyst in the casing, gas feed is located adhere to under the filler that has the catalyst, the liquid import is located adhere to on the filler that has the catalyst, the gas outlet is located on the liquid import, vapour and liquid separator is located between gas outlet and the liquid import. The utility model provides a reaction unit has the catalyst and distributes evenly, and catalyst bed layer temperature is even, conversion rate with the high advantage of selectivity, the jam that can alleviate the catalysis bed, life -span of extension catalyst, the utility model discloses a reaction unit still has the good advantage of the heat energy power of removing, can make reactor long -time operation the in succession, is applicable to the reaction of high concentration acetylene hydrogenation.

Description

A kind of device of preparing ethylene by selective hydrogenation of acetylene
Technical field
This utility model is related to a kind of reaction unit of preparing ethylene by selective hydrogenation of acetylene, belongs to chemical industry equipment device neck Domain.
Background technology
Low concentration acetylene gas and solid phase catalyzing hydrogen addition technology is highly developed in the oil industry, is mainly used in removing in ethylene Acetylene impurities but because ethyne reactive is high, hydrogenation reaction thermal discharge is big, even there is a small amount of acetylene in cracking gas, traditional gas Solid phase fixed bed hydrogenation reactor there are still that green oil generating amount is big, catalyst cycle period is short, reactor easily " temperature runaway " etc. is tight Weight problem.Therefore traditional gas-solid phase fixed-bed catalytic hydrogenation technique is not appropriate for the selective hydrogenation of acetylene second of high concentration Alkene;Although paste state bed reactor overcomes the defect of fixed bed temperature runaway, but still generally existing gas-liquid-solid uniformly mixes difficulty, operation Defect that elasticity is little, catalyst granules easily deposits, gas distributor easily blocks and liquid phase solvent consumption is big etc..Trickle bed is by being catalyzed The particle-filled reactor of agent, gas and liquid cocurrent flow downward, and bed pressure drop is little to be difficult liquid flooding, but trickle bed has footpath To conduct heat poor, be also easy to produce channel, short circuit and the incomplete moistening of catalyst so that operational circumstances degenerate.
Utility model content
(1) technical problem to be solved
Device for preparing ethylene by selective hydrogenation of acetylene of the prior art there is catalyst granules easily deposition it is impossible to and When the defect that radiates, this utility model provides a kind of novel ethyne preparing ethylene by selective hydrogenation being attached to catalyst on filler Device.
(2) technical scheme
Device described in the utility model, comprising: housing, the gas feed being located on described housing, gas outlet, liquid Gas-liquid separator in import, liquid outlet and housing, also includes: the filler being attached with catalyst in housing;
Described gas feed is located under the described filler being attached with catalyst, and described liquid-inlet is located at described being attached with On the filler of catalyst;
Described gas outlet is located on described liquid-inlet, and described gas-liquid separator is located at described gas outlet and liquid Between import.
Device described in the utility model, in the described filler being attached with catalyst, filler is to have regular cavernous structure The metal gauze of high-specific surface area,
Preferably, described filler is specific surface area 650~750m2/m3, the anodised aluminium ripple of porosity 90~95% Silk screen.
Further preferably, filler is specific surface area 700m2/m3, the anodised aluminium ripple silk net of porosity 93%.
What described filler was regular is filled in housing, and implant of jumping a queue between filler and tower body wall is allowed to seamless.
Device described in the utility model, in the described filler being attached with catalyst the active component of catalyst be pd, mo, The combination of one or more of au and co, auxiliary agent is one or more of ag, zn, in and mg.
Described catalyst activity component and described auxiliary agent are reduced into metal and are deposited on anode by the method for chemical plating Alumina surface.
Device described in the utility model, described gas-liquid separator is impingement separator, the filtration of metal gauze Formula gas-liquid separator, rotational flow type gas-liquid separater or combined multi-stage gas-liquid separator.
Device described in the utility model, is also included positioned between described liquid-inlet and the filler being attached with catalyst Liquid distribution trough, positioned at the described gas distributor being attached between the filler of catalyst and gas feed.
Device described in the utility model, described liquid distribution trough is tank type liquid distributor;Described liquid distribution trough with There is no gap between the inwall of described housing.
Device described in the utility model, described gas distributor includes many concentric tubees, positions positioned at same level Multiple downward opening gas nozzle on described concentric tube and the vapor riser being connected with described concentric tube;
Pass through pipeline between described concentric tube to be connected, the other end of described vapor riser is connected with gas feed;
Also include two orthogonal support beams, this support beam provides to described concentric tube and supports, support beam Two ends are fixed on reaction unit wall.
Device described in the utility model, also includes the liquid level and liquid distribution trough between below described liquid-inlet Automatic controller, described liquid level self-controller includes liquid level emasuring device, automatic admission valve and automatic air outlet valve;By controlling Pressure above liquid distributing board is keeping the constant liquid level on liquid distributing board.
Device described in the utility model, is provided with filler in described being attached between the filler of catalyst and gas distributor Eyelid retractor.
The reaction unit of preparing ethylene by selective hydrogenation of acetylene described in the utility model, its structure is preferably:
Including housing, and the liquid outlet that the outside of housing sets gradually from the bottom up, gas feed, liquid automatic control Device, liquid-inlet, gas outlet;
The inside of described housing is sequentially provided with from the bottom up, gas distributor, packing support device, is attached with filling out of catalyst Material, liquid distribution trough, gas-liquid separator;
Described gas distributor is located on described gas feed, and described liquid distribution trough is located at described liquid automatic control Under device, described gas-liquid separator is located between described liquid-inlet and described gas outlet;
Described filler is specific surface area 700m2/m3, the anodised aluminium ripple silk net of porosity 93%;The activity of catalyst Composition is the combination of one or more of pd, mo, au and co, and auxiliary agent is one or more of ag, zn, in and mg;
Described liquid distribution trough is tank type liquid distributor;
Described gas distributor includes many concentric tubees positioned at same level, multiple opening of being located on described concentric tube The gas nozzle of mouth down and the vapor riser being connected with described concentric tube;
Pass through pipeline between described concentric tube to be connected, the other end of described vapor riser is connected with gas feed;
Described liquid level self-controller includes liquid level emasuring device, automatic admission valve and automatic air outlet valve;By controlling liquid Pressure above body distribution grid is keeping the constant liquid level on liquid distributing board;
Described gas-liquid separator is impingement separator.
The method carrying out pure preparing ethylene by selective hydrogenation of acetylene with device described in the utility model, walks including following Rapid:
1) by the preheating temperature in described housing to 110~190 DEG C, 3:1~6:1 mixes by volume to be passed through hydrogen and acetylene Close gas, reacted under the catalysis of catalyst;
2) it is passed through liquid during reacting to be lowered the temperature, control the reaction temperature in described housing to be 150~180 DEG C, Pressure is 1.2~1.8mpa.
Device described in the utility model has the advantages that
1) in device described in the utility model, catalyst is equably attached to the surface of filler, and no precipitation produces, and can fill Play catalytic action with dividing;Catalytic bed hot localised points are not resulted in, reaction bed temperature is uniform, it is to avoid green in course of reaction The generation of oil, improves the stability of catalyst.
2) reaction and separation is made to complete in an equipment using packing type catalyst, small investment, operating cost reduce, borrow Help the centrifugation of filler, improve conversion of alkyne and ethylene selectivity, mitigate the blocking of catalytic bed, extend catalyst Life-span.
3) the regular metal material of Fillers selection shape described in the utility model, metal material has good heat conduction Property, the heat producing in course of reaction can be conducted in time, and easy processing becomes variously-shaped, has good anti-vibration resistance Energy, high mechanical properties;Made regular shape, effectively solving can be loaded a difficult problem, also available higher bed voidage, Be conducive to being uniformly distributed of gas-liquid.
4) gas distributor can make reaction gas be fully contacted with catalyst, and what liquid distribution trough can improve liquid removes heat energy Power, is quickly moved out selective hydrogenation of acetylene and generates the heat that ethylene produces, reduce the temperature of reaction bed, suppresses sending out of side reaction Raw, improve conversion ratio, the selectivity of ethylene of acetylene, reduce the content generating green oil;Liquid phase solvent constantly washes away catalysis simultaneously The surface of agent, the green oil on catalyst is dissolved down, and extends the life-span of catalyst.
5) liquid-level auto-control device maintains liquid level on liquid distributing board by the pressure adjusting above liquid distributing board Constant it is ensured that liquid phase solvent smoothly flows into filler surface.
In a word, the reaction unit that this utility model provides has catalyst distribution uniformly, and reaction bed temperature is uniform, instead Answer conversion ratio and the high advantage of selectivity, the blocking of catalytic bed can be mitigated, extend the life-span of catalyst;Of the present utility model anti- Answer device also to have the advantages that reactor removes heat energy power good, reactor can be made to be continuously long-running it is adaptable to high concentration acetylene Hydrogenation reaction.
Brief description
Fig. 1 is the apparatus structure schematic diagram of producing ethylene with acetylene hydrogenation reaction described in the utility model;
In figure: 1. housing, 2. gas feed, 3. gas distributor, 4. liquid outlet, 5. packing support device, 6. filler, 7. liquid distribution trough, 8. liquid-inlet, 9. liquid-level auto-control device, 10. gas-liquid separator, 11. gas outlets.
Specific embodiment
Following examples are used for this utility model is described, but are not limited to scope of the present utility model.
Embodiment 1
The present embodiment is related to the reaction unit of preparing ethylene by selective hydrogenation of acetylene described in the utility model, comprising:
Housing 1, the gas feed 2 being located on described housing, gas outlet 11, liquid-inlet 8, liquid outlet 4 and shell Internal gas-liquid separator 10,
Also include: the filler 6 being attached with catalyst in housing;
Described gas feed 2 is located under the described filler 6 being attached with catalyst, and described liquid-inlet 8 is located at described attached On the filler 6 of catalyst, described liquid outlet is located at the bottom of housing;
Described gas outlet 11 is located on described liquid-inlet 8, and described gas-liquid separator 10 is located at described gas outlet 8 between 11 and liquid-inlet.
Embodiment 2
Compared with embodiment 1, its difference is, the filler 6 also including positioned at described liquid-inlet 8 and being attached with catalyst Between liquid distribution trough 7, the gas distributor 3 between described filler eyelid retractor 5 and gas feed 2.
Described liquid distribution trough is tank type liquid distributor;
Described gas distributor includes many concentric tubees positioned at same level, multiple opening of being located on described concentric tube The gas nozzle of mouth down and the vapor riser being connected with described concentric tube;
Pass through pipeline between described concentric tube to be connected, the other end of described vapor riser is connected with described gas feed.
Embodiment 3
The present embodiment is related to the reaction unit of preparing ethylene by selective hydrogenation of acetylene described in the utility model, its structural representation Figure such as Fig. 1,
On the housing 1 of reaction unit, it is sequentially provided with liquid outlet 4, gas feed 2 from the bottom up, liquid automatic control fills Put 9, liquid-inlet 8, gas outlet 11;
The inside of described housing is sequentially provided with from top to bottom, gas distributor 3, and packing support device 5 is attached with catalyst Filler 6, liquid distribution trough 7, air-flow liquid/gas separator 10;
Described gas distributor 3 is located on described gas feed 2, and it is automatic that described liquid distribution trough 7 is located at described liquid level Under control device 9, described gas-liquid separator 10 is located between described liquid level liquid-inlet 8 and described gas outlet 11.
In this device, described filler is specific surface area 700m2/m3, the anodised aluminium ripple silk net of porosity 93%;Institute Stating catalyst active component is pd, and auxiliary agent is ag;
In this device, described liquid distribution trough 7 is tank type liquid distributor, and including major trough and point groove, described point of groove is located at The lower section of described major trough, described major trough is provided with inverted trapezoidal spout hole, and a point groove is provided with rectangle spout hole, and the bottom land of point groove is opened There is drain hole two.
Described gas distributor includes many concentric tubees positioned at same level, multiple opening of being located on described concentric tube The gas nozzle of mouth down and the vapor riser being connected with described concentric tube;
Pass through pipeline between described concentric tube to be connected, the other end of described vapor riser is connected with gas feed;
Also include two orthogonal support beams, this support beam provides to described concentric tube and supports, support beam Two ends are fixed on reaction unit wall.
In this device, described liquid level self-controller 9 includes liquid level emasuring device, automatic admission valve and automatic air outlet valve; Keep the constant liquid level on liquid distributing board by controlling the pressure above liquid distributing board;
In this device, described gas-liquid separator 10 is impingement separator.
Embodiment 4
The reaction unit of the selective hydrogenation of acetylene described in embodiment 3, its operational approach comprises the steps:
1) liquid phase solvent of heat enters from reaction unit top, flows to filler 6 surface by liquid distribution trough 7, will react Device preheats;
2) mixed gas of hydrogen and acetylene enter from gas feed 2, through gas distributor 3, the gas entering are carried out Distribution, so that gas can be even in reaction unit;
3) enter the gas in reaction tower and react generation ethylene in the presence of catalyst, liquid phase solvent is from reaction unit top Portion enters liquid distribution trough 7 and flows to filler 6 surface, takes away reaction heat, makes reaction be in temperature constant state;During the course of the reaction, liquid Level automatic control device keeps the constant liquid level on liquid distributing board by controlling the pressure put on liquid distributing board;
4) ethylene that reaction generates moves upwards, has necessarily in the gas feed of distance from top impingement separator 10 Gas-liquid separation space, after air-flow enters impingement separator 10, the liquid phase solvent carried secretly in air-flow drops back into reaction dress In putting, gas goes out reaction unit from reactor head gas outlet 11.
Embodiment 5
The present embodiment is related to apply device described in the utility model, the method preparing ethylene by pure acetylene and hydrogen, Comprise the steps:
1) liquid phase solvent of heat is passed through from liquid-inlet, flows to filler surface by liquid distribution trough, and reaction unit is pre- Heat arrives 150 DEG C of reaction temperature;
2) 5:1 mixed gas enter from gas feed by volume, through gas distributor 3 to entrance for hydrogen and acetylene Gas is allocated, and distributor pressure drop is not higher than 0.02mpa, so that gas can be even in reaction unit;
3) enter the gas in reaction tower and react generation ethylene in the presence of catalyst, liquid phase solvent is from reaction unit top Portion enters liquid distribution trough and flows to filler surface, takes away reaction heat, makes reaction be in temperature constant state, reaction temperature controls 170 DEG C, operating pressure is 1.5mpa;During the course of the reaction, liquid-level auto-control device passes through to control the pressure put on liquid distributing board To keep the constant liquid level on liquid distributing board;
4) ethylene that reaction generates moves upwards, has certain in the gas feed of distance from top impingement separator Gas-liquid separation space, after air-flow enters impingement separator, the liquid phase solvent carried secretly in air-flow drops back in reaction unit, Gas goes out reaction unit from reactor head gas outlet.
The specification of packing type catalyst is specific surface area 700m2/m3, filler porosity 93%.
Using device described in the utility model, continuous operation three months, the stable temperature control of reaction bed;Liquid level is certainly Dynamic control device stable operation;Liquid phase solvent heat-exchange system is reasonable in design, and the temperature of reaction is easy to adjust when occurring fluctuating;Built-in Impingement segregation apparatuss effect is good, and in the air-flow after the completion of separating, liquid hold-up is less than 1%, and the conversion ratio of acetylene is maintained at 100%, the selectivity of ethylene is not less than 85%.
Although, above used general explanation, specific embodiment and test, this utility model made in detail Description, but on the basis of this utility model, it can be made some modifications or improvements, this is aobvious to those skilled in the art And be clear to.Therefore, these modifications or improvements on the basis of without departing from this utility model spirit, belong to this practicality New claimed scope.

Claims (10)

1. a kind of device of preparing ethylene by selective hydrogenation of acetylene, comprising: housing, the gas feed being located on described housing, gas Gas-liquid separator in outlet, liquid-inlet, liquid outlet and housing is it is characterised in that also include: being attached with housing The filler of catalyst;
Described gas feed is located under the described filler being attached with catalyst, and described liquid-inlet is located at and described is attached with catalysis On the filler of agent;
Described gas outlet is located on described liquid-inlet, and described gas-liquid separator is located at described gas outlet and liquid-inlet Between.
2. device according to claim 1 it is characterised in that in the described filler being attached with catalyst filler be that there are rule The metal gauze of the high-specific surface area of whole cavernous structure is it is preferred that described filler is specific surface area 650~750m2/m3, porosity 90~95% anodised aluminium ripple silk net.
3. device according to claim 1 and 2 is it is characterised in that catalyst in the described filler being attached with catalyst Active component is the combination of one or more of pd, mo, au and co, and auxiliary agent is one or more of ag, zn, in and mg.
4. device according to claim 3 is it is characterised in that described gas-liquid separator is impingement separator, gold Belong to filtering type gas-liquid separator, rotational flow type gas-liquid separater or the combined multi-stage gas-liquid separator of silk screen.
5. device according to claim 3 is it is characterised in that also including positioned at described liquid-inlet and being attached with catalyst Filler between liquid distribution trough, positioned at the described gas distributor being attached between the filler of catalyst and gas feed.
6. device according to claim 5 is it is characterised in that described liquid distribution trough is tank type liquid distributor.
7. the device according to claim 5 or 6 is it is characterised in that described gas distributor is included positioned at same level Many concentric tubees, be located at described concentric tube on multiple downward opening gas nozzle and the gas being connected with described concentric tube Tedge;
Pass through pipeline between described concentric tube to be connected, the other end of described vapor riser is connected with described gas feed.
8. device according to claim 7 it is characterised in that also include positioned at described liquid-inlet and liquid distribution trough it Between liquid level self-controller, described liquid level self-controller includes liquid level emasuring device, automatic admission valve and automatic air outlet valve; Keep the constant liquid level on liquid distributing board by controlling the pressure above liquid distributing board.
9. the device according to claim 1 or 8 is it is characterised in that divide in the described filler being attached with catalyst and gas It is provided with packing support device between cloth device.
10. device according to claim 1 is it is characterised in that include housing, and the outside of housing sets from the bottom up successively The liquid outlet put, gas feed, liquid level self-controller, liquid-inlet, gas outlet;
The inside of described housing is sequentially provided with from the bottom up, gas distributor, packing support device, is attached with the filler of catalyst, Liquid distribution trough, gas-liquid separator;
Described gas distributor be located at described gas feed on, described liquid distribution trough be located at described liquid level self-controller it Under, described gas-liquid separator is located between described liquid-inlet and described gas outlet;
Described filler is specific surface area 700m2/m3, the anodised aluminium ripple silk net of porosity 93%;The active component of catalyst Combination for one or more of pd, mo, au and co, auxiliary agent is one or more of ag, zn, in and mg;
Described liquid distribution trough is tank type liquid distributor;
Described gas distributor includes the many concentric tubees positioned at same level, the multiple opening courts on described concentric tube Under gas nozzle and the vapor riser being connected with described concentric tube;
Pass through pipeline between described concentric tube to be connected, the other end of described vapor riser is connected with gas feed;
Described liquid level self-controller includes liquid level emasuring device, automatic admission valve and automatic air outlet valve;Divided by controlling liquid Pressure above fabric swatch is keeping the constant liquid level on liquid distributing board;Described gas-liquid separator is impingement separator.
CN201620710002.4U 2016-07-06 2016-07-06 Device of acetylene selective hydrogenation system ethylene Active CN205886829U (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201620710002.4U CN205886829U (en) 2016-07-06 2016-07-06 Device of acetylene selective hydrogenation system ethylene

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201620710002.4U CN205886829U (en) 2016-07-06 2016-07-06 Device of acetylene selective hydrogenation system ethylene

Publications (1)

Publication Number Publication Date
CN205886829U true CN205886829U (en) 2017-01-18

Family

ID=57772308

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201620710002.4U Active CN205886829U (en) 2016-07-06 2016-07-06 Device of acetylene selective hydrogenation system ethylene

Country Status (1)

Country Link
CN (1) CN205886829U (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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

Similar Documents

Publication Publication Date Title
CN105175208B (en) Acetylene hydrogenation prepares the method for ethene and the reaction tower for this method
CN104826558B (en) Paste state bed reactor and response system for preparing ethylene by selective hydrogenation of acetylene
CN204973827U (en) A reaction tower for acetylene hydrogenation makes ethylene
CN104549060B (en) A kind of slurry bed circulatory flow reactor and application and the method for producing hydrogen peroxide
CN104107671B (en) Fluidized-bed reactor and the method for carrying out methanol to olefins reaction with the fluidized-bed reactor
CN105859502B (en) A kind of reaction system and method preparing ethylene
CN205886829U (en) Device of acetylene selective hydrogenation system ethylene
CN106629622A (en) Hydrogenation method and hydrogenation device for oxanthranol-containing working solution
CN107930540A (en) A kind of controlling temp type multilayer FCC reactor
CN206014415U (en) A kind of anthraquinone fixed bed reactors for producing hydrogen peroxide
CN101024603B (en) Methanol absorbing system
CN206616014U (en) A kind of hydrogenation apparatus of hydrogeneous anthraquinone working solution
CN104418309B (en) A kind of preparation method of hydrogen peroxide
CN206045986U (en) A kind of de- arylation reaction device of environmentally friendly hydrocarbon solvent low-voltage hydrogenation
CN105582854B (en) A kind of fixed bed hydrogenation reactor and application method
CN102498191A (en) Method for producing hydrocarbon oil and synthetic reaction system
CN205893120U (en) Reaction system of preparation ethylene
CN206045989U (en) A kind of response system of utilization prepared in slurry bed reactor for ethylene
CN205893121U (en) Utilize reaction system of thick liquid attitude bed reactor preparation ethylene
CN206051888U (en) A kind of response system for preparing ethylene
CN105944627A (en) Device for preparing ethylene from acetylene through selective hydrogenation
CN206519141U (en) Shell and tube paste state bed reactor and reaction system
CN106147849B (en) Two sections of heavy-oil slurry hydrogenation plants of one kind and method
CN100569725C (en) Formaldehyde absorbing method and system
CN209696864U (en) Synthesis reaction system with porous type central tube

Legal Events

Date Code Title Description
GR01 Patent grant
C14 Grant of patent or utility model
PP01 Preservation of patent right

Effective date of registration: 20201216

Granted publication date: 20170118

PP01 Preservation of patent right