CN204973827U - A reaction tower for acetylene hydrogenation makes ethylene - Google Patents
A reaction tower for acetylene hydrogenation makes ethylene Download PDFInfo
- Publication number
- CN204973827U CN204973827U CN201520595697.1U CN201520595697U CN204973827U CN 204973827 U CN204973827 U CN 204973827U CN 201520595697 U CN201520595697 U CN 201520595697U CN 204973827 U CN204973827 U CN 204973827U
- Authority
- CN
- China
- Prior art keywords
- reaction tower
- liquid
- column plate
- gas
- reaction
- 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
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to a reaction tower for acetylene hydrogenation makes ethylene. The reaction tower is the solid three -phase mass transfer equipment of gas -liquid, and its structure includes tower body, liquid phase exit, gaseous phase exit, column plate, air distributor, vapour and liquid separator, downspout, wherein, the column plate has the sieve structure and/or has the injection apparatus structure. Adopt the reaction tower, can solve the problem that the difficulty was removed to high -purity acetylene hydrogenation system ethylene fixed bed " temperature runaway " and reaction heat, avoided that the bed pressure drop is big, the acetylene polymerization generates the green oil and covers the defect that the inactivation was sent to the catalyst, overcome simultaneously the solid homogeneous mixing difficulty of thick liquid attitude bed gas -liquid, the easy deposit of catalyst granules again, air distributor easily blocks up and liquid phase solvent quantity defect such as big.
Description
Technical field
The utility model relates to a kind of reaction tower for producing ethylene with acetylene hydrogenation, belongs to technical field of chemical material preparation.
Background technology
Ethene is most important basic material, is called as " mother of petrochemical industry ".Take acetylene as raw material, under selective hydrocatalyst effect, Hydrogenation is for ethene, in conjunction with ethene PVC, China's tradition acetylene can not only be solved and directly produce mercury consumption and a mercury pollution difficult problem in PVC process, and expand Coal Chemical Industry Route further, simultaneously for ethylene industry provides a kind of new raw material to originate, and reduce ethene to the degree of dependence of petroleum resources and production cost of ethylene, have broad application prospects.
The technique preparing ethene with high concentration acetylene for catalytic material selec-tive hydrogenation is at present carried out usually in fixed bed or slurry bed system.But because acetylene hydrogenation is strong exothermal reaction, reactant concentration of acetylene is higher, and reaction speed is faster, and exothermic heat of reaction is more, and easily cause catalytic bed " temperature runaway ", cause catalyst with sintering deactivation, and acetylene is easily polymerized generation green oil, covering catalyst causes inactivation.Meanwhile, ubiquity gas-liquid-solid Homogeneous phase mixing difficulty, the defect such as operating flexibility is little, catalyst granules easily deposits, gas distributor easily blocks and liquid phase solvent consumption is large.
Utility model content
The purpose of this utility model is to provide a kind of reaction tower for producing ethylene with acetylene hydrogenation, it can realize gas-liquid-solid phase reaction, solve the problem that high purity acetylene Hydrogenation ethene fixed bed " temperature runaway " and reaction heat remove difficulty, avoid that bed pressure drop is large, acetylene polymerization generates the defect that green oil covering catalyst causes inactivation; The defect such as simultaneously overcome again slurry bed system gas-liquid-solid Homogeneous phase mixing difficulty, catalyst granules easily deposits, gas distributor easily blocks and liquid phase solvent consumption is large.
To achieve these goals, the utility model adopts following technical scheme:
For a reaction tower for producing ethylene with acetylene hydrogenation, described reaction tower is gas-liquid-solid three-phase mass transfer apparatus, and it comprises tower body, liquid phase import and export, gas phase import and export, column plate, gas distributor, gas-liquid separator, downspout;
Wherein, described column plate is with sieve-plate structure and/or with injection apparatus structure.
Reaction tower described in the utility model, column plate is equipped with catalyst, gas phase reaches column plate through sieve plate or injection apparatus from bottom to top, it is that serpentine flow is through column plate that liquid phase passes through downspout, liquid phase fully contacts with catalyst at column plate place, the fixed beds such as slurry bed system " temperature runaway " and reaction heat effectively can be avoided to remove the problem of difficulty, avoid the defect that bed pressure drop is large, acetylene polymerization generation green oil covering catalyst causes inactivation; The defect such as simultaneously overcome again slurry bed system gas-liquid-solid Homogeneous phase mixing difficulty, catalyst granules easily deposits, gas distributor easily blocks and liquid phase solvent consumption is large.
In reaction tower described in the utility model, described column plate comprises overfall, seal pot and reaction member; Described injection apparatus is arranged in reaction member, comprises riser and jet cover.
Wherein, described riser is cylindrical, taper, wedge shape or trapezoidal, high 10-100mm; Described jet cover is pyramidal structure, and top has some spray-holes, and jet cover and tray spacing are 5-25mm, is 1-10mm with riser spacing bottom jet cover.Filling solid catalyst between described injection apparatus, loading height is 150mm.The injection apparatus that the present invention proposes greatly improves acetylene and liquid phase solvent contact area, is conducive to acetylene rapid solution.
In reaction tower described in the utility model, the percent opening of described column plate is 1-20%, preferred 10-13%, and number is 2-30.Reasonable Arrangement position of opening and quantity are conducive to gas-liquid and fully contact, provide liquid phase solvent utilization rate and reaction tower operating flexibility.
In reaction tower described in the utility model, described column plate is 8-30 layer altogether, and every interlamellar spacing is 280-330mm; Rational reaction compartment is more conducive to sufficient reacting to carry out, and product is overflowed, and avoids pressure drop greatly to the adverse effect of reaction simultaneously.
Wherein, described gas-liquid separator is the one in wire mesh demister, cyclone separator, swirl separator or deflection plate.
Reaction tower described in the utility model is used for the method that acetylene hydrogenation prepares ethene, and concrete steps are as follows:
1) acetylene and hydrogen are to enter from the gas phase import of reaction tower bottom through compressor boost after certain proportion mixing, move from bottom to top after gas distributor distribution in reaction tower; Meanwhile, liquid phase solvent enters from the fluid inlet on reaction tower top and moves from top to down in reaction tower;
2) liquid phase material the first column plate place contact in reaction tower, and hydrogenation reaction is there is under solid catalyst effect on column plate, generate ethene;
3) ethene is overflowed from liquid phase solvent, and unreacted acetylene continues reaction along with gaseous mixture rises to last layer column plate;
4) remove after the liquid phase solvent wherein carried secretly through gas-liquid separator from reaction tower the superiors column plate gaseous mixture out, leave reaction tower by the gaseous phase outlet at reaction tower top, enter later separation operation through overhead condenser; Liquid phase solvent is back to fluid inlet and recycles after then flowing out from the liquid-phase outlet bottom reaction tower after removal of impurities.
Wherein, step 1) in, the volume ratio of described acetylene and hydrogen is 1:1-8, preferred 1:5.
Wherein, step 1) in, described liquid phase solvent be selected from ethylenediamine, paraffin, pyridine, acetone, METHYLPYRROLIDONE, ionic liquid or cyclohexanone one or more, preferred METHYLPYRROLIDONE.
Wherein, step 2) in, described hydrogenation conditions is: operating pressure is 0.1-2.5MPa, and operating temperature is 70-210 DEG C; Preferred pressure is 02-1.8MPa, and operating temperature is 120-160 DEG C.
Wherein, the active component of described solid catalyst is selected from one or more in palladium, silver, platinum, cobalt, tungsten, molybdenum, nickel, zinc, iron, calcium, magnesium, zirconium, cerium, phosphorus and boron etc.; Its carrier is one or more mixing in active carbon, carbon fiber, carbon felt, aluminium oxide, molecular sieve, titanium oxide, silica, pottery, float stone, diatomite and clay etc.; Filling form is that regular catalyst is directly laid or solid particle catalyst Zha Bao places, and loading height is 10-200mm.
The beneficial effects of the utility model are:
Monoblock type can be adopted in producing ethylene with acetylene hydrogenation reaction tower described in the utility model or prick packet mode loading catalyst, load and draw off convenience, loadings is large, pressure drop is little and does not block gas distribution tube, overcome slurry bed system solid particle catalyst skewness, easily the defect such as deposition and equipment attrition; Reaction tower space availability ratio is high, solution height on column plate, loaded catalyst is adjustable, and operating flexibility is large; Gas-liquid-solid contact is good, the time of staying is long, conversion of alkyne is high, and reaction tower disposal ability is large; Reaction tower can utilize exothermic heat of reaction maintenance reaction to carry out, and in tower, heat exchange element and condenser conveniently regulate temperature, avoid fixed bed temperature runaway and cause the problem that catalysqt deactivation, by-product green oil and yield of ethene are low.Mercury consumption and the difficult problem of mercury pollution when the utility model can not only solve China tradition acetylene production PVC, and expand Coal Chemical Industry Route further, simultaneously for ethylene industry provides a kind of new raw material to originate, and reduce ethene to the degree of dependence of petroleum resources and production cost of ethylene.
Accompanying drawing explanation
Fig. 1 is reaction tower structural representation in the utility model embodiment.
Fig. 2 is column plate top view.
Fig. 3 is the front view of injection apparatus in column plate.
In figure: 1-tower body; 2-gas distributor; The import of 3-gas phase; 4-liquid-phase outlet; 5-column plate; 6-downspout; 7-fluid inlet; 8-gaseous phase outlet; 9-gas-liquid separator (demister); 10-seal pot; 11-overfall; 12-injection apparatus; 13-solid catalyst; 14-jet cover; 15-riser.
Detailed description of the invention
Following examples for illustration of the utility model, but are not used for limiting scope of the present utility model.
Embodiment 1
For a reaction tower for producing ethylene with acetylene hydrogenation, described reaction tower is gas-liquid-solid three-phase mass transfer apparatus, reaction tower diameter 600mm, height overall 5m.As Figure 1-3, its structure comprises tower body 1, and liquid phase imports and exports 7,4, and gas phase imports and exports 3,8, column plate 5, gas distributor 2, gas-liquid separator 9, downspout 6;
Wherein, tower tray 5 arranges 10 layers altogether, and spacing is 300mm; It comprises overfall 11, seal pot 10 and reaction member; Be provided with multiple injection apparatus 12 in reaction member, described injection apparatus comprises riser 15 and jet cover 14, and the percent opening of described injection apparatus is 13%.Described riser 15 is conical, hollow, head-up little, high 50mm; Described jet cover 14 is pyramidal structure, and spray-hole is evenly opened in top, and bottom and tower tray 5 spacing are 10mm, are 5mm with riser 15 spacing.Filling solid catalyst 13 between described injection apparatus 12, loading height is 150mm.
Wherein, described gas-liquid separator is wire mesh demister.
The method utilizing above-mentioned reaction tower to prepare ethene comprises the steps:
1) by particle type catalyst Zha Bao, filling even is between injection apparatus 12, with inert gas, reacting pipe and equipment are purged, after oxygen content detection is qualified, liquid phase solvent METHYLPYRROLIDONE pumps into from fluid inlet 7 and moves from top to bottom, when reaction tower bottoms level reaches 50%, from liquid-phase outlet 4 Extract phase solvent continuously, be back to fluid inlet after delivering to regeneration or heat exchange unit process and recycle.
Switched to by nitrogen hydrogen and acetylene volume ratio to be the gaseous mixture of 5:1, enter from reaction tower bottom gas phase import 3 through compressor supercharging, move from bottom to top in reaction tower after gas distributor 2 distributes;
2) liquid phase material is in the contact of orlop column plate place, and under solid catalyst effect, hydrogenation reaction occurs on column plate, generates ethene;
3) ethene is overflowed from liquid phase solvent, and unreacted acetylene continues reaction along with gaseous mixture rises to last layer column plate;
4) remove after the liquid phase solvent wherein carried secretly through gas-liquid separator from reaction tower the superiors column plate gaseous mixture out, leave reaction tower by the gaseous phase outlet at reaction tower top, enter later separation operation through overhead condenser; Liquid phase solvent is then back to fluid inlet and recycles after the liquid-phase outlet outflow removal of impurities bottom reaction tower.
Wherein, step 1) in, the volume ratio of described acetylene and hydrogen is 1:5.Wherein, step 2) in, described hydrogenation conditions is: operating pressure is 0.3MPa, and operating temperature is 120-160 DEG C.
Detect: overhead product gas detects through chromatography of gases, and conversion of alkyne is 96.58%, and yield of ethene is 87.99%.Full tower pressure drop is 540mmH
2o.
Although above done detailed description to the utility model with a general description of the specific embodiments, on the utility model basis, can make some modifications or improvements it, this will be apparent to those skilled in the art.Therefore, these modifications or improvements on the basis of not departing from the utility model spirit, all belong to the scope that the utility model is claimed.
Claims (9)
1. for a reaction tower for producing ethylene with acetylene hydrogenation, it is characterized in that, described reaction tower is gas-liquid-solid three-phase mass transfer apparatus, and its structure comprises tower body, liquid phase import and export, gas phase import and export, column plate, gas distributor, gas-liquid separator, downspout;
Wherein, described column plate is with sieve-plate structure and/or with injection apparatus structure.
2. reaction tower according to claim 1, is characterized in that, described column plate comprises overfall, seal pot and reaction member; Described injection apparatus is arranged in reaction member, comprises riser and jet cover.
3. reaction tower according to claim 2, is characterized in that, described riser height 10-100mm; Be 5-25mm with tray spacing bottom described jet cover, described jet cover and riser spacing are 1-10mm.
4. the reaction tower according to Claims 2 or 3, is characterized in that, described riser is cylindrical, taper, wedge shape or trapezoidal.
5. the reaction tower according to Claims 2 or 3, is characterized in that, described jet cover is pyramidal structure, and top has some spray-holes.
6., according to the arbitrary described reaction tower of claim 1-3, it is characterized in that, the percent opening of described column plate is 1-20%.
7. reaction tower according to claim 6, is characterized in that, the percent opening of described column plate is 10-13%.
8., according to the arbitrary described reaction tower of claim 1-3, it is characterized in that, described column plate is 8-30 layer altogether, and every interlamellar spacing is 280-330mm.
9., according to the arbitrary described reaction tower of claim 1-3, it is characterized in that, described gas-liquid separator is the one in wire mesh demister, cyclone separator, swirl separator or deflection plate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520595697.1U CN204973827U (en) | 2015-08-07 | 2015-08-07 | A reaction tower for acetylene hydrogenation makes ethylene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520595697.1U CN204973827U (en) | 2015-08-07 | 2015-08-07 | A reaction tower for acetylene hydrogenation makes ethylene |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204973827U true CN204973827U (en) | 2016-01-20 |
Family
ID=55108247
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520595697.1U Active CN204973827U (en) | 2015-08-07 | 2015-08-07 | A reaction tower for acetylene hydrogenation makes ethylene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204973827U (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105797651A (en) * | 2016-05-25 | 2016-07-27 | 北京神雾环境能源科技集团股份有限公司 | Gas demister of slurry bed for hydrogenation of acetylene to ethylene |
| CN105833806A (en) * | 2016-05-27 | 2016-08-10 | 北京神雾环境能源科技集团股份有限公司 | Gas foam remover for acetylene hydrogenation type ethylene preparation three-phase fluidized bed |
| CN105833803A (en) * | 2016-05-27 | 2016-08-10 | 北京神雾环境能源科技集团股份有限公司 | Gas foam remover for acetylene hydrogenation type ethylene preparation packing bubbling bed |
| CN105833801A (en) * | 2016-05-27 | 2016-08-10 | 北京神雾环境能源科技集团股份有限公司 | Gas foam remover for acetylene hydrogenation type ethylene preparation trickle bed |
| 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 |
| CN108250016A (en) * | 2016-12-29 | 2018-07-06 | 中国石油天然气股份有限公司 | A kind of acetylene hydrogenation method of preparing light olefins from methanol |
| CN112915933A (en) * | 2021-01-29 | 2021-06-08 | 常州大学 | Large-flux continuous gas-liquid heterogeneous reactor |
| CN113209912A (en) * | 2021-05-26 | 2021-08-06 | 中国石油化工股份有限公司 | Up-flow fixed bed reactor and outlet collector thereof |
-
2015
- 2015-08-07 CN CN201520595697.1U patent/CN204973827U/en active Active
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105797651A (en) * | 2016-05-25 | 2016-07-27 | 北京神雾环境能源科技集团股份有限公司 | Gas demister of slurry bed for hydrogenation of acetylene to ethylene |
| CN105797651B (en) * | 2016-05-25 | 2019-02-12 | 北京华福工程有限公司 | A kind of gas demister for producing ethylene with acetylene hydrogenation slurry bed system |
| CN105833806A (en) * | 2016-05-27 | 2016-08-10 | 北京神雾环境能源科技集团股份有限公司 | Gas foam remover for acetylene hydrogenation type ethylene preparation three-phase fluidized bed |
| CN105833803A (en) * | 2016-05-27 | 2016-08-10 | 北京神雾环境能源科技集团股份有限公司 | Gas foam remover for acetylene hydrogenation type ethylene preparation packing bubbling bed |
| CN105833801A (en) * | 2016-05-27 | 2016-08-10 | 北京神雾环境能源科技集团股份有限公司 | Gas foam remover for acetylene hydrogenation type ethylene preparation trickle bed |
| 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 |
| CN108250016A (en) * | 2016-12-29 | 2018-07-06 | 中国石油天然气股份有限公司 | A kind of acetylene hydrogenation method of preparing light olefins from methanol |
| CN112915933A (en) * | 2021-01-29 | 2021-06-08 | 常州大学 | Large-flux continuous gas-liquid heterogeneous reactor |
| CN113209912A (en) * | 2021-05-26 | 2021-08-06 | 中国石油化工股份有限公司 | Up-flow fixed bed reactor and outlet collector thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN204973827U (en) | A reaction tower for acetylene hydrogenation makes ethylene | |
| CN105175208B (en) | Acetylene hydrogenation prepares the method for ethene and the reaction tower for this method | |
| CN100563829C (en) | Integral supported carbon molecular sieve catalyst and preparation method thereof is used | |
| CN104826558A (en) | Slurry bed reactor and reaction system for producing ethylene by using acetylene selective hydrogenation | |
| CN102489225B (en) | Slurry bubble column technology for preparing ethylene through acetylene hydrogenation and device thereof | |
| CN103044179A (en) | Method for preparing ethylene through liquid-phase selective hydrogenation of acetylene in slurry reactor | |
| CN105582854A (en) | Fixed bed hydrogenation reactor and application method thereof | |
| CN110980742A (en) | Reactive distillation purification method and device for removing carbon-containing impurities in chlorosilane | |
| CN104418309A (en) | Method for preparing hydrogen peroxide | |
| CN105561617A (en) | Efficient catalysis rectification apparatus and applications thereof | |
| CN102463072B (en) | Reaction device for producing p-xylene | |
| CN102068945A (en) | Reactive distillation device and method for separating and purifying methylal | |
| CN104130097A (en) | Process for continuously preparing exo-tetrahydrodicyclopentadiene in liquid phase | |
| CN211964113U (en) | Ethylene glycol liquid phase hydrogenation reactor | |
| JP2023522374A (en) | Production apparatus and preparation method for poly-α-olefin | |
| CN204522947U (en) | For paste state bed reactor and the reaction system of preparing ethylene by selective hydrogenation of acetylene | |
| CN1634860A (en) | Gas distributor in fluidized bed of aniline synthesis and aniline synthesis method | |
| CN105060297A (en) | Method and apparatus for producing trichlorosilane | |
| CN206519141U (en) | Shell and tube paste state bed reactor and reaction system | |
| CN102463085B (en) | Reaction device for producing dimethylbenzene from methanol or dimethyl ether and methylbenzene | |
| CN106311094B (en) | Fischer-Tropsch catalyst reduction reactor and Fischer-Tropsch catalyst reduction method | |
| CN104419453A (en) | Method for selective hydrogenation of unsaturated polyhydrocarbon | |
| CN107235821B (en) | Device, method and application for preparing olefin from methanol | |
| CN102649564B (en) | Method for dehydrogenating CO-containing mixed gas raw material by means of catalytic oxidation reaction | |
| CN105561615A (en) | Catalysis rectification apparatus and applications thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| 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: 20160930 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 | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20200602 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. |