CN105170035A - Hydrogenation reactor and method for preparing ethylene - Google Patents
Hydrogenation reactor and method for preparing ethylene Download PDFInfo
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- CN105170035A CN105170035A CN201510543784.7A CN201510543784A CN105170035A CN 105170035 A CN105170035 A CN 105170035A CN 201510543784 A CN201510543784 A CN 201510543784A CN 105170035 A CN105170035 A CN 105170035A
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- Y—GENERAL 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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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Abstract
The invention relates to a reactor for preparing ethylene through acetylene hydrogenation and a method for preparing ethylene. The reactor comprises a main body having an upper segment and a lower segment with two diameters, a product outlet formed in the lower segment of the main body and a catalyst bed layer positioned in the lower segment of the main body, wherein the catalyst bed layer is of grid structure and can be driven by a transmission shaft to rotate; a reactant feed inlet is formed at the center of the transmission shaft, and a plurality of atomizing nozzles are formed in the bottom of the transmission shaft. Due to the design of the grid, a catalyst can be fixed in the catalyst bed layer, so that breakage and loss of the catalyst are effectively reduced. Moreover, the reactant is attached to the surface of the catalyst through the atomizing nozzles in a liquid film manner for reaction, so that side reactions are further reduced, and a lot of heat released by the reaction is taken away at the maximum as the latent heat of vaporization, so that the temperature runaway phenomenon is avoided, and the utilization ratio of the catalyst and the ethylene yield are improved.
Description
Technical field
The present invention relates to a kind of hydrogenation reactor and prepare the method for ethene, belong to producing ethylene with acetylene hydrogenation technical field.
Background technology
In coal chemical technology, be that raw material produces acetylene by calcium carbide technique, extensive use with coal; Take acetylene as raw material again, under selective hydrocatalyst effect, by Hydrogenation for ethylene product.But because acetylene hydrogenation is strong exothermal reaction, traditional fixed bed device and catalyst move heat difficulty, cause temperature runaway phenomenon, uncontrollable acetylene hydrogenation reaction depth causes the deep hydrogenation of acetylene to generate ethane, and a large amount of reaction heat can make catalyst carbon deposition inactivation; In addition, the green oil that acetylene polymerization generates covers catalyst surface and causes rapid catalyst deactivation.
In order to overcome temperature runaway problem, existing researching and proposing adds liquid phase solvent heat transfer in the reactor.Prior art discloses and add water as liquid phase solvent in reactor; Or to acetylene, there is high Selective dissolution to adding in the reactor, ethene is had to the liquid phase solvent of low Selective dissolution.But be liquid phase solvent with water, be unfavorable for the dissolving of acetylene and being uniformly distributed of catalyst, water saturation vapour pressure is lower, easily undergoes phase transition and causes water content in ethene higher; And in the green oil water fast that catalyst surface generates.And adopt Selective dissolution solvents for ethyne, dissolve more polyacetylene in liquid phase, impel catalyst active center to adsorb more polyacetylene, when reaction temperature is too high or hydrogen deficient time, the acetylene of activated centre absorption easily generates a large amount of green oil and causes catalysqt deactivation, and yield of ethene declines.And, due to solid catalyst dispersion in the liquid phase, easily broken under gas disturbance and flow regime, wear and tear and carried by liquid product the loss causing catalyst; When catalyst regeneration, there is again the problems such as sad filter, difficult recovery and easy occluding device because catalyst grain size is little.
Summary of the invention
The object of the invention is to provide a kind of hydrogenation reactor, and it effectively can reduce fragmentation and the extent of deterioration of catalyst in course of reaction, has floor space little, the feature that treating capacity is large.
To achieve these goals, the present invention adopts following technical scheme:
For a reactor for producing ethylene with acetylene hydrogenation, its front view as shown in Figure 1, comprises the main body of upper and lower section of two kinds of diameters, is positioned at the product exit of hypomere main body, and is positioned at the beds of hypomere main body;
Wherein, described beds is cell structure, the power transmission shaft that the center establishes to run through main body, is connected with rotary electric machine bottom power transmission shaft; Described power transmission shaft is connected with beds, and beds can be driven to rotate;
Wherein, described center transmission shaft place establishes a reaction-ure feeding pipe, and its bottom is positioned at catalyst bed interlayer, and the surface being positioned at the reaction-ure feeding tube portion of catalyst bed interlayer is provided with multiple atomizer.
Acetylene hydrogenation reactor of the present invention drives power transmission shaft and beds to rotate by rotary electric machine, make the wetting catalyst surface rapidly of the solution after atomization, and under fast rotational state, form liquid film, when there is hydrogenation reaction in reaction raw materials in the reacting environment that catalyst and liquid film provide, product can desorption reaction place rapidly, thus effectively avoids the generation of acetylene deep hydrogenation and ethene hydrogenation side reaction again.In addition, because catalyst can be fixed in beds by the design of grid, fragmentation and the loss of catalyst is effectively reduced.Simultaneous reactions thing is attached to catalyst surface through atomizer with form of liquid film and reacts, the generation of further minimizing side reaction, and the amount of heat of reaction release is taken away to greatest extent in latent heat of vaporization mode, avoid temperature runaway phenomenon, improve catalyst utilization and ethylene yield.
In reactor of the present invention, described beds built with solid catalyst, and is fixed it by grid.
In reactor of the present invention, described Grill space is 3-100mm; Preferred 5-10mm.
In reactor of the present invention, 10-100mm, preferred 10-15mm above the position of opening distance beds of described atomizer, 3-100mm, preferred 5-10mm below beds.
In reactor of the present invention, the laying length of described atomizer and beds aspect ratio are 0.5-1:1, preferred 0.8:1.
In reactor of the present invention, the aperture of described atomizer is 0.1 ~ 1mm, preferred 0.2-0.8mm; Pitch of holes is 1 ~ 5mm.
In reactor of the present invention, described product exit is positioned at the upper end of beds, and concordant with the most top layer of beds.
The present invention also provides a kind of method utilizing above-mentioned reactor to prepare ethene, comprises the steps:
(1) the reactant input reaction-ure feeding mouth will be mixed to get by acetylene, hydrogen, solvent;
(2) reactant to be overlying on form of liquid film through atomizer and to be fixed in bed grid, and keeps the catalyst surface of rotation status to react;
(3), after reaction terminates, gained gas-liquid mixture is flowed out by product exit.
Wherein, in step (1), the volume ratio of described solvent, acetylene, hydrogen is 1:4 ~ 200:8 ~ 900; Because atomizer aperture is less, and beds is in rotation status, and reactant mixes within the scope of aforementioned proportion promptly can form liquid film at catalyst surface, thus realizes technique effect of the present invention.In the present invention, feeding manner can adopt hydrogen, acetylene and liquid respectively charging be mixed to form reactant, or first by acetylene gas dissolve be mixed to form reactant with hydrogen more in the solution.
Wherein, in step (1), described solvent is high to acetylene solubility, the organic solvent low to ethylene dissolution degree; Preferred 1-METHYLPYRROLIDONE (NMP).
Wherein, in step (2), described catalyst is with molecular sieve, aluminium oxide, silica, kaolin and imvite etc. for carrier, the catalyst of load P d active metal and Ag auxiliary agent; Wherein, the tenor of Pd is the mass ratio of 0.01 ~ 0.1% (wt), Pd and Ag is 1:1 ~ 5.
Wherein, in step (2), reaction temperature is 100 ~ 200 DEG C.
Wherein, in step (2), described beds rotating speed is 50 ~ 1000rpm, preferred 500-600rpm.
Beneficial effect of the present invention is as follows:
In acetylene hydrogenation device, catalyst is fixed on the fragmentation and loss that can reduce catalyst in beds by grid.Reactant is attached to catalyst surface with form of liquid film and reacts after atomizer, and due to the solubility of solvent to ethene lower, the further hydrogenation side reaction of ethene can not be caused.Meanwhile, solvent exists with form of liquid film can carry in acetylene hydrogenation course of reaction the large calorimetric of releasing to greatest extent, and takes away in the mode of the latent heat of vaporization.Catalyst regeneration can adopt monoblock type regeneration, simple and easy to operate.Whole device is in rotation status due to beds, and acetylene is produced in the first step flash hydrogcnation reaction being applicable to selective hydrogenation of acetylene.And this hydrogenation plant significantly can reduce the floor space of selective hydrogenation of acetylene device, the treating capacity of aggrandizement apparatus.
Accompanying drawing explanation
Fig. 1 is the structural representation of hydrogenation reactor of the present invention.
Detailed description of the invention
Following examples for illustration of the present invention, but are not used for limiting the scope of the invention.
Embodiment 1 one kinds of acetylene hydrogenation reactors
For a reactor for producing ethylene with acetylene hydrogenation, its front view as shown in Figure 1, comprises the main body of upper and lower section of two kinds of diameters, is positioned at the product exit of hypomere main body, and is positioned at the beds 4 of hypomere main body;
Wherein, described beds is cell structure 7, the power transmission shaft 2 that the center establishes to run through main body, is connected with rotary electric machine 5 bottom power transmission shaft; Described power transmission shaft is connected with beds, and beds can be driven to rotate;
Wherein, described center transmission shaft place establishes a reaction-ure feeding pipe 1, and its bottom is positioned at catalyst bed interlayer, and the surface being positioned at the reaction-ure feeding tube portion of catalyst bed interlayer is provided with multiple atomizer 3.
Wherein, described beds built with solid catalyst, and is fixed it by grid.
Wherein, described Grill space is 6mm.
Wherein, described atomizer length is 16cm, and catalyst bed layer height is 20cm.
Wherein, described atomizer perforate 35, aperture is 2mm; The pitch-row beds upper end level of top is 12mm, and under beds, segment distance is 6mm.
Wherein, described product exit 6 is positioned at the upper end of beds, and concordant with the most top layer of beds.
The method of embodiment 2 one kinds of acetylene ethene
Utilize reactor described in embodiment 1 to prepare a method for ethene, comprise the steps:
(1) reactant be mixed to get by acetylene, hydrogen, solvent is inputted in reaction-ure feeding mouth;
(2) reactant to be overlying on form of liquid film through atomizer and to be fixed in beds grid, and keeps the catalyst surface of rotation status to react;
(3), after reaction terminates, gained gas-liquid mixture is flowed out by product exit.
Wherein, in step (1), acetylene raw gas pressure is 0.3MPa, and hydrogen feed gas is 0.3MPa, and nmp solution is suppressed to 0.3MPa by pump, and three enters reactor after being mixed to form reactant.Wherein, the flow-control of acetylene is at 10Nm
3/ h, the flow of hydrogen is 40Nm
3the flow of/h, NMP is 3m
3/ h.
Wherein, in step (2), the catalyst that beds adopts is α-Al
2o
3bead, particle size distribution range is 2 ~ 5mm, supported active metals Pd and Ag.The load capacity of Pd is the load capacity of 0.02% (wt), Ag is 0.05% (wt).
Wherein, in step (2), bed temperature controls at 150 DEG C.
Wherein, in step (2), described beds rotating speed is 600rpm.
After this device process, the conversion ratio of acetylene is 99.8%, and the selective of ethene is 87%.
Although above the present invention is described in detail with a general description of the specific embodiments, on basis of the present invention, can make some modifications or improvements it, this will be apparent to those skilled in the art.Therefore, these modifications or improvements without departing from theon the basis of the spirit of the present invention, all belong to the scope of protection of present invention.
Claims (10)
1. for a reactor for producing ethylene with acetylene hydrogenation, it is characterized in that, comprise the main body of upper and lower section of two kinds of diameters, be positioned at the product exit of hypomere main body, and be positioned at the beds of hypomere main body;
Wherein, described beds is cell structure, the power transmission shaft that the center establishes to run through main body, is connected with rotary electric machine bottom power transmission shaft; Described power transmission shaft is connected with beds, and beds can be driven to rotate;
Described center transmission shaft place establishes a reaction-ure feeding pipe, and its bottom is positioned at catalyst bed interlayer, and the surface being positioned at the reaction-ure feeding tube portion of catalyst bed interlayer is provided with multiple atomizer.
2. reactor according to claim 1, is characterized in that, described beds built with solid catalyst, and is fixed it by grid.
3. reactor according to claim 1, is characterized in that, described Grill space is 3-100mm.
4. reactor according to claim 1, is characterized in that, 10-100mm, 3-100mm below beds above the position of opening distance beds of described atomizer.
5. reactor according to claim 1, is characterized in that, the laying length of described atomizer and beds aspect ratio are 0.5-1:1.
6. reactor according to claim 1, is characterized in that, the aperture of described atomizer is 0.1 ~ 1mm, and pitch of holes is 1 ~ 5mm.
7. reactor according to claim 1, is characterized in that, described product exit is positioned at the upper end of beds, and concordant with the most top layer of beds.
8. utilize the arbitrary described reactor of claim 1-7 to prepare the method for ethene, it is characterized in that, comprise the steps:
(1) the reactant input reaction-ure feeding mouth will be mixed to get by acetylene, hydrogen, solvent;
(2) reactant to be overlying on form of liquid film through atomizer and to be fixed in bed grid, and keeps the catalyst surface of rotation status to react;
(3), after reaction terminates, gained gas-liquid mixture is flowed out by product exit.
9. method according to claim 8, is characterized in that, in step (2), reaction temperature is 100 ~ 200 DEG C.
10. method according to claim 8, is characterized in that, in step (2), described beds rotating speed is 50 ~ 1000rpm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510543784.7A CN105170035A (en) | 2015-08-28 | 2015-08-28 | Hydrogenation reactor and method for preparing ethylene |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510543784.7A CN105170035A (en) | 2015-08-28 | 2015-08-28 | Hydrogenation reactor and method for preparing ethylene |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20050049445A1 (en) * | 2003-09-03 | 2005-03-03 | Synfuels International, Inc. | Process for liquid phase hydrogenation |
| CN1895766A (en) * | 2005-07-14 | 2007-01-17 | 中国石油化工股份有限公司 | Catalytic selective hydrogenation |
| CN102489225A (en) * | 2011-12-10 | 2012-06-13 | 太原理工大学 | Slurry bubble column technology for preparing ethylene through acetylene hydrogenation and device thereof |
| CN103992200A (en) * | 2014-05-20 | 2014-08-20 | 榆林科大高新能源研究院有限公司 | Process method for obtaining acetylene gas from semi-coke via calcium carbide and further producing ethylene by hydrogenation |
| CN204973829U (en) * | 2015-08-28 | 2016-01-20 | 北京神雾环境能源科技集团股份有限公司 | Hydrogenation reactor |
-
2015
- 2015-08-28 CN CN201510543784.7A patent/CN105170035A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20050049445A1 (en) * | 2003-09-03 | 2005-03-03 | Synfuels International, Inc. | Process for liquid phase hydrogenation |
| CN1895766A (en) * | 2005-07-14 | 2007-01-17 | 中国石油化工股份有限公司 | Catalytic selective hydrogenation |
| CN102489225A (en) * | 2011-12-10 | 2012-06-13 | 太原理工大学 | Slurry bubble column technology for preparing ethylene through acetylene hydrogenation and device thereof |
| CN103992200A (en) * | 2014-05-20 | 2014-08-20 | 榆林科大高新能源研究院有限公司 | Process method for obtaining acetylene gas from semi-coke via calcium carbide and further producing ethylene by hydrogenation |
| CN204973829U (en) * | 2015-08-28 | 2016-01-20 | 北京神雾环境能源科技集团股份有限公司 | Hydrogenation reactor |
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Effective date of registration: 20161010 Address after: 102200 Beijing City, Changping District science and Technology Park Fukang Road No. 18 Applicant after: Beijing Huafu Engineering Co., Ltd. Address before: 102200 Beijing city Changping District Machi Town cow Road No. 18 Applicant before: Beijing Shenwu Environment Energy Technology Group Co., Ltd. |
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Application publication date: 20151223 |