CN109876739A - A kind of fixed bed reactors - Google Patents
A kind of fixed bed reactors Download PDFInfo
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- CN109876739A CN109876739A CN201910221899.2A CN201910221899A CN109876739A CN 109876739 A CN109876739 A CN 109876739A CN 201910221899 A CN201910221899 A CN 201910221899A CN 109876739 A CN109876739 A CN 109876739A
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Abstract
The invention discloses a kind of fixed bed reactors, including catalyst reaction bed, the catalyst reaction bed includes at least two layers of reaction zone；Each reaction zone is equipped with multiple reacting spaces；The reacting space of reaction zone described in adjacent two layers is staggered；Filled with the catalyst granules that partial size is different in the adjacent reaction interval of same reaction zone.The present invention flows material in the shape of a spiral in catalyst reaction bed, different material can be made to come into full contact with reaction using the catalyst reaction bed for intersecting fish bone structure, thus with high efficiency, the features such as low material consumption, low energy consumption.
Description
Technical field
The invention belongs to fixed bed reactors fields, and in particular to a kind of fixed bed reactors.
Background technique:
Fixed bed reactors refer to loads particulate solid catalyst or solid reactant in reactor, is formed certain high
The accumulation bed of degree while gas or liquid material flow through static fixed bed by particulate interspaces, realizes heterogeneous reaction
Process.It is different from the moving bed and fluidized bed that solid material moves in equipment, the solid filled in fixed bed reactors
Particle is fixed, therefore also known as packed bed reactor, is one of widest chemical reactor of current industrial application.
Fixed bed reactors are not only simple in structure, easy to operate, and compared with moving bed and fluidized bed, have catalyst
The features such as mechanical loss is small, and service efficiency is high, still, for such reactor due to the presence of granule filler, material flows through catalysis
The resistance of agent reaction bed is larger, and flowing is more slow, and flows approximate laminar flow, will lead to point between different liquids (i.e. material)
Phase causes reaction efficiency low so that material be made to be unable to fully contact and react, and material consumption, energy consumption are high.
Summary of the invention
The purpose of the present invention is to provide a kind of fixed bed reactors, have not only given full play to the excellent of fixed bed reactors
Point has also been significantly greatly increased the mixability between different material, and then can improve reaction efficiency, reduces material consumption and energy consumption.
A kind of fixed bed reactors, including catalyst reaction bed, the catalyst reaction bed include at least two layers of reaction zone；
Each reaction zone is equipped with multiple reacting spaces；The reacting space of reaction zone described in adjacent two layers is staggered；Same reaction
Filled with the catalyst granules that partial size is different in the adjacent reaction interval in area.
It preferably, further include hollow housing, the inner cavity of the shell is adapted with the shape of catalyst reaction bed, the shell
One end on body corresponding to catalyst reaction bed offers feed inlet, offers discharging corresponding to the other end of catalyst reaction bed
Mouthful.
Preferably, distributor is additionally provided at the feed inlet of the shell.
Preferably, staggered two reacting spaces are obliquely installed in opposite direction in adjacent reaction area.
Preferably, the angle of staggered two reacting spaces is 0-180 degree in adjacent reaction area.
Preferably, the catalyst granules includes: coarse grain diameter catalyst granules that partial size is 1~2mm and partial size is 0.25
The fine grain catalyst granules of~0.75mm.
Preferably, the axial length of each reacting space is 0.25%-25% times of total reactor length, and axial
Length > 2cm.
Preferably, the porosity in same reaction interval, the coefficient of conductivity are all the same, the coefficient of conductivity of adjacent two reacting space
Difference, but porosity is identical.
The present invention has the advantages that this kind intersects fish bone structure fixed bed reactors, intersect fish bone structure using multilayer
Catalyst reaction bed makes streamline of the material by catalyst reaction bed when twist, different material can be made to come into full contact with instead
It answers, to have higher efficiency, material consumption, energy consumption are relatively low.
Detailed description of the invention
Fig. 1 shows the vertical cross section schematic diagram of double-layer catalyst reaction bed in the present invention；
Fig. 2 shows the three-dimensional figure of double-layer catalyst reaction bed in the present invention；
Fig. 3 shows the top view of double-layer catalyst reaction bed in the present invention；
Fig. 4 is the product distribution map of the embodiment of the present invention and comparative example；
Fig. 5 is the streamline and equal hydraulic head surfaces of the embodiment of the present invention；
Fig. 6 is the streamline and equal hydraulic head surfaces of comparative example of the present invention.
Wherein: 1- feed inlet, 2- distributor, 3- reactor left head, 4- shell, 5- catalyst reaction bed, 6- reactor
Right end socket, 7- discharge port.
Specific embodiment
To be easy to understand the technical means, the creative features, the aims and the efficiencies achieved by the present invention, below with reference to
Specific embodiment, the present invention is further explained.
As shown in Figure 1, a kind of fixed bed reactors include catalyst reaction bed, the catalyst reaction bed includes at least two
Layer reaction zone；Each reaction zone is equipped with multiple reacting spaces；The reacting space of reaction zone described in adjacent two layers is staggered；
Filled with the catalyst granules that partial size is different in the adjacent reaction interval of same reaction zone.
Fixed bed reactors left and right ends are respectively inlet port and outlet port, and feed distributor is arranged.
As shown in Fig. 2, catalyst reaction bed is cuboid, length, width and height are respectively 40cm, 7cm and 7cm；Catalyst reaction
Bed uses double-layer structure, and every layer height is selected according to reactant.
As shown in figure 3, solid catalyst particle different by two kinds of partial sizes in the adjacent reaction interval of same reaction zone
(partial size is respectively 0.4~0.6mm and 1.25~1.75mm) subregion is alternately filled, and is divided when filling using interval partition
Area is again removed interval partition after the completion of to be filled, each slanted bar partition length s=3cm, phase with forming intersection fish bone structure
The angle of staggered two reacting spaces is 45 ° in adjacent reaction zone.
Solid catalyst particle in different reclamation districts fully relies on gravity and uniformly fills, in each reacting space
Porosity, the coefficient of conductivity are all the same, and the coefficient of conductivity of adjacent two reacting space is different, but porosity is identical, size 0.4.
The double-deck reaction process for intersecting fish bone structure is illustrated using numerical simulation for the ease of observation present case, is
The advantages of more preferable performance intersects fish bone structure fixed bed reactors, select fixed bed reactors (the solid-filling layer uniformly filled
Partial size is 0.4-0.6mm, remaining parameter is identical as embodiment) as a comparison case.
In simulation, the flow of inlet reactant A and reactant B is 2.84m3/ s, the concentration of injection are 1mol/m3,
And reaction A+B → C is transient response.The diffusion coefficient of reactant is 10-9m2/ s, dispersion coefficient is using Chiogna et al.
2010 in Evidence of Compound-Dependent Hydrodynamic and Mechanical Transverse
The formula derived in Dispersion by Multitracer Laboratory Experiments paper:
Dt=Dp+vd/(Pe+123)0.5
Thus it obtains uniformly filling the yield with the product on the double-deck intersection fish-bone knot fixed bed reactors different location,
It can be found that in exit, when fixed bed reactors are using the catalyst reaction bed uniformly filled, product is 0.78 ×
10-8Mol, but when catalyst reaction bed is using the double-deck intersection fish bone structure, product is 3.1 × 10-8Mol, yield are about
4 times of uniform filled layer.It is possible thereby to illustrate, bilayer intersects fish bone structure porous particle packed bed and greatly accelerates reaction product
Formation efficiency.
The product Yield comparison table of different schemes
For the formation efficiency that reaction product is explained further, the reaction process of embodiment and comparative example is simulated, it is made
Streamline and hydraulic head surfaces are waited, see Fig. 5 and Fig. 6, it can be found that intersecting the streamlines of fish bone structure fixed bed reactors twist, therefore
The mixing between reactive material is increased, thus the significant increase formation efficiency of reaction product.
As known by the technical knowledge, the present invention can pass through the embodiment party of other essence without departing from its spirit or essential feature
Case is realized.Therefore, embodiment disclosed above, in all respects are merely illustrative, not the only.Institute
Have within the scope of the present invention or is included in the invention in the change being equal in the scope of the present invention.
Claims (8)
1. a kind of fixed bed reactors, which is characterized in that including catalyst reaction bed, the catalyst reaction bed includes at least two
Layer reaction zone；Each reaction zone is equipped with multiple reacting spaces；The reacting space of reaction zone described in adjacent two layers is staggered；
Filled with the catalyst granules that partial size is different in the adjacent reaction interval of same reaction zone.
2. fixed bed reactors according to claim 1, which is characterized in that further include hollow housing, the shell it is interior
Chamber is adapted with the shape of catalyst reaction bed, on the shell corresponding to catalyst reaction bed one end offer feed inlet,
The other end corresponding to catalyst reaction bed offers discharge port.
3. fixed bed reactors according to claim 2, which is characterized in that be additionally provided with distribution at the feed inlet of the shell
Device.
4. fixed bed reactors according to claim 1, which is characterized in that staggered two reactions in adjacent reaction area
Interval is obliquely installed in opposite direction.
5. fixed bed reactors according to claim 4, which is characterized in that staggered two reactions in adjacent reaction area
The angle at interval is 0-180 degree.
6. fixed bed reactors according to claim 1, which is characterized in that the catalyst granules include: partial size be 1 ~
The coarse grain diameter catalyst granules and partial size of 2mm is the fine grain catalyst granules of 0.25 ~ 0.75mm.
7. fixed bed reactors according to claim 1, which is characterized in that the axial length of each reacting space is anti-
0.25%-25% times for answering device total length, and axial length > 2cm.
8. fixed bed reactors according to claim 1, which is characterized in that porosity, conduction in same reaction interval
Coefficient is all the same, and the coefficient of conductivity of adjacent two reacting space is different, but porosity is identical.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910221899.2A CN109876739B (en) | 2019-03-22 | 2019-03-22 | Fixed bed reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910221899.2A CN109876739B (en) | 2019-03-22 | 2019-03-22 | Fixed bed reactor |
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| CN109876739A true CN109876739A (en) | 2019-06-14 |
| CN109876739B CN109876739B (en) | 2021-06-08 |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19936675A1 (en) * | 1999-08-04 | 2001-07-05 | Borsig Energy Gmbh | Continually-operated gas reactor has bulk solid packing promoting exothermic treatment in regenerative reverse-flow process |
| AU2003293840A1 (en) * | 2002-12-12 | 2004-06-30 | Basf Aktiengesellschaft | Method for the production of chlorine by means of gas phase oxidation of hydrogen chloride |
| CN102225322A (en) * | 2011-04-12 | 2011-10-26 | 纪群 | Reactor with interval filling bed |
| CN104926586A (en) * | 2015-05-11 | 2015-09-23 | 浙江大学 | Multilayer fixed bed reaction process for producing propylene by taking oxygen-containing compounds as raw material |
| CN107281981A (en) * | 2017-06-26 | 2017-10-24 | 清华大学 | A kind of inner member, fluidized-bed reactor and application process |
| CN208098030U (en) * | 2018-03-06 | 2018-11-16 | 兰州兰石集团有限公司 | Plate and frame fixed bed Fischer-Tropsch synthesis device |
-
2019
- 2019-03-22 CN CN201910221899.2A patent/CN109876739B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19936675A1 (en) * | 1999-08-04 | 2001-07-05 | Borsig Energy Gmbh | Continually-operated gas reactor has bulk solid packing promoting exothermic treatment in regenerative reverse-flow process |
| AU2003293840A1 (en) * | 2002-12-12 | 2004-06-30 | Basf Aktiengesellschaft | Method for the production of chlorine by means of gas phase oxidation of hydrogen chloride |
| CN102225322A (en) * | 2011-04-12 | 2011-10-26 | 纪群 | Reactor with interval filling bed |
| CN104926586A (en) * | 2015-05-11 | 2015-09-23 | 浙江大学 | Multilayer fixed bed reaction process for producing propylene by taking oxygen-containing compounds as raw material |
| CN107281981A (en) * | 2017-06-26 | 2017-10-24 | 清华大学 | A kind of inner member, fluidized-bed reactor and application process |
| CN208098030U (en) * | 2018-03-06 | 2018-11-16 | 兰州兰石集团有限公司 | Plate and frame fixed bed Fischer-Tropsch synthesis device |
Non-Patent Citations (1)
| Title |
|---|
| 叶正才: "固定床加氢反应器内件的结构及应用", 《化学工程与装备》 * |
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