CN201603549U - Reactors for exothermic reactions in the gas phase - Google Patents
Reactors for exothermic reactions in the gas phase Download PDFInfo
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- CN201603549U CN201603549U CN2010201073115U CN201020107311U CN201603549U CN 201603549 U CN201603549 U CN 201603549U CN 2010201073115 U CN2010201073115 U CN 2010201073115U CN 201020107311 U CN201020107311 U CN 201020107311U CN 201603549 U CN201603549 U CN 201603549U
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- reactive moieties
- reactor
- air cooling
- water
- cooled
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 51
- 230000035939 shock Effects 0.000 claims abstract description 5
- 239000003054 catalyst Substances 0.000 claims description 49
- 238000001816 cooling Methods 0.000 claims description 35
- 239000000919 ceramic Substances 0.000 claims description 6
- 239000000498 cooling water Substances 0.000 claims description 6
- 238000010791 quenching Methods 0.000 claims description 6
- 230000002706 hydrostatic effect Effects 0.000 claims description 5
- 239000000376 reactant Substances 0.000 claims description 5
- 238000005259 measurement Methods 0.000 claims description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract description 26
- 230000015572 biosynthetic process Effects 0.000 abstract description 15
- 238000003786 synthesis reaction Methods 0.000 abstract description 15
- 239000010410 layer Substances 0.000 abstract 1
- 239000002356 single layer Substances 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 63
- 229910002091 carbon monoxide Inorganic materials 0.000 description 12
- 238000002360 preparation method Methods 0.000 description 11
- 239000000047 product Substances 0.000 description 6
- 239000002994 raw material Substances 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 4
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 3
- 238000009413 insulation Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 239000012495 reaction gas Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000000470 constituent Substances 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical group O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
本实用新型涉及一种适用于气相放热反应的反应器。所述的反应器由水冷反应部分、气冷反应部分和气冷激部分组成，水冷反应部分经气冷激部分与气冷反应部分连通，且水冷反应部分、气冷反应部分和气冷激部分集成于一圆柱形密闭容器中。本实用新型所设计的适用于气相放热反应(特别适用于由合成气制备甲烷)的反应器的最大优点在于，其床层温度序列合理，单层转化率得到提高，可用一个反应器替代现有的多个合成反应器，降低了装置投资费用。
The utility model relates to a reactor suitable for gas phase exothermic reaction. The reactor is composed of a water-cooled reaction part, an air-cooled reaction part and an air-cooled shock part. in a cylindrical airtight container. The biggest advantage of the reactor suitable for gas phase exothermic reaction (especially suitable for preparing methane from synthesis gas) designed by the utility model is that the temperature sequence of the bed layer is reasonable, the single-layer conversion rate is improved, and one reactor can replace the existing one. There are multiple synthesis reactors, which reduces the investment cost of the device.
Description
Technical field
The utility model relates to a kind of reactor that is applicable to the gas phase exothermic reaction, particularly a kind of reactor that is applicable to by synthesis gas preparation methane.
Background technology
By synthesis gas preparation methane is a kind of strong exothermal reaction, and its reactional equation is as follows:
The characteristics of this reaction are: reversible, heat release, volume-diminished.Catalyst is generally 250 ℃～650 ℃ of nickel catalysts, reaction pressure 3MPa～7MPa, reaction temperature, and reaction speed is fast.
At present, the reactor that is used for synthesis gas preparation methane mostly is fixed bed adiabatic reactor.The defective of its existence is: (1) needs a plurality of fixed bed adiabatic reactor series connection are used for improving the conversion ratio of carbon monoxide.In other words, the conversion ratio of the carbon monoxide of single fixed bed adiabatic reactor is not high.(2) higher because of reaction temperature, for preventing the outer cylinder body overtemperature of used fixed bed adiabatic reactor, (thickness is about 250mm～300mm) generally to need liner one deck thermal insulation layer within it.Because the existence of thermal insulation layer has reduced the effective volume that catalyst loads.In addition, existing by needing a plurality of fixed bed adiabatic reactor series connection to use in the synthesis gas preparation methane production technology, cause must having in the whole flow process many heat exchangers to remove reaction heat, the process route complexity.
Given this, develop a kind of novel reactor that is applicable to gas phase exothermic reaction (being specially adapted to) and become the utility model technical issues that need to address by synthesis gas preparation methane.
Summary of the invention
The utility model purpose is, a kind of reactor that is applicable to gas phase exothermic reaction (being specially adapted to by synthesis gas preparation methane) is provided, and overcomes problems of the prior art.
The reactor that is applicable to gas phase exothermic reaction (being specially adapted to) described in the utility model by synthesis gas preparation methane, it partly is made up of water-cooled reactive moieties, the gentle cold shock of air cooling reactive moieties, the water-cooled reactive moieties swashs part through air cooling and is communicated with the air cooling reactive moieties, and water-cooled reactive moieties, the gentle cold shock of air cooling reactive moieties are partly integrated in a cylindrical closed vessel;
Mainly be provided with in described water-cooled reactive moieties: product outlet, the entry and exit of at least one pair of cooling water and some tubes that is used for loading catalyst;
Mainly be provided with in described air cooling reactive moieties: (raw material) import of at least one reactant and some tubes that is used for loading catalyst;
Swashing part in described air cooling mainly is provided with: at least one quench gas inlet and at least one gas mixer.
In optimized technical scheme of the utility model, the total measurement (volume) of the tube that is used for loading catalyst of air cooling reactive moieties is 1 with the ratio of the total measurement (volume) of the tube that is used for loading catalyst of water-cooled reactive moieties: (1～5).
The great advantage of the reactor that is applicable to gas phase exothermic reaction (being specially adapted to by synthesis gas preparation methane) that the utility model is designed is, its bed temperature sequence is reasonable, the individual layer conversion ratio is improved, an available reactor substitutes existing a plurality of synthesis reactor, has reduced the plant investment expense.
Description of drawings
Fig. 1. be the structural representation that is applicable to the reactor of gas phase exothermic reaction described in the utility model;
Wherein: the outlet of 1-product, 2-cooling water inlet, 3-cylindrical shell, 4-catalyst filling pipe (water-cooled reactive moieties), the 5-coolant outlet, 6-gas mixer, 7-quench gas inlet, 8-reactant (raw material) inlet, 9-catalyst filling pipe (air cooling reactive moieties), 10-upper perforated plate, 11-lower perforated plate, the 12-inert ceramic balls, the 13-catalyst supports;
Spiral aperture on the 601-gas mixer 6, the aperture on the 1001-upper perforated plate 10.
Fig. 2. be the profile of A-A face among Fig. 1.
Fig. 3. be the vertical view of gas mixer among Fig. 16.
Fig. 4. be the vertical view of upper perforated plate among Fig. 1 10.
Fig. 5. gas mixer 6 profiles
The specific embodiment
In conjunction with the accompanying drawings, the reactor of gas phase exothermic reaction that is applicable to described in the utility model is described further.
By Fig. 1. as can be known: reactor described in the utility model is an airtight hydrostatic column, is provided with product outlet 1 at an end end face of described hydrostatic column;
Export 1 end at nearly product, be the water-cooled reactive moieties, the outlet 5 of a pair of cooling water is set at least at the lateral surface of water-cooled reactive moieties, with inlet 2, mainly be provided with several catalyst filling pipes 4 in water-cooled reactive moieties inside, two ends at catalyst filling pipe 4 (or deserve to be called, the lower end) is respectively equipped with upper perforated plate 10 and lower perforated plate 11, said upper perforated plate 10 and lower perforated plate 11 are provided with several circular holes 1001 (referring to Fig. 4, the vertical view of lower perforated plate 11 is identical with Fig. 4, the Therefore, omited), the number of circular hole 1001 is identical with the number of catalyst filling pipe 4, and the area of circular hole 1001 equates with the sectional area of catalyst filling pipe 4, is provided with inert ceramic balls 12 and catalyst and supports 13 below lower perforated plate 11;
The other end in product outlet 1, be the air cooling reactive moieties, lateral surface in the air cooling reactive moieties is provided with a reactant (raw material) inlet 8 at least, mainly be provided with several catalyst filling pipes 9 in air cooling reactive moieties inside, be provided with inert ceramic balls 12 (being used for the catalyst in the support catalyst filling pipe 9) at catalyst filling pipe 9 nearly water-cooled reactive moieties one ends;
Connect water-cooled reactive moieties and air cooling reactive moieties (promptly in the middle of water-cooled reactive moieties and air cooling reactive moieties), for air cooling swashs part, the lateral surface that swashs part in air cooling is provided with a quench gas inlet 7 at least, and the inside of swashing part in air cooling mainly is provided with gas mixer 6;
Said gas mixer 6 is for being provided with the sieve plate (referring to Fig. 3 and Fig. 5) of some spiral apertures 601.
In addition, the diameter of whole reactor is preferably 2 meters～6 meters, in the air cooling reactive moieties, the radical of catalyst filling pipe 9 is fixed according to production scale, is generally 300～7,000, the internal diameter (diameter) of single catalyst filling pipe 9 is 22mm～58mm, highly is 4m～10m;
Equally, in the water-cooled reactive moieties, the radical of catalyst filling pipe 4 is fixed according to production scale, is generally 300～7,000, and single catalyst filling pipe 4 internal diameters (diameter) are 22mm～58mm, height 4m～10m.
Gas mixer 6 used sieve plates are provided with 2,000～6,000 spiral aperture that diameter is 2mm～5mm.
Below being example, the use of reactor described in the utility model is described further by synthesis gas preparation methane.
At first, in described catalyst filling pipe 4 and 9, be filled with the existing loaded catalyst that is used for synthesis gas preparation methane, its active constituent is a metallic nickel, and carrier is aluminium oxide (Al
2O
3).
Then, when " driving ", with 3MPa～8MPa unstripped gas (CO+H
2) enter in the air cooling reactive moieties of described reactor by reactant (raw material) inlet 8 by external electric heater preheating material gas to 200 ℃～230 ℃, top by catalyst filling pipe 9 enters catalyst filling pipe 9 internal reactions, reaction back gas temperature is 400 ℃～450 ℃, when reaching stable operation, stop heating raw gas.Follow-up unstripped gas [(CO+H
2) its temperature is 20 ℃～40 ℃] and with catalyst filling pipe 9 in gas converting heats, make its temperature rise to 230 ℃～250 ℃.
Deriving gas by catalyst filling pipe 9 is that 20 ℃～40 ℃ unstripped gas (being entered by quench gas inlet 7) mix through gas mixer 6 with another burst temperature, temperature is 220 ℃～250 ℃ a mist, this mist is in upper perforated plate 10 enters catalyst filling pipe 4, temperature is controlled at 220 ℃～280 ℃ in the temperature of catalyst filling pipe 4, reaction heat in the catalyst filling pipe 4 is removed by the cooling water of its outside, generate gaseous product through lower perforated plate 11 and inert ceramic balls 12 etc. in the catalyst filling pipe 4, derive by product outlet 1.
This reactor is owing to adopted the mode of air cooling-cold shock-water-cooled, make the temperature sequence of whole reactor bed reasonable, the individual layer conversion ratio is improved, and Catalyst Production intensity also is improved, an available reactor substitutes existing a plurality of synthesis reactor, has reduced the plant investment expense.
As for for synthesis gas preparation methane case, on the top of reactor (air cooling reactive moieties), reaction temperature is 240 ℃～450 ℃, and in the bottom of reactor (water-cooled reactive moieties), reaction temperature is 220 ℃～280 ℃.Because the methane synthetic reaction is exothermic reaction, on the top of reactor, away from chemical balance, reaction is violent, the reaction temperature height, preheating unstripped gas, again because unstripped gas at shell, the unstripped gas temperature can not surpass 250 ℃, and heat-insulation layer can be set, and increases the space reactor utilization rate; In the bottom of reactor, reaction temperature is low, and favourable to the chemical balance of reaction, reaction heat is removed by managing outer water, byproduct steam, and heat can access reasonable utilization.
The utility model is described in further detail below by embodiment, and its purpose only is better to understand content of the present utility model and unrestricted protection domain of the present utility model.In the following embodiments, except that specifying, described percentage is percent by volume.
Embodiment 1
Unstripped gas is formed: CO:17.82%, CO
2: N 1.62%,
2+ Ar 0.54%, H
2: CH 61.01%,
4: 19.01%, add up to 100.00,32 ℃ of unstripped gas temperature, reaction pressure 5.0MPa, enter in air cooling-cold shock-water cooled reactor, gas converting heat in unstripped gas and the reaction tube, temperature is raised to 230 ℃, and in the air cooling section, unstripped gas is at reaction tube 9 internal reactions, temperature is elevated to 400 ℃ from 230 ℃, at cold shocking section, reaction temperature is that 400 ℃ reaction gas and temperature is that 32 ℃ unstripped gas mixes, and mixed gas temperature is 240 ℃, enter the reaction of water-cooled section, the temperature of reacting gas is elevated to 275 ℃ from 240 ℃.CO and CO in the raw material
2Total conversion be 99.7%,
Exit gas consists of: CO 0.09%, CO
20.01%, N
2+ Ar 0.89%, H
20.41%, CH
463.43%, H
2O35.17%;
The exit gas butt is formed: CO 0.14%, CO
20.01%, N
2+ Ar 1.37%, H
20.64%, CH
497.84%.
Embodiment 2
Unstripped gas is formed: CO 17.82%, CO
21.62%, N
2+ Ar 0.54%, H
261.01%, CH
419.01%, add up to 100.00,32 ℃ of unstripped gas temperature, reaction pressure 8.0MPa, enter in air cooling-cold shock-water cooled reactor, gas converting heat in unstripped gas and the reaction tube, temperature is raised to 230 ℃, and in the air cooling section, unstripped gas is at reaction tube 9 internal reactions, temperature is elevated to 420 ℃ from 230 ℃, at cold shocking section, reaction temperature is that 400 ℃ reaction gas and temperature is that 32 ℃ unstripped gas mixes, and mixed gas temperature is 250 ℃, enter the reaction of water-cooled section, the temperature of reacting gas is elevated to 280 ℃ from 250 ℃.CO and CO in the raw material
2Total conversion be 99.9%,
Exit gas consists of: CO 0.03%, CO
20.00%, N
2+ Ar 0.89%, H
20.22%, CH
463.58%, H
2O35.28%;
The exit gas butt is formed: CO 0.05%, CO
20.00%, N
2+ Ar 1.37%, H
20.33%, CH
498.24%.
Claims (9)
1. reactor that is applicable to the gas phase exothermic reaction, it is characterized in that, described reactor partly is made up of water-cooled reactive moieties, the gentle cold shock of air cooling reactive moieties, the water-cooled reactive moieties swashs part through air cooling and is communicated with the air cooling reactive moieties, and water-cooled reactive moieties, the gentle cold shock of air cooling reactive moieties are partly integrated in a cylindrical closed vessel;
Mainly be provided with in described water-cooled reactive moieties: product outlet, the entry and exit of at least one pair of cooling water and some tubes that is used for loading catalyst;
Mainly be provided with in described air cooling reactive moieties: at least one reaction-ure inlet and some tubes that is used for loading catalyst;
Swashing part in described air cooling mainly is provided with: at least one quench gas inlet and at least one gas mixer.
2. reactor as claimed in claim 1 is characterized in that, the total measurement (volume) of the tube that is used for loading catalyst of air cooling reactive moieties is 1 with the ratio of the total measurement (volume) of the tube that is used for loading catalyst of water-cooled reactive moieties: (1～5).
3. reactor as claimed in claim 1 or 2 is characterized in that, described reactor is an airtight hydrostatic column, is provided with product outlet (1) at an end end face of described hydrostatic column;
At nearly product outlet (1) end, be the water-cooled reactive moieties, the outlet (5) of a pair of cooling water is set at least at the lateral surface of water-cooled reactive moieties, and inlet (2), mainly be provided with several catalyst filling pipes (4) in water-cooled reactive moieties inside, upper end and lower end at catalyst filling pipe (4) are respectively equipped with upper perforated plate (10) and lower perforated plate (11), said upper perforated plate (10) and lower perforated plate (11) are provided with several circular holes, the number of described circular hole is identical with the number of catalyst filling pipe (4), and the area of circular hole equates with the sectional area of catalyst filling pipe (4), is provided with inert ceramic balls (12) and catalyst in the below of lower perforated plate (11) and supports (13);
The other end in product outlet 1, be the air cooling reactive moieties, lateral surface in the air cooling reactive moieties is provided with a reactant entrance (8) at least, mainly be provided with several catalyst filling pipes (9) in air cooling reactive moieties inside, be provided with inert ceramic balls 12 at nearly water-cooled reactive moieties one end of catalyst filling pipe (9);
Connecting water-cooled reactive moieties and air cooling reactive moieties is that air cooling swashs part, and the lateral surface that swashs part in air cooling is provided with a quench gas inlet (7) at least, and the inside of swashing part in air cooling mainly is provided with gas mixer (6);
Described gas mixer (6) is for being provided with the sieve plate of some spiral apertures (601).
4. reactor as claimed in claim 3 is characterized in that, the diameter of wherein said hydrostatic column is 2 meters～6 meters.
5. reactor as claimed in claim 3 is characterized in that, wherein the quantity of catalyst filling pipe (9) is 300～7,000.
6. reactor as claimed in claim 5 is characterized in that, wherein single catalyst filling pipe (9) internal diameter is 22 millimeters～58 millimeters, highly is 4 meters～10 meters.
7. reactor as claimed in claim 3 is characterized in that, wherein the quantity of catalyst filling pipe (4) is 300～7,000.
8. reactor as claimed in claim 7 is characterized in that, wherein single catalyst filling pipe (4) internal diameter is 22 millimeters～58 millimeters, highly is 4 meters～10 meters.
9. reactor as claimed in claim 3 is characterized in that, wherein said gas mixer (6) is for being provided with 2,000～6,000, and diameter is the sieve plate of the spiral aperture (601) of 2mm～5mm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010201073115U CN201603549U (en) | 2010-01-21 | 2010-01-21 | Reactors for exothermic reactions in the gas phase |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010201073115U CN201603549U (en) | 2010-01-21 | 2010-01-21 | Reactors for exothermic reactions in the gas phase |
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| Publication Number | Publication Date |
|---|---|
| CN201603549U true CN201603549U (en) | 2010-10-13 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102133512A (en) * | 2010-01-21 | 2011-07-27 | 华东理工大学 | Reactor applied to gas-phase exothermic reaction |
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2010
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102133512A (en) * | 2010-01-21 | 2011-07-27 | 华东理工大学 | Reactor applied to gas-phase exothermic reaction |
| CN102133512B (en) * | 2010-01-21 | 2013-05-15 | 华东理工大学 | Reactors for exothermic reactions in the gas phase |
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|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20101013 Termination date: 20140121 |