CN101804314A - Fluidized bed reactor - Google Patents
Fluidized bed reactor Download PDFInfo
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- CN101804314A CN101804314A CN201010170003A CN201010170003A CN101804314A CN 101804314 A CN101804314 A CN 101804314A CN 201010170003 A CN201010170003 A CN 201010170003A CN 201010170003 A CN201010170003 A CN 201010170003A CN 101804314 A CN101804314 A CN 101804314A
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Abstract
The invention provides a fluidized bed reactor. A fine particle catalyst makes a suspension motion under the effect of the ascending reaction gas air steam, the solid particles flip up and down dramatically to fully mixing the reaction gas air together with the particles in a bed layer and avoid the 'hot spot' in a stationary bed reactor, the temperature distribution inside the bed layer is uniform, a laminar boundary layer nearby a heat transfer surface is damaged to improve the heat transfer coefficient, large amount of heat generated by catalytic reactions such as methane synthesis is removed through a raw gas in a heat exchange tube so as to reduce the temperature of a catalyst bed layer, make the temperature distribution of the bed layer more uniform, improve the conversion rate of the raw gas, and enhance the production capability of the reactor. The reactor has the advantages of reasonable structure, uniform bed layer temperature, reduced bed layer pressure, high efficiency for heat transfer and mass transfer and strong reaction capability.
Description
Technical field
The present invention relates to field of catalytic reactions, particularly a kind of catalytic process reactor.
Background technology
Fluidized-bed reactor is a class reactor of extensive use in chemical process, is particularly suitable for exothermic effect significantly or to the system of temperature control requirement strictness.Reaction such as synthetic as catalytic cracking reaction, ethylene oxychlorination, butylene oxidation-dehydrogenation, acrylonitrile, that methane is synthetic.The key character of fluidized-bed reactor is that fine grain catalyst is made suspended motion under the ascending air effect, and solid particle acutely stirs up and down.This forms of motion makes the bed inner fluid fully stir with particle to mix, avoided " focus " phenomenon in the fixed bed reactors, uniformity of temperature profile in the bed, whole reaction system is in isothermal environment, and destroyed near the laminar boundary layer the heat-transfer area, heat transfer system between bed and the heat-transfer surface is all more much higher than blank pipe and fixed bed, thus better than the heat exchange effect of fixed bed, thus make reactor satisfy heat endurance.
The methane synthetic reaction is at high temperature and CO, CO in the gas is arranged under the situation of catalyst existence
2And H
2React, generate CH
4And H
2O.The methane synthetic reaction is a strong exothermal reaction, and the exothermic heat of reaction amount is big, and the operating temperature of methane synthetic reaction is higher relatively simultaneously, must in time take reaction heat away in reactor, and the control reaction temperature could guarantee the normal operation of reactor.Shift out a large amount of reaction heat effectively, make the reactor stable operation, prolong catalyst service life, the structural shape of reactor becomes one of core technology of methanation process.
Methane synthesis reactor mainly adopts fixed bed reactors at present, comprises heat-insulating fixed bed reactors and heat exchange type fixed bed reactors.Heat-insulating fixed bed reactors (US4,064,256, US4,298,694 and US4,130,573) catalyst layer does not have heat transmission equipment, utilize a large amount of loop control reaction bed temperatures of product gas, relatively simple for structure, the space availability ratio height, cost is low, but if reaction heat can't in time shift out, for the heat release reversible reaction, because temperature rise is excessive, the axial temperature of reactor distributes can be away from optimum temperature profile, thereby cause the production capacity of reactor to reduce, even can make reactor outlet not reach desired conversion ratio owing to the restriction of chemical balance, and cause burden can for the selection and the cost of equipment, even reduce the reactor operating temperature, excessive product gas internal circulating load will directly increase reaction gas linear velocity and catalyst bed layer height, causes the increase of the excessive and outer loop compressor horsepower of reactor pressure decrease.Heat exchange type fixed bed reactors (ZL00208802.9 and CN87102871) adopt the pipe apparatus with catalyst inside, and pipe is outer to be heat transfer medium, and the advantage that this reactor has is that bed has a narrow range of temperature, stable operation, easy to adjust, but the catalyst packing factor is little, and the gas flow resistance is bigger.
Summary of the invention
Technical problem to be solved by this invention be propose at above-mentioned prior art present situation a kind of have rational in infrastructure, bed temperature equilibrium, the fluidized-bed reactor that bed pressure drop is low and production capacity is high.
The technical scheme that technical problem to be solved by this invention adopts is:
This fluidized-bed reactor, comprise at the bottom of the awl of reactor upper end enlarged tube 1, reactor middle part straight tube 2, reactor lower part 3, on the cyclone separator 4, internals 5, heat-exchanger rig 6, case top product gas outlet 7, enlarged tube in catalyst filler 8, the heat exchanger in heat transfer medium outlet 9, gas distributor 10, the heat exchanger heat transfer medium inlet 11 and unstripped gas go into pipe 12 and reactor straight tube lower catalytic agent outlet 13.
The diameter of described reactor upper end enlarged tube 1 is 1.5/1 ~ 5/1 with the diameter ratio of middle part straight tube 2, and the aspect ratio of the height of upper end enlarged tube 1 and middle part straight tube 2 is 1/3 ~ 1/20.
3 is the pre-distributor of unstripped gas at the bottom of the awl of described reactor lower part, adopts the inverted cone of bottom surface radius r than high h=1/0.5 ~ 1/2.
Described cyclone separator 4 adopts the series connection of single cyclone separator or a plurality of cyclone separator.
Described internals 5 is positioned at reactor straight tube conversion zone, adopt baffle plate or backstop, the material of baffle plate or backstop adopts the high strength carbon steel usually, adopting the purpose of baffle plate or backstop is the air pocket that broken gas produces in bed, improve the gas-solid contact, reduce back-mixing, thereby increase reaction rate and improve conversion ratio.
Described heat-exchanger rig 6 is positioned at the conversion zone (emulsion zone) of reactor straight tube, adopts plate type heat exchanger, U pipe heat exchanger, coil heat exchanger or tubular heat exchanger usually; Cooling medium shifts out the catalytic reaction liberated heat rapidly in the heat exchanger, and reaction temperature is maintained about optimal reaction temperature, and heat exchanger can be one or more levels.Wherein plate type heat exchanger and tubular heat exchanger adopt the staggered form multi-stage heat exchanger usually, and the plate type heat exchanger of staggered form multi-stage heat exchanger and tubular heat exchanger have the baffle plate function simultaneously.
Described catalyst filler 8 and outlet 13 can make things convenient for the loading and unloading of catalyst.
Described unstripped gas is gone into pipe 12 and is positioned at the reactor awl at the end, adopts open type or bent-tube boiler.
Fluidized-bed reactor of the present invention is rational in infrastructure, bed temperature is balanced, bed pressure drop is low, mass-and heat-transfer efficient height, respond are big, of many uses, is particularly suitable for the methane synthetic reaction.
The operating condition that fluidized-bed reactor of the present invention is used for the methane synthetic reaction is: the catalyst granules particle diameter is 50 ~ 200 μ m, and catalyst concn is for accounting for 10 ~ 60wt% of material (gas and catalyst) total amount; Entering the gas reactor volume flow is 0.2 ~ 1.0m/s with reactor straight length cross-sectional area than (being linear gas velocity), 260 ~ 370 ℃ of temperature, pressure 1.0 ~ 6.0MPa.
The methane synthetic catalyst is Ni-based methane synthetic catalyst, with the Al of high-wearing feature
2O
3Be carrier, adopt step impregnation method successively magnesium nitrate, lanthanum nitrate, cerous nitrate and nickel nitrate to be loaded on the carrier of moulding in advance, drying is 12 hours in 120 ℃ air atmosphere; Sample after the drying 600 ℃ of calcinings 4 hours, is prepared into loading type nickel-based catalyst, and Raney nickel consists of NiO ﹕ 10%～30wt%; MgO ﹕ 1～4wt%; La
2O
3﹕ 0.5～2wt%; CeO
2﹕ 0.5～2wt% satisfies the requirement of active and selectivity, high abrasion resistance in the cycle of long-term operation continuously, and has good CO and CO
2Methane synthesizes performance.
The invention has the advantages that:
The heat exchange type fluidized-bed reactor is applied to the catalytic reaction process of strong heat release, finely grained catalyst is made suspended motion in the fluidized-bed reactor under the ascending air effect, solid particle acutely stirs up and down, can avoid " focus " phenomenon in the fixed bed reactors, can make uniformity of temperature profile in the system rapidly, whole reaction system is in isothermal environment, and solid particle strenuous exercise, destroyed near the laminar boundary layer of heat-transfer area, improve its heat transfer coefficient greatly, the big calorimetric that violent catalytic reaction is emitted is removed by heat transfer medium in the heat-exchanger rig rapidly, thereby can reduce reaction bed temperature, methane synthetic reaction that makes strong heat release etc. is fully carried out in the optimum temperature range of catalyst.
Compare with fixed bed, the operating gas velocity of fluid bed is much higher relatively, operates under higher air speed, under the equipment size situation identical with fixed bed, realizes being higher than the output of fixed bed several times.
The disposal ability of fixed bed reactors is subjected to the restriction of unstripped gas gas speed, gas speed is big more, the resistance of system (being pressure drop) is big more, activity of such catalysts can not be given full play to, and be steady state value in the fluidized bed reaction system pressure drop, if unstripped gas gas speed can improve in the activity of such catalysts allowed band at loaded catalyst one regularly.
So, to compare with fixed bed reactors, fluidized-bed reactor can obviously improve reactor production capacity; The axial temperature that can improve fixed bed reactors distributes, and makes it near the catalytic reaction optimum temperature, improves the catalytic reaction conversion ratio, increases reactor production capacity; Good reactor heat-exchanger rig is controlled in the optimum temperature reactor operation temperature, and handling safety is ensured, and can produce high steam or middle pressure steam.
?
Description of drawings
Fig. 1 is the vertical sectional structure chart of the present invention.
Fig. 2 is the vertical sectional structure chart of fluidized-bed reactor of three layers of heat exchanger of band of the present invention.
Fig. 3 is the vertical sectional structure chart of fluidized-bed reactor of band U type heat exchanger of the present invention.
Fig. 4-a is the vertical sectional structure chart of fluidized-bed reactor of band tubular heat exchanger of the present invention.
Fig. 4-b is the vertical view of the fluidized-bed reactor straight tube of band tubular heat exchanger of the present invention.
Fig. 5 is the vertical sectional structure chart of fluidized-bed reactor of band three stratose heats exchange of heat pipe of the present invention.
Fig. 6-a is the vertical sectional structure chart of fluidized-bed reactor of band plate formula heat exchanger of the present invention.
Fig. 6-b is the vertical view of the fluidized-bed reactor straight tube of band plate formula heat exchanger of the present invention.
Fig. 7 is the vertical sectional structure chart of fluidized-bed reactor of band three ply board formula heat exchanger of the present invention.
Among the figure, the 1-enlarged tube; The 2-straight tube; 3-bores the end; The 4-cyclone separator; The 5-internals; The 6-heat-exchanger rig; The 7-product gas outlet; 8-catalyst filler; The 9-heat transfer medium outlet; The 10-gas distributor; The 11-heat transfer medium inlet; The 12-unstripped gas is gone into pipe; 13-catalyst outlet.
Wherein, Fig. 1 is a Figure of abstract.
The specific embodiment
To the detailed description of the invention, below only is preferred embodiment of the present invention below in conjunction with accompanying drawing, can not limit scope of the present invention with this.Promptly the equalization of being done according to the present patent application claim generally changes and modifies, and all should still belong in the scope that patent of the present invention contains.
Below in conjunction with accompanying drawing the present invention is further described.
As shown in Figure 1, the present invention includes: at the bottom of the awl of reactor upper end enlarged tube 1, reactor middle part straight tube 2, reactor lower part 3, on the cyclone separator 4, internals 5, heat-exchanger rig 6, case top product gas outlet 7, enlarged tube in catalyst filler 8, the heat exchanger in the gas distributor 10 between heat transfer medium outlet 9, the awl end and straight tube, the heat exchanger heat transfer medium inlet 11 and awl at the end unstripped gas go into pipe 12 and reactor straight tube lower catalytic agent outlet 13.
The structure and the progression of the thermic load decision reactor heat-exchanger rig 6 in the reactor.Three layers of heat exchanger are set in the reactor shown in Figure 2, improve heat exchange efficiency, reduce the temperature of reaction bed.As shown in Figure 3, heat exchanger is double-deck U type heat exchanger.
In Fig. 1, the methane synthetic raw gas is gone into pipe 12 by reactor awl end raw material and is entered the awl end, 3 advanced promoting the circulation of qi bodies distribute in advance at the bottom of the awl of reactor lower part, distribute by 10 pairs of gases of gas distributor then, the designed gas distribution grid form and the size shape of pore guarantee that gas can evenly enter in the straight tube of fluid bed middle part, form good fluidization conditions, concrete principle is in the fluidisation attitude for guaranteeing catalyst granules, and gas speed is between critical fludization velocity and the maximum fluidization velocity.
In the methane synthetic raw gas usually each component volumn concentration be: the content of CO is 12.2%, H
2Content be 45.6%, CH
4Content is 10.2%, CO
2Content is 31.8%, N
2Content 0.2%.
The methane synthetic reaction is a strong exothermal reaction, the exothermic heat of reaction amount is big, the uprising gas that enters reactor middle part straight tube 2 from gas distributor 10 makes the methane synthetic catalyst of fine particle make suspended motion, solid particle acutely stirs up and down, can make uniformity of temperature profile in the system rapidly, whole reaction system is in isothermal environment, and can destroy near the laminar boundary layer of heat-transfer surface, improve the heat transfer coefficient between bed and heat-transfer surface greatly, heat can be removed by heat transfer medium in the heat-exchanger rig 6 rapidly in the reactor, thereby can reduce reaction bed temperature, the methane synthetic reaction of strong heat release is fully carried out in the optimum temperature range (280 ~ 330 ℃) of catalyst, and then the conversion ratio of raising unstripped gas, increase the production capacity of reactor, and can produce high steam or middle pressure steam.
The air pocket that the internals backstop 5 of reactor straight tube conversion zone can spallation reaction gas gas produces in bed improves the gas-solid contact, reduces back-mixing, thereby increases reaction rate and improve conversion ratio.
Reaction gas is realized and most of particle separation in reactor upper end enlarged tube 1, and entering cyclone separator 4, further separates the gas that has small quantities of particles, solid particles sediment is in cyclone separator 4 bottoms, reactor straight tube 2 reaction zones that fall back then, product gas exports 7 outflow reactors from reactor head.Catalyst granules adds from filler 8, and outlet 13 shifts out.
The catalyst average grain diameter is 50 μ m in the methane synthetic reaction, and catalyst concn is the 40wt% that accounts for the material total amount, and linear gas velocity is 0.74m/s, 330 ℃ of temperature, pressure 4.0MPa.
Claims (10)
1. fluidized-bed reactor comprises: enlarged tube (1), straight tube (2), the awl end (3), cyclone separator (4), internals (5), heat-exchanger rig (6), product gas outlet (7), catalyst filler (8), heat transfer medium outlet (9), gas distributor (10), heat transfer medium inlet (11), unstripped gas are gone into pipe (12) and catalyst outlet (13).
2. according to the described reactor of claim 1, it is characterized in that: heat-exchanger rig (6) adopts plate type heat exchanger, U pipe heat exchanger, coil heat exchanger or tubular heat exchanger.
3. according to claim 1 or 2 described reactors, it is characterized in that: heat-exchanger rig (6) is one or more levels.
4. according to the described reactor of claim 3, it is characterized in that: adopt the staggered form multi-stage heat exchanger in heat-exchanger rig (6) plate type heat exchanger and the tubular heat exchanger.
5. according to the described reactor of claim 4, it is characterized in that: the plate type heat exchanger and the tubular heat exchanger of heat-exchanger rig (6) staggered form multi-stage heat exchanger have the baffle plate function.
6. according to the described reactor of claim 1, it is characterized in that: gas distributor (10) adopts straight hole sieve-board type gas distribution grid, bubble cap side opening distribution grid or straight hole bubble cap distribution grid.
7. according to the described reactor of claim 1, it is characterized in that: reactor operation pressure drop is 0.005 ~ 0.2MPa.
8. according to the application of described any one fluidized-bed reactor of claim 1～7 in methane is synthetic.
9. described according to Claim 8 application is characterized in that: reaction pressure is 1.0 ~ 6.0MPa.
10. described according to Claim 8 application is characterized in that: methane synthesis reaction catalyst grain diameter is 50 ~ 200 μ m.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010170003A CN101804314A (en) | 2010-05-12 | 2010-05-12 | Fluidized bed reactor |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010170003A CN101804314A (en) | 2010-05-12 | 2010-05-12 | Fluidized bed reactor |
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|---|---|
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Cited By (16)
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|---|---|---|---|---|
| CN102407087A (en) * | 2011-10-25 | 2012-04-11 | 奎屯西龙无纺土工制品有限公司 | Method using multi-tube segmental heat exchange type fluidized bed reactor |
| CN102641696A (en) * | 2012-04-25 | 2012-08-22 | 东营海源化工股份有限公司 | Multilayered fluidized bed for alkylation reaction of phenolic compounds and application of multilayered fluidized bed |
| CN103480306A (en) * | 2013-09-06 | 2014-01-01 | 攀钢集团攀枝花钢铁研究院有限公司 | Low-temperature boiling chlorination furnace and method for producing titanium tetrachloride |
| CN103785334A (en) * | 2012-11-02 | 2014-05-14 | 河北化大科技有限公司 | Large fluidized bed reactor |
| CN105214574A (en) * | 2015-10-12 | 2016-01-06 | 南京佳业检测工程有限公司 | Multifunctional examining measured reaction device |
| CN105214576A (en) * | 2015-10-12 | 2016-01-06 | 南京佳业检测工程有限公司 | Cylinder detection reaction device |
| CN105214573A (en) * | 2015-10-12 | 2016-01-06 | 南京佳业检测工程有限公司 | Novel detection reaction device |
| CN105944631A (en) * | 2016-07-15 | 2016-09-21 | 中国海洋石油总公司 | Fluidized bed synthesis gas methanation device |
| CN106111023A (en) * | 2016-07-15 | 2016-11-16 | 中国海洋石油总公司 | A kind of fluid bed syngas methanation process |
| CN106247323A (en) * | 2016-09-14 | 2016-12-21 | 东南大学 | A kind of chemical chain combustion apparatus based on tower bubbling fluidized bed fuel reactor and method thereof |
| CN107140675A (en) * | 2017-07-06 | 2017-09-08 | 华南理工大学 | A kind of energy-saving copper sludge recycling prepares the device of copper sulphate |
| CN109745925A (en) * | 2019-02-26 | 2019-05-14 | 国家能源投资集团有限责任公司 | The loading method of n-butene direct hydration reactor |
| CN110252213A (en) * | 2019-05-27 | 2019-09-20 | 河北科技大学 | A kind of fluidized bed reaction producing chloromethanes and ammonia |
| CN110252216A (en) * | 2019-04-24 | 2019-09-20 | 中国科学院山西煤炭化学研究所 | A kind of fluidized-bed reactor taking heat for methane conversion and intensification |
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| CN113663606A (en) * | 2021-08-06 | 2021-11-19 | 四川金象赛瑞化工股份有限公司 | Dicyandiamide dimerization reactor and process thereof |
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2010
- 2010-05-12 CN CN201010170003A patent/CN101804314A/en active Pending
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| CN102407087A (en) * | 2011-10-25 | 2012-04-11 | 奎屯西龙无纺土工制品有限公司 | Method using multi-tube segmental heat exchange type fluidized bed reactor |
| CN102407087B (en) * | 2011-10-25 | 2013-09-18 | 奎屯西龙无纺土工制品有限公司 | Method using multi-tube segmental heat exchange type fluidized bed reactor |
| CN102641696A (en) * | 2012-04-25 | 2012-08-22 | 东营海源化工股份有限公司 | Multilayered fluidized bed for alkylation reaction of phenolic compounds and application of multilayered fluidized bed |
| CN102641696B (en) * | 2012-04-25 | 2016-06-15 | 东营海源化工股份有限公司 | A kind of multicompartment fluidized bed for phenolic compound alkylated reaction and application thereof |
| CN103785334A (en) * | 2012-11-02 | 2014-05-14 | 河北化大科技有限公司 | Large fluidized bed reactor |
| CN103480306A (en) * | 2013-09-06 | 2014-01-01 | 攀钢集团攀枝花钢铁研究院有限公司 | Low-temperature boiling chlorination furnace and method for producing titanium tetrachloride |
| CN105214574A (en) * | 2015-10-12 | 2016-01-06 | 南京佳业检测工程有限公司 | Multifunctional examining measured reaction device |
| CN105214576A (en) * | 2015-10-12 | 2016-01-06 | 南京佳业检测工程有限公司 | Cylinder detection reaction device |
| CN105214573A (en) * | 2015-10-12 | 2016-01-06 | 南京佳业检测工程有限公司 | Novel detection reaction device |
| CN106111023A (en) * | 2016-07-15 | 2016-11-16 | 中国海洋石油总公司 | A kind of fluid bed syngas methanation process |
| CN105944631A (en) * | 2016-07-15 | 2016-09-21 | 中国海洋石油总公司 | Fluidized bed synthesis gas methanation device |
| CN106247323A (en) * | 2016-09-14 | 2016-12-21 | 东南大学 | A kind of chemical chain combustion apparatus based on tower bubbling fluidized bed fuel reactor and method thereof |
| CN107140675A (en) * | 2017-07-06 | 2017-09-08 | 华南理工大学 | A kind of energy-saving copper sludge recycling prepares the device of copper sulphate |
| CN107140675B (en) * | 2017-07-06 | 2019-05-14 | 华南理工大学 | A kind of energy-saving copper sludge recycling prepares the device of copper sulphate |
| CN109745925A (en) * | 2019-02-26 | 2019-05-14 | 国家能源投资集团有限责任公司 | The loading method of n-butene direct hydration reactor |
| CN110252216A (en) * | 2019-04-24 | 2019-09-20 | 中国科学院山西煤炭化学研究所 | A kind of fluidized-bed reactor taking heat for methane conversion and intensification |
| CN110252213A (en) * | 2019-05-27 | 2019-09-20 | 河北科技大学 | A kind of fluidized bed reaction producing chloromethanes and ammonia |
| CN110252213B (en) * | 2019-05-27 | 2022-03-22 | 河北科技大学 | Fluidized bed reaction device for producing chloromethane and ammonia |
| WO2021082166A1 (en) * | 2019-10-29 | 2021-05-06 | 山东泽石新材料科技有限公司 | Method and device for preparing transition metal lithium oxide |
| KR20210054486A (en) * | 2019-10-29 | 2021-05-13 | 산동 지스톤 뉴 머티리얼 테크놀로지 컴퍼니 리미티드. | Lithium transition metal oxide manufacturing method and manufacturing apparatus |
| KR102405107B1 (en) * | 2019-10-29 | 2022-06-07 | 산동 지스톤 뉴 머티리얼 테크놀로지 컴퍼니 리미티드. | Manufacturing method and manufacturing apparatus of lithium transition metal oxide |
| US11643338B2 (en) | 2019-10-29 | 2023-05-09 | Shandong Zstone New Material Technology Co., Ltd. | Method and device for producing lithium transition metal oxide |
| CN113663606A (en) * | 2021-08-06 | 2021-11-19 | 四川金象赛瑞化工股份有限公司 | Dicyandiamide dimerization reactor and process thereof |
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Open date: 20100818 |