CN103922403A - Method for producing powdery vanadic anhydride by ammonium polyorthovanadate in fluidization state - Google Patents
Method for producing powdery vanadic anhydride by ammonium polyorthovanadate in fluidization state Download PDFInfo
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- CN103922403A CN103922403A CN201410111170.7A CN201410111170A CN103922403A CN 103922403 A CN103922403 A CN 103922403A CN 201410111170 A CN201410111170 A CN 201410111170A CN 103922403 A CN103922403 A CN 103922403A
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The invention provides a method for producing powdery vanadic anhydride by ammonium polyorthovanadate in a fluidization state. The method comprises the following steps: employing a pre-fluidization system to perform pre-fluidization on an ammonium polyorthovanadate material, introducing the ammonium polyorthovanadate material into a main structure of a fluidized bed in a fluidization state, simultaneously providing compressed air with flow velocity of 120-250Nm<3>/h and pressure of 60-70kPa in the main structure of the fluidized bed from a fluidization gas inlet, controlling the temperature in the main structure of the fluidized bed at 490-560 DEG C through a bar-shaped or plate-shaped member, staying the ammonium polyorthovanadate material for 40-60 minutes in the main structure of the fluidized bed, and obtaining the powdery vanadic anhydride at a coarse grain material outlet and a fine grain material outlet. The method has the advantages of low reaction temperature, energy saving and consumption reduction, the method enables long time and continuous operation; and the V2O5 grade of the products can reach 98 national standard.
Description
Technical field
The present invention relates to fluidization Vanadium Pentoxide in FLAKES production technical field, specifically, relate to a kind of ammonium poly-vanadate fluidization and produce powdery Vanadium Pentoxide in FLAKES (V
2o
5) method.
Background technology
At present, domestic and international suitability for industrialized production powdery V
2o
5method be mainly " two-step approach " of decomposing furnace, electric furnace or rotary kiln." two-step approach " produces powdery V
2o
5, easily there is caking phenomenon in temperature control complexity, and energy consumption is large, and heat utilization efficiency is not high.In addition, " two-step approach " is static decomposition, and decomposition obtains ammonia and hydrogen can be by V
2o
5reduction, thus make V
2o
5appearance color is inhomogeneous.
Summary of the invention
The object of the invention is to solve at least one in prior art above shortcomings.
For example, one of object of the present invention is to provide a kind of and can produces powdery Vanadium Pentoxide in FLAKES and the low method of energy consumption in fluidization mode with ammonium poly-vanadate.
The invention provides a kind of ammonium poly-vanadate fluidization and produce the method for powdery Vanadium Pentoxide in FLAKES.Described method adopts fluidized bed reaction system to realize, described fluidized bed reaction system comprises the pre-fluidization system of material and fluidizer, fluidizer comprises fluidized-bed agent structure, be arranged on the opening for feed of fluidized-bed agent structure one side, be arranged on the outlet of coarse particles material and the fine granular materials outlet of fluidized-bed agent structure opposite side, be arranged on gas distributor and the fluidizing agent entrance of fluidized-bed agent structure bottom, and the short transverse of fluidized-bed agent structure to be arranged on fluidized-bed agent structure inner and have bar shaped or a plate type member of temperature controlling function, the difference of altitude of opening for feed and the outlet of coarse particles material is 1.20～1.30m, described method comprises step: adopt pre-fluidization system to carry out pre-fluidization treatment to ammonium poly-vanadate material, so that ammonium poly-vanadate material enters fluidized-bed agent structure with fluidized state from opening for feed, simultaneously from fluidizing agent entrance to fluidized-bed agent structure, providing flow velocity is 120～250Nm
3the pressurized air that/h, pressure are 60～70kPa, it is 490～560 DEG C by the temperature in bar shaped or plate type member control fluidized-bed agent structure, the residence time of ammonium poly-vanadate material in fluidized-bed agent structure is 40～60min, obtains powdery Vanadium Pentoxide in FLAKES from the outlet of coarse particles material and fine granular materials outlet.
Compared with prior art, beneficial effect of the present invention comprises: temperature of reaction is low, is conducive to save energy and reduce the cost; Technique can long-time continuous direct motion; The V producing
2o
5grade can reach 98 national standards.
Brief description of the drawings
Fig. 1 shows ammonium poly-vanadate fluidization of the present invention and produces the structural representation of the fluidizer that the method for powdery Vanadium Pentoxide in FLAKES uses.
Description of reference numerals is as follows:
1-fluidized-bed agent structure, 2-opening for feed, the outlet of 3a-coarse particles material, the outlet of 3b-fine granular materials, 4-gas distributor, 5-fluidizing agent entrance, 6-temperature control member
Embodiment
Hereinafter, describe the method for ammonium poly-vanadate fluidization production powdery Vanadium Pentoxide in FLAKES of the present invention in detail in connection with exemplary embodiment.
As shown in Figure 1, the fluidizer using in method of the present invention comprises fluidized-bed agent structure 1, opening for feed 2, coarse particles material outlet 3a, fine granular materials outlet 3b, gas distributor 4, fluidizing agent entrance 5 and temperature control member 6.Wherein, opening for feed 2 is arranged on a side (as the left side in Fig. 1) of fluidized-bed agent structure 1, and opening for feed 2 is along the direction setting being tilted to; Coarse particles material outlet 3a and fine granular materials outlet 3b are arranged on the opposite side of fluidized-bed agent structure 1, fine granular materials outlet 3b is positioned at the top of coarse particles material outlet 3a, 3b is along the direction setting being tilted in fine granular materials outlet, the direction setting under coarse particles material outlet 3a edge is tilted to.Coarse particles material outlet 3a is higher than opening for feed 2, and difference of altitude (as shown in the L in Fig. 1) between the two is 1.20～1.30m.Gas distributor 4 and fluidizing agent entrance 5 are arranged on the bottom of fluidized-bed agent structure 1, and fluidizing agent (for example, air) after fluidizing agent entrance and gas distributor, enters the inside of fluidized-bed agent structure 1 successively.Temperature control member is that to be arranged on fluidized-bed agent structure 1 along the short transverse of fluidized-bed agent structure 1 inner and have bar shaped or the plate type member of temperature controlling function, and for example, temperature control member can be tubulose.Temperature control member (for example, baffle plate or heat transfer tube etc.) is set in the short transverse of fluidized-bed inside and can effectively suppresses back-mixing, destroy air pocket, the material being conducive to uniting carries out fragmentation, extends the residence time of material.
In one exemplary embodiment of the present invention, the method that powdery Vanadium Pentoxide in FLAKES is produced in ammonium poly-vanadate fluidization adopts fluidized bed reaction system to realize.Fluidized bed reaction system comprises the pre-fluidization system of material (for example, U-shaped feed system) and above-mentioned fluidizer.Specifically, the method that powdery Vanadium Pentoxide in FLAKES is produced in ammonium poly-vanadate fluidization is: adopt pre-fluidization system to carry out pre-fluidization treatment to ammonium poly-vanadate (being abbreviated as APV) material, so that ammonium poly-vanadate material enters fluidized-bed agent structure 1 with fluidized state from opening for feed 2, providing flow velocity simultaneously from fluidizing agent entrance to fluidized-bed agent structure 1 is 120～250Nm
3the pressurized air that/h, pressure are 60～70kPa, it is 490～560 DEG C by the temperature in bar shaped or plate type member control fluidized-bed agent structure 1, the residence time of ammonium poly-vanadate material in fluidized-bed agent structure 1 is 40～60min, obtains powdery Vanadium Pentoxide in FLAKES from coarse particles material outlet 3a and fine granular materials outlet 3b.For example, obtain powdery Vanadium Pentoxide in FLAKES product and (comprise the V obtaining from coarse particles discharge port and fine particle discharge port
2o
5particle) in, the product that granularity is greater than 120 mesh sieve institute correspondingly-sized accounts for more than 80%, and the product that granularity is less than 200 mesh sieve institute correspondingly-sized accounts for below 20%.
In addition,, in exemplary embodiment of the present invention, it is 200～300 DEG C that compressed-air actuated temperature control is preferably controlled.
In exemplary embodiment of the present invention, preferably, the particle diameter of ammonium poly-vanadate material is less than the corresponding size of 200 mesh sieve (referred to as being less than 200 orders), otherwise be not easy to realize pre-fluidization, but method of the present invention also can be used particle diameter to be greater than the ammonium poly-vanadate material of 200 mesh sieve institute correspondingly-sized.In addition, pre-fluidization treatment step gas flow rate is preferably 4～8Nm
3/ h.
In the method for the invention, carry out pre-fluidisation to ammonium poly-vanadate early stage can make ammonium poly-vanadate raw material enter fluidized-bed with fluidized state, material is evenly distributed in fluidized-bed, be heated more evenly fast, compared with spiral charging, pre-fluidisation can be broken up ammonium poly-vanadate in advance, having avoided material enters fluidized-bed and also has the situations such as bulk material, lumpy material, make material fluid effect in fluidized-bed better, being conducive to provides good environment and atmosphere for the reaction of ammonium poly-vanadate material in fluidized-bed agent structure; In addition, be 1.20～1.30m by the difference of altitude of opening for feed and the outlet of coarse particles material, the residence time on ammonium poly-vanadate material in fluidized-bed is played direct impact, also the flow to fluidizing agent in fluidized-bed, flow velocity, pressure play remote effect, thereby be conducive to Reaction time shorten, reduce fluidized-bed reaction temperature, reduce energy consumption, environment protection is played a good role; In addition, the factors such as the flow velocity of residence time of material, fluidized-bed reaction temperature, fluidizing agent, flow, pressure influence each other, and can be finally technique long-time continuous of the present invention direct motions; In addition can make and reach the V that is 98% to grade in GB GB3283-87
2o
5the powder Vanadium Pentoxide in FLAKES of the requirement of (referred to as 98 national standards).
Compared with prior art, the beneficial effect of method of the present invention comprises: temperature of reaction is low, is conducive to save energy and reduce the cost; Technique can long-time continuous direct motion; The V producing
2o
5grade can reach 98 national standards.
Below in conjunction with concrete example, exemplary embodiment of the present invention is described.
Example 1
The difference of altitude that opening for feed and coarse particles outlet are set is 1.21m.
The granularity of ammonium poly-vanadate material is less than 200 orders.Adopt U valve feed system to carry out pre-fluidization treatment to ammonium poly-vanadate material, so that ammonium poly-vanadate material is entering before fluidized-bed in fluidized state.The compressed-air actuated flow velocity that control enters fluidized-bed agent structure from fluidizing agent entrance is 160 ± 10Nm
3/ h, pressure are 62 ± 2kPa.Be 520 ± 5 DEG C by the temperature in temperature control member control fluidized-bed agent structure, the residence time of ammonium poly-vanadate material in fluidized-bed agent structure is 50 ± 5min, obtains powdery Vanadium Pentoxide in FLAKES from the outlet of coarse particles material and fine granular materials outlet.Obtain in powdery Vanadium Pentoxide in FLAKES product, the product that granularity is greater than 120 mesh sieve institute correspondingly-sized accounts for approximately 82%, and the product that granularity is less than 200 mesh sieve institute correspondingly-sized accounts for approximately 16%.Gained Vanadium Pentoxide in FLAKES V
2o
5grade is 98.2%, meets the requirement of 98 national standards.
Example 2
The difference of altitude that opening for feed and coarse particles outlet are set is 1.24m.
The granularity of ammonium poly-vanadate material is for being less than 200 orders.Adopt U valve feed system to carry out pre-fluidization treatment to ammonium poly-vanadate material, so that ammonium poly-vanadate material is entering before fluidized-bed in fluidized state.The compressed-air actuated flow velocity that control enters fluidized-bed agent structure from fluidizing agent entrance is 220 ± 10Nm
3/ h, pressure are 68 ± 2kPa.Be 500 ± 5 DEG C by the temperature in temperature control member control fluidized-bed agent structure, the residence time of ammonium poly-vanadate material in fluidized-bed agent structure is 45 ± 5min, obtains powdery Vanadium Pentoxide in FLAKES from the outlet of coarse particles material and fine granular materials outlet.Obtain in powdery Vanadium Pentoxide in FLAKES product, the product that granularity is greater than 120 mesh sieve institute correspondingly-sized accounts for approximately 85%, and the product that granularity is less than 200 mesh sieve institute correspondingly-sized accounts for approximately 13%.Gained Vanadium Pentoxide in FLAKES V
2o
5grade can reach 98.3%, meets 98 national standards.
Example 3
The difference of altitude that opening for feed and coarse particles outlet are set is 1.30m.
The granularity of ammonium poly-vanadate material is for being less than 200 orders.Adopt U valve feed system taking flow velocity as 4 ± 1Nm
3the gas of/h carries out pre-fluidization treatment to ammonium poly-vanadate material, so that ammonium poly-vanadate material is entering before fluidized-bed in fluidized state.The compressed-air actuated flow velocity that control enters fluidized-bed agent structure from fluidizing agent entrance is 200 ± 10Nm
3/ h, pressure are that 65 ± 2kPa, temperature are 220 ± 5 DEG C.Be 530 ± 5 DEG C by the temperature in temperature control member control fluidized-bed agent structure, the residence time of ammonium poly-vanadate material in fluidized-bed agent structure is 55 ± 5min, obtains powdery Vanadium Pentoxide in FLAKES from the outlet of coarse particles material and fine granular materials outlet.Obtain in powdery Vanadium Pentoxide in FLAKES product, the product that granularity is greater than 120 mesh sieve institute correspondingly-sized accounts for approximately 95%, and the product that granularity is less than 200 mesh sieve institute correspondingly-sized accounts for approximately 4%.Gained Vanadium Pentoxide in FLAKES V
2o
5grade can reach 98.4%, meets 98 national standards.
Example 4
The difference of altitude that opening for feed and coarse particles outlet are set is 1.25m.
The granularity of ammonium poly-vanadate material is for being less than 200 orders.Adopt U valve feed system taking flow velocity as 6 ± 1Nm
3the gas of/h carries out pre-fluidization treatment to ammonium poly-vanadate material, so that ammonium poly-vanadate material is entering before fluidized-bed in fluidized state.The compressed-air actuated flow velocity that control enters fluidized-bed agent structure from fluidizing agent entrance is 220 ± 10Nm
3/ h, pressure are that 65 ± 2kPa, temperature are 280 ± 5 DEG C.Be 500 ± 5 DEG C by the temperature in temperature control member control fluidized-bed agent structure, the residence time of ammonium poly-vanadate material in fluidized-bed agent structure is 50 ± 5min, obtains powdery Vanadium Pentoxide in FLAKES from the outlet of coarse particles material and fine granular materials outlet.Obtain in powdery Vanadium Pentoxide in FLAKES product, the product that granularity is greater than 120 mesh sieve institute correspondingly-sized accounts for approximately 90%, and the product that granularity is less than 200 mesh sieve institute correspondingly-sized accounts for approximately 9%.Gained Vanadium Pentoxide in FLAKES V
2o
5grade can reach 98.0%, meets 98 national standards.
In sum, the advantages such as the inventive method has that technique is simple and easy to, wide adaptability low, easy to operate by, equipment requirements, cost is low, product purity is high, epigranular, energy consumption are low, environmental protection, have good Social benefit and economic benefit.
Although described the present invention with exemplary embodiment by reference to the accompanying drawings above, those of ordinary skill in the art should be clear, in the case of not departing from the spirit and scope of claim, can carry out various amendments to above-described embodiment.
Claims (5)
1. the method that powdery Vanadium Pentoxide in FLAKES is produced in ammonium poly-vanadate fluidization, it is characterized in that, described method adopts fluidized bed reaction system to realize, described fluidized bed reaction system comprises the pre-fluidization system of material and fluidizer, fluidizer comprises fluidized-bed agent structure, be arranged on the opening for feed of fluidized-bed agent structure one side, be arranged on the outlet of coarse particles material and the fine granular materials outlet of fluidized-bed agent structure opposite side, be arranged on gas distributor and the fluidizing agent entrance of fluidized-bed agent structure bottom, and the short transverse of fluidized-bed agent structure to be arranged on fluidized-bed agent structure inner and have bar shaped or a plate type member of temperature controlling function, the difference of altitude of opening for feed and the outlet of coarse particles material is 1.20～1.30m, described method comprises step: adopt pre-fluidization system to carry out pre-fluidization treatment to ammonium poly-vanadate material, so that ammonium poly-vanadate material enters fluidized-bed agent structure with fluidized state from opening for feed, simultaneously from fluidizing agent entrance to fluidized-bed agent structure, providing flow velocity is 120～250Nm
3the pressurized air that/h, pressure are 60～70kPa, it is 490～560 DEG C by the temperature in bar shaped or plate type member control fluidized-bed agent structure, the residence time of ammonium poly-vanadate material in fluidized-bed agent structure is 40～60min, obtains powdery Vanadium Pentoxide in FLAKES from the outlet of coarse particles material and fine granular materials outlet.
2. the method for powdery Vanadium Pentoxide in FLAKES is produced in ammonium poly-vanadate fluidization according to claim 1, it is characterized in that, described compressed-air actuated temperature control is 200～300 DEG C.
3. the method for powdery Vanadium Pentoxide in FLAKES is produced in ammonium poly-vanadate fluidization according to claim 1, it is characterized in that, the particle diameter of described ammonium poly-vanadate material is less than the corresponding size of 200 mesh sieve.
4. the method for powdery Vanadium Pentoxide in FLAKES is produced in ammonium poly-vanadate fluidization according to claim 1, it is characterized in that, described method also comprises that adopting fine granular materials to export gas discharge, that process through gathering dust carrys out pre-hot compressed air.
5. the method for powdery Vanadium Pentoxide in FLAKES is produced in ammonium poly-vanadate fluidization according to claim 1, it is characterized in that, described pre-fluidization treatment step gas flow rate is 4～8Nm
3/ h.
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| WO2016119722A1 (en) * | 2015-01-30 | 2016-08-04 | 中国科学院过程工程研究所 | System and method for purifying and preparing high-purity vanadium pentoxide powder |
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| WO2016119719A1 (en) * | 2015-01-30 | 2016-08-04 | 中国科学院过程工程研究所 | System and method for producing high-purity vanadium tetraoxide powder |
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| CN111498835A (en) * | 2020-04-27 | 2020-08-07 | 内蒙古骏成新能源科技有限公司 | Horizontal fluidizing device for gas-phase purification of carbon nano tube and fluidizing purification method |
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| US10099939B2 (en) | 2015-01-30 | 2018-10-16 | Institute Of Process Engineering, Chinese Academy Of Sciences | System and method for producing high-purity vanadium pentoxide powder |
| RU2670866C1 (en) * | 2015-01-30 | 2018-10-25 | Инститьют Оф Процесс Инжиниринг, Чайнис Академи Оф Сайнсис | System and method for producing high-purity vanadium pentoxide powder |
| US10112846B2 (en) | 2015-01-30 | 2018-10-30 | Institute Of Process Engineering, Chinese Academy Of Sciences | System and method for producing high-purity vanadium tetraoxide powder |
| US10125024B2 (en) | 2015-01-30 | 2018-11-13 | Institute Of Procees Engineering Chinese Academy Of Sciences | System and method for purifying and preparing high-purity vanadium pentoxide powder |
| RU2670866C9 (en) * | 2015-01-30 | 2018-12-11 | Инститьют Оф Процесс Инжиниринг, Чайнис Академи Оф Сайнсис | System and method for producing high-purity vanadium pentoxide powder |
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| CN111498835A (en) * | 2020-04-27 | 2020-08-07 | 内蒙古骏成新能源科技有限公司 | Horizontal fluidizing device for gas-phase purification of carbon nano tube and fluidizing purification method |
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