CN1183542A - Ammonium diuranate fluidized drying process and apparatus - Google Patents
Ammonium diuranate fluidized drying process and apparatus Download PDFInfo
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- CN1183542A CN1183542A CN 96117804 CN96117804A CN1183542A CN 1183542 A CN1183542 A CN 1183542A CN 96117804 CN96117804 CN 96117804 CN 96117804 A CN96117804 A CN 96117804A CN 1183542 A CN1183542 A CN 1183542A
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- drying
- adu
- bed
- fluidizing
- drying bed
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- 238000001035 drying Methods 0.000 title claims abstract description 71
- ZAASRHQPRFFWCS-UHFFFAOYSA-P diazanium;oxygen(2-);uranium Chemical compound [NH4+].[NH4+].[O-2].[O-2].[O-2].[O-2].[O-2].[O-2].[O-2].[U].[U] ZAASRHQPRFFWCS-UHFFFAOYSA-P 0.000 title claims abstract description 47
- 239000000843 powder Substances 0.000 claims abstract description 26
- 238000000034 method Methods 0.000 claims abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 22
- 239000002002 slurry Substances 0.000 claims abstract description 18
- 238000005516 engineering process Methods 0.000 claims abstract description 11
- 239000008187 granular material Substances 0.000 claims abstract description 3
- 208000011580 syndromic disease Diseases 0.000 claims description 7
- 239000012530 fluid Substances 0.000 claims description 5
- 238000003825 pressing Methods 0.000 claims description 5
- 238000005243 fluidization Methods 0.000 claims description 4
- 239000008367 deionised water Substances 0.000 claims description 2
- 229910021641 deionized water Inorganic materials 0.000 claims description 2
- 239000004809 Teflon Substances 0.000 claims 1
- 229920006362 Teflon® Polymers 0.000 claims 1
- 230000008676 import Effects 0.000 claims 1
- 239000007788 liquid Substances 0.000 claims 1
- 238000004886 process control Methods 0.000 claims 1
- 239000000463 material Substances 0.000 abstract description 4
- 239000003758 nuclear fuel Substances 0.000 abstract description 4
- 238000006243 chemical reaction Methods 0.000 abstract description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 239000002994 raw material Substances 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract description 3
- 239000012535 impurity Substances 0.000 abstract 1
- 239000000047 product Substances 0.000 description 10
- 238000004537 pulping Methods 0.000 description 8
- 239000012065 filter cake Substances 0.000 description 7
- 238000001694 spray drying Methods 0.000 description 5
- 238000003756 stirring Methods 0.000 description 5
- 238000001914 filtration Methods 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 238000013467 fragmentation Methods 0.000 description 2
- 238000006062 fragmentation reaction Methods 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000013067 intermediate product Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 1
- 229910052770 Uranium Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 230000001427 coherent effect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 239000011737 fluorine Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- JFALSRSLKYAFGM-UHFFFAOYSA-N uranium(0) Chemical compound [U] JFALSRSLKYAFGM-UHFFFAOYSA-N 0.000 description 1
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Abstract
The invention provides an Ammonium Diuranate (ADU) drying process technology and device, and relates to an intermediate process of chemical conversion in nuclear fuel production for a nuclear power station. Water content in ADU slurry<When 45 percent of the total amount of the raw materials is needed, the raw materials are fed into the fluidized drying bed by a spiral feeder,>when 45 percent of the total amount of the ADU powder is obtained, introducing the ADU powder into a fluidized drying bed by a pressure air ejector, wherein the drying capacity is 35-55 kg/h, the water content of the produced ADU powder is less than or equal to 3 percent by weight, and the diameter of the granules is<0.1mm, loose packed density< 1.4g/cm3The product has no impurity pollution, and is easy to store and transport by air flow. The technology has the advantages of short process, energy saving, small volume, low investment, simple operation, safety and reliability, and is suitable for235Drying materials with the U abundance of less than or equal to 5 percent by weight.
Description
The present invention relates to the production of used in nuclear power station nuclear fuel, be specifically related to the dry and device of the intermediate products ammonium diuranate (ADU) in the chemical industry transfer process.
In the nuclear fuel Chemical Manufacture, by raw material UF
6To producing UO
2Powder has intermediate products ADU, and the drying of ADU is that ADU sedimentation and filtration filter cake is reduced into UO
2Pilot process before the powder.What adopt at present is spray drying technology, and shortcoming is that the ADU filter cake must add the water pulping, makes it be suitable for the spray-drying operation.Pulping process has increased by three running devices (pulping groove, pump groove and head tank), and operating cost is increased; Next is that (Φ 1000 * 3500mm), and wall sticking phenomenon is arranged, and only are fit to greatly for equipment volume
235The drying of U＜3%wtADU, and dry products needs just to be convenient to the air-flow conveying after screen(ing) machine is wiped sieve and to enter reduction furnace transform through wiping.Abroad, the dry employing of the ADU multistage drying machine of East Sea cause institute of Japanese nuclear fuel exploitation cause group; Drying time is long, and dry products need crush and screen, operate numerous, pollute big; The ADU drying that the remote Nuo Geersi of Russia Wu Sijika digests worker's conversion plant, U.S.'s Westinghouse Electrical Corp. all adopts rotary furnace, and (Φ 420～500 * 5000～8000mm) dehydrates, and changes into U
3O
8, change into UO again
2This technology advanced person, but device structure complexity, investment are big needs also that filter plant is supporting with it efficiently, is difficult to realize.
The objective of the invention is provides plant-scale technology and device for the drying of ADU, and this technology satisfies the nuclear criticality safety requirement, and dry products ADU powder satisfies UO
2The processing request of powder has overcome the shortcoming of above-mentioned technology, can satisfy
235The drying of U≤5%wtADU.
The present invention is achieved by following technical measures: fluidizing drying bed (6) with agitator (7) and carrier (5) under the acting in conjunction of pressure fan (11) and exhaust blower (10), make fluidizing drying bed in carrier (5) part fluidisation, the part shape that becomes to roll; When the preheating temperature to 120 of powder dust collecting system (8) ℃, the ADU filter cake is stirred by slurry vessel (3), and its slurry enters screw feeder (4), goes into the interior carrier of fluidisation drying bed (6) (5) by screw feeding again and goes up dry; As if ADU cake moisture＞45%wt (this kind material＜1%), add the slurry of water furnishing 55～65%wt, stir through tank diameter (1), by pressing empty injector (2) injection slurry to go on the interior carrier of fluid bed (6) (5).Pressure reduction 1.5～3.5kPa in the control bed, wind speed 2.5～4.5m/s in the bed, 135～145 ℃ of fluidizing drying bed outlet wind-warm syndrome.The ADU wet feed under the effect of carrier (5) and hot blast, make its dehydration, drying, collision fragmentation after, dry again.Up to the powder output of certain particle size, certain water content, just bring powder collection system (8) into and be gathered into product and enter in the hopper (9) with tail gas.If fluidizing drying bed (6) pressure reduction＞3.5kPa starts agitator (7) and smashes coherent mass, keep the unimpeded and fluidized drying of hot blast.
Technical data:
Pressure fan (11) air quantity: 500～800m
3/ h (adjustable), blast:＞4.5kPa;
Exhaust blower (10) air quantity: 1300～1600m
3/ h (adjustable), blast: 8kPa;
Slurry vessel (3) speed of agitator: 60r/min;
Fluidizing drying bed (6) inlet wind-warm syndrome: 200～300 ℃;
Fluidizing drying bed (6) outlet wind-warm syndrome: 135～145 ℃;
Fluidizing drying bed (6) pressure reduction: 1.5～3.5kPa;
ADU cake moisture＜44%wt, feeding speed: 60～80kg/h;
ADU slip water content is 55～65%wt, feeding speed: 70～90l/h;
Fluidizing drying bed (6) drying capacity: ADU powder 35～55kg/h;
ADU powder granule diameter:＜0.1mm;
ADU powder moisture :≤3%wt;
ADU apparent density of powder:＜1.4g/cm
3
The present invention need not add the water pulping because of the ADU filter cake, than the low 30%wt of spraying material water content, therefore, does not need pulping groove, pump groove, high-order storage tank etc., has shortened technical process, has saved the energy.The drying device volume is little, and (Φ 250 * 4000mm), reduced investment, seedless accident potential.Be the outlet temperature of stabilization fluid drying bed (6), adopt the instrument tandem to adjust storage heater power, easy and simple to handle, the technology continous-stable; Product moisture≤3%wt, nothing caking, no bulky grain do not need fragmentation to sieve with dry again; Be beneficial to air-flow conveying and spiral and infeed reduction furnace conversion or storage.
Fig. 1 is fluidizing drying bed process equipment connection layout.Form by feed drying system, powder collection system and hot air source system three parts among the figure.
The feed drying system: the ADU slurry (water content＜45%wt material) that is come by centrifuge flows directly into slurry vessel (3), sends into screw feeder (4) after stirring, and sends in fluidizing drying bed (6) again; During ADU slurry water content＞45%wt, adding deionized water furnishing water content in tank diameter (1) is the homogeneous slurry of 55～65%wt, by pressing empty injector (5) to introduce in fluidizing drying bed (6).In fluidizing drying bed (6), the ADU wet pulp is dry under the mass-and heat-transfer of hot blast and carrier (5), and the stirring of agitator (7) in addition ensures that hot blast is unimpeded.
Powder collection system: this system comprises cyclone separator, bagroom, hopper (9).Under the effect of exhaust blower (10), the ADU powder enters powder collection system (8) with tail gas and is gathered into product, enters in the hopper (9).
The hot air source system: pressure fan (11) blasts air cleaner (12) with room air, enters air heater (13) after the filtration and is heated to 200～300 ℃, enters fluidizing drying bed (6) carrier layer (5) by fluidizing drying bed (6) bottom; Exhaust blower (10) ensures in fluidizing drying bed (6) and is little negative pressure, makes fluidizing drying bed (6) interior pressure reduction in control range.
Fig. 2 is for pressing empty injector schematic diagram.ADU slurry feed tube (15) is Φ 18 * 200mm, presses empty air inlet pipe (16) to be Φ 14 * 85mm, and angle is 35 °.
Embodiment:
Use the type testing (seeing Table 1) that present technique and device carry out:
In mode 1, after the ADU filtration direct charging stock tank of filter cake (3) stirs, send into fluidizing drying bed (6) carriers (5) by the feed spiral of screw feeder (4) and go up drying, broken, powder collection;
In mode 2, the ADU filter cake advances in the tank diameter (1), and adding water, it is transferred to water content is 55～65%wt, after stirring, go up by the carrier (5) of pressing empty injector (2) to introduce fluidizing drying bed (6) dry, broken, powder collection.
In order to contrast, special spray-drying mode and this method used compares, and operating condition is shown in table 1.
The dry products performance is shown in table 2, and item compared has ADU powder total uranium amount (U
Always), fluorine content (F), water content (H
2O), specific surface (SSA), apparent density (ρ
a) and percent by weight median particle size (d
50).
From table 1 and table 2 as can be seen: this technological process is short, power consumption less, drying capacity is big, product need not wiped sieve, the product water content is lower and stable, and is safe and reliable to operation, this method is better than spray drying technology.
Table 1.
| Item compared | Fluidizing drying bed mode | The spray- | |
| Mode | |||
| 1 | | ||
| ADU filter cake pulping | Need not | Add 10～20% water pulpings | Add 30% water pulping |
| ADU slurry feeding speed | ??70kg/h | ???80～90l/h | ???90～1001/h |
| Press empty injection pressure (MPa) | Need not | ???0.10～0.25 | ???0.40～0.45 |
| Heating furnace power (kW) | ??80～90 | ?????80～90 | ??????135 |
| Advance the bed (tower) wind-warm syndrome (℃) | ??200～250 | ????250～300 | ????400～450 |
| Go out the bed (tower) wind-warm syndrome (℃) | ??135～145 | ????135～145 | ????140～150 |
| Drying capacity (kg powder) | ??33～55 | ?????35～55 | ??????35～45 |
| The ADU powder is wiped sieve | Need not | Need not | Need to wipe sieve |
| The transferred product mode | Air-flow is carried | Air-flow is carried | Air-flow is carried |
| The operation difficulty or ease | Easily | Easily | Difficult |
| Nuclear safety | Safety | Safety | Dangerous |
Table 2.
| The ADU performance | Fluidizing drying bed mode | Sparge dry mode (contrast) | |
| | | ||
| ???U Always(％) | ??73.89 | ??75.37 | ????????75.0 |
| ????F(％) | ???2.4 | ???2.31 | ?????????2.31 |
| ???H 2O(％) | ???2.21 | ???2.01 | (2.62 indivedual＞3) |
| ???SSA(m 2/g) | ??16.26 | ???9.76 | ?????????7.37 |
| ??ρ a(g/cm 3) | ???1.09 | ???1.18 | (1.25 having removed agglomerate) |
| ??d 50(μm) | ???5.22 | ???10.2 | ?????????12.4 |
Claims (10)
1. an ammonium diuranate (ADU) drying technique is characterized in that, this technology adopts fluid drying, and its process control parameter is:
When ADU slurry water content is 40～44%wt, it is poured in the slurry vessel (3), go into fluidisation drying bed (6) by screw feeder (4) feed, feeding speed is 60～80kg/h;
During ADU slurry water content＞45%wt, it is added deionized water in tank diameter (1) to be transferred to water content be 55～65%wt, and by pressing empty injector (2) feed to go into fluidisation drying bed (6), feeding speed is 70～90l/h;
Fluidizing drying bed (6) import wind-warm syndrome: 200～300 ℃;
Fluidizing drying bed (6) outlet wind-warm syndrome: 135～145 ℃;
Fluidizing drying bed (6) pressure reduction: 1.5～3.5kPa;
Fluidizing drying bed (6) interior wind speed: 2.5～4.5m/s;
ADU powder moisture :≤3%wt;
ADU powder granule diameter:＜0.1mm;
ADU apparent density of powder:＜1.4g/cm
3This fluid drying is suitable for the continous-stable operation.
2. according to the drying technique of claim 1, it is characterized in that the drying cartridge of this process using is equipped with: fluidizing drying bed (6), press empty injector (2) and tank diameter (1), screw feeder (4) and slurry vessel (3).
3. according to the drying technique of claim 1 or 2, it is characterized in that described fluidizing drying bed (6) are of a size of Φ 250 * 4000mm; In carrier (5) is housed, be teflon rod, be of a size of Φ 4 * 4～5mm, charge weight is 18～20kg; And be provided with agitator (7), power of motor 1.1kW, rotating speed 60r/min, adjustable in the bottom.
4. according to the drying technique of claim 1 or 2, it is characterized in that, described fluidizing drying bed (6) outlet temperature adopts tandem instrument control heater power, be that the fluidizing drying bed thermometric instrument of going up is made homophony, thermometric instrument of the fluidizing drying bed end is done secondary the accent, transfers instrument to regulate scr voltage converter by pair.
5. according to the drying technique of claim 1 or 2, it is characterized in that the agitator (7) of described fluidizing drying bed (6) bottom is enabled during pressure reduction＞3.5kPa in bed.
6. according to the drying technique of claim 1 or 2, it is characterized in that described fluidizing drying bed (6) bottom is provided with sieve plate (14), percent opening is 21～24%, and the aperture is 3mm.
7. according to the drying technique of claim 1 or 2, it is characterized in that the slurry pipe (15) that advances of the empty injector of described pressure (2) is Φ 18 * 200mm, air inlet pipe (16) is Φ 14 * 85mm, and angle is 35 °; The pressure pneumatics power of using is purifying air of 0.1～0.25MPa.
8. according to the drying technique of claim 1 or 2, it is characterized in that described screw feeder (4) is Φ 60 * 1200mm; Power of motor is 1.1kW, rotating speed 60r/min, adjustable.
9. according to the drying technique of claim 1 or 2, it is characterized in that described slurry vessel (3) is of a size of Φ 250 * 1200mm; The bottom of its agitator is the cone spiral, with shell wall gap＜2mm, and the spacing＜100mm that is connected of cone spiral top and screw feeder (4); Power of motor is 0.75kW, and rotating speed is 60r/min.
10. according to the drying technique of claim 1 or 2, it is characterized in that described tank diameter (1) is located at presses near the empty injector (2), the entry position of interior liquid level of tank diameter (1) and the empty injector of pressure (2) is at equal height.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 96117804 CN1076467C (en) | 1996-11-26 | 1996-11-26 | ammonium diuranate fluidized drying method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 96117804 CN1076467C (en) | 1996-11-26 | 1996-11-26 | ammonium diuranate fluidized drying method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1183542A true CN1183542A (en) | 1998-06-03 |
| CN1076467C CN1076467C (en) | 2001-12-19 |
Family
ID=5124622
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 96117804 Expired - Fee Related CN1076467C (en) | 1996-11-26 | 1996-11-26 | ammonium diuranate fluidized drying method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1076467C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101596430A (en) * | 2003-10-16 | 2009-12-09 | 原子燃料工业株式会社 | Dripping surface solidfying device and apparatus for manufacturing ammonium diuranate particle |
-
1996
- 1996-11-26 CN CN 96117804 patent/CN1076467C/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101596430A (en) * | 2003-10-16 | 2009-12-09 | 原子燃料工业株式会社 | Dripping surface solidfying device and apparatus for manufacturing ammonium diuranate particle |
| CN1867516B (en) * | 2003-10-16 | 2010-11-03 | 原子燃料工业株式会社 | Dropping supply device |
| CN101596430B (en) * | 2003-10-16 | 2012-11-28 | 原子燃料工业株式会社 | Dripping surface solidfying device and apparatus for manufacturing ammonium diuranate particle |
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| Publication number | Publication date |
|---|---|
| CN1076467C (en) | 2001-12-19 |
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| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
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Granted publication date: 20011219 Termination date: 20131126 |