CN106732306A - The method of multicompartment fluidized bed steam reformer apparatus and treatment spent resin - Google Patents
The method of multicompartment fluidized bed steam reformer apparatus and treatment spent resin Download PDFInfo
- Publication number
- CN106732306A CN106732306A CN201611192421.4A CN201611192421A CN106732306A CN 106732306 A CN106732306 A CN 106732306A CN 201611192421 A CN201611192421 A CN 201611192421A CN 106732306 A CN106732306 A CN 106732306A
- Authority
- CN
- China
- Prior art keywords
- bed
- chamber
- reaction
- fluidized
- distribution grid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0006—Controlling or regulating processes
- B01J19/0013—Controlling the temperature of the process
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0046—Sequential or parallel reactions, e.g. for the synthesis of polypeptides or polynucleotides; Apparatus and devices for combinatorial chemistry or for making molecular arrays
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0053—Details of the reactor
- B01J19/006—Baffles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/248—Reactors comprising multiple separated flow channels
- B01J19/249—Plate-type reactors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
- B01J8/28—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations the one above the other
-
- G—PHYSICS
- G21—NUCLEAR PHYSICS; NUCLEAR ENGINEERING
- G21F—PROTECTION AGAINST X-RADIATION, GAMMA RADIATION, CORPUSCULAR RADIATION OR PARTICLE BOMBARDMENT; TREATING RADIOACTIVELY CONTAMINATED MATERIAL; DECONTAMINATION ARRANGEMENTS THEREFOR
- G21F9/00—Treating radioactively contaminated material; Decontamination arrangements therefor
- G21F9/28—Treating solids
- G21F9/30—Processing
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00002—Chemical plants
- B01J2219/00027—Process aspects
- B01J2219/0004—Processes in series
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00162—Controlling or regulating processes controlling the pressure
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00274—Sequential or parallel reactions; Apparatus and devices for combinatorial chemistry or for making arrays; Chemical library technology
- B01J2219/00277—Apparatus
- B01J2219/00279—Features relating to reactor vessels
- B01J2219/00306—Reactor vessels in a multiple arrangement
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00761—Details of the reactor
- B01J2219/00763—Baffles
- B01J2219/00765—Baffles attached to the reactor wall
- B01J2219/00777—Baffles attached to the reactor wall horizontal
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/24—Stationary reactors without moving elements inside
- B01J2219/2401—Reactors comprising multiple separate flow channels
- B01J2219/245—Plate-type reactors
- B01J2219/2451—Geometry of the reactor
- B01J2219/2453—Plates arranged in parallel
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- General Engineering & Computer Science (AREA)
- High Energy & Nuclear Physics (AREA)
- Combustion & Propulsion (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention provides a kind of multicompartment fluidized bed steam reformer apparatus and the method for the treatment of spent resin, belong to chemical field.Steam reforming reaction equipment is multicompartment fluidized bed reactor, by setting distribution grid and overflow pipe in a fluidized bed reactor, fluidized-bed reactor is divided into at least two independent beds；Spent resin, catalyst, additive and mineralizer are added into top bed, cracking reaction and/or mineralising reaction and/or reduction reaction occur, generate mineralized particles and cracking gas；Carbonaceous material reaction heat supply is added in the bed of lower section；The mineralized particles for reacting generation flow downward through overflow pipe under gravity, are finally discharged from fluidized-bed reactor bottom；The gas for reacting generation is discharged from fluidized-bed reactor top.The present invention can obtain that volume reduction ratio is big, the product that nucleic capture rate is high and anti-leaching performance is good, improve the controllability of course of reaction and the operation stability of fluidized-bed reactor.
Description
Technical field
The invention belongs to chemical field, and in particular to a kind of multicompartment fluidized bed steam reformer apparatus and treatment spent resin
Method.
Background technology
With the development of China's nuclear technology, gone in nuclear power plant's operation, nuclear fuel cycle, radioactive liquid waste treatment, nuclear facilities
It is dirty with retired, Isotope production with application and nuclear chemistry, radiochemical experiment etc. during, can produce useless containing active core
Thing, such as ion exchange resin, activated carbon, filter element, spent organic solvent, appliances for labor protection.Wherein, spent resin radioactivity is lived
Degree accounts for the 80% of nuclear power waste gross activity.At present, disposal of the China to radioactive spent resin mainly uses cement solidification method,
Curing agent is prepared with cement, miberal powder etc. and directly solidify not specially treated spent resin, then encapsulate, bury.This method into
This is low, simple to operate, but has the shortcomings that volume of waste increase-volume is big, nucleic anti-leaching performance is low, resin loading is small, nothing
Method meets the growing radioactive spent resin process demand of China and environmental requirement.
Fluidized bed steam reforming technique is that under the high temperature conditions, spent resin occurs the complex reactions such as cracking, mineralising and produces ore deposit
Thing residue such as metal oxide or carbide, then the method disposed after being carried out to residue.Steam reformation technology can be by organic resin
Inorganic matter is fully converted to, radioactive element is enriched in mineralizer, the mineralizer structure durability of generation, good stability, core
Plain anti-leaching performance is high, can reach the purpose of safe volume reduction.The method has significant volume reduction effect, and Waste volume can be reduced to
The 1/10~1/5 of before processing.And secondary pollution will not be produced in processing procedure, the synthesis gas produced after cracking can after treatment
It is converted into N2、CO2And water, generated without waste liquid substantially, safety non-pollution.There is fluidized bed steam reforming technique reaction temperature relatively to burn
The low, vent gas treatment of burning is simpler, waste residue is more stable compared with glass solidified body, do not produce the advantages such as liquid wastes, abroad nuclear power
The existing history for many years of the application of the process field of low-level radioactive waste in factory.
Fluidized bed steam reforming technique can be implemented in a fluidized-bed reactor, it is also possible in the fluidisation of multiple series connection
Implement in bed reactor, as described in United States Patent (USP) US6084147, US7011800.In fluidized bed steam reforming reactor, when
When spent resin occurs cracking and mineralising reaction, it also occur that carbonaceous material combustion reaction, reduction reaction etc. are various different types of
Reaction.These courses of reaction intercouple, once fluidized-bed reactor manipulation is bad, easily form hot localised points or production viscosity
Material, cause fluidized particles reunite caking, gently then influence fluidization quality and reaction effect, it is heavy then can cause defluidizationization parking.Cause
This, is badly in need of the new fluidized-bed reactor of exploitation and radioactive spent resin processing method, and the operation for improving fluidized-bed reactor is steady
The treatment effeciency of qualitative and spent resin.
The content of the invention
It is an object of the invention to provide a kind of use multicompartment fluidized bed steam reformer apparatus treatment spent resin method and its
Equipment, by decoupling and the optimal control of reaction temperature and its distribution to fluid bed steam reforming reaction process, improves fluidisation
The operation stability and reaction efficiency of bed reactor, acquisition nucleic anti-leaching performance is high, the solid product that volume reduction ratio is big.
The invention provides a kind of method that use multicompartment fluidized bed steam reformer apparatus process spent resin, including, with useless
Resin, carbonaceous material, mineralizer, additive, catalyst are raw material, with vapor and/or air and/or oxygen and/or nitrogen
Used as fluidizing gas, in the fluidized-bed reactor containing inert bed and under hot conditions, there is cracking reaction in spent resin
Become small organic molecule and the mineralized particles of metallic element are contained in mineralising reaction generation.Wherein, steam reforming reaction equipment
It is multicompartment fluidized bed reactor, by setting distribution grid and overflow pipe in a fluidized bed reactor, fluidized-bed reactor is divided into
At least two independent beds；By spent resin, catalyst, additive and mineralizer add top bed, occur cracking reaction and/
Or mineralising reaction and/or reduction reaction, generate mineralized particles and cracking gas；Carbonaceous material reaction is added to supply in the bed of lower section
Heat；The mineralized particles for reacting generation flow downward through overflow pipe under gravity, are finally arranged from fluidized-bed reactor bottom
Go out；The gas for reacting generation is discharged from fluidized-bed reactor top, and after removing dust through filter, feeding incinerator is burned, then
Through alkali cleaning, dry heel row deflation or row's torch.It is to be noted that follow-up gas treatment can be selected according to actual condition
Select, not as restriction.
Described carbonaceous material enters the first bed of multicompartment fluidized bed reactor bottom, with oxygen in the first bed
And/or water vapour reacts.Described carbonaceous material can also pass into other beds in addition to the first bed, in other beds
As reducing agent in layer.
C+O2→CO2
C+H2O→H2+CO
CO+H2O→CO2+H2
CO+O2→CO2
H2+O2→H2O
The raw materials such as described spent resin, mineralizer, additive, catalyst enter other beds in addition to the first bed,
There is cracking reaction and/or mineralising reaction and/or reduction reaction etc. in other beds, generate mineralized particles and cracking gas.Make
For a kind of preferred embodiment, additive and mineralizer are added spent resin by some beds of spent resin and catalyst addition the top
Place layer and carbonaceous material between layers one or more layers.There is cracking reaction in described resin, generate small molecule
Compound, discharges radioactive element, zwitterion etc..
CxHyOzSm→C+CH4+CO+H2+SOn+etc
CxHyOzNm→C+CH4+CO+H2+NOn+etc
The raw materials such as described mineralizer, additive enter other beds in addition to the first bed, are sent out in other beds
Raw mineralising reaction generation mineralized particles, complete the containing absorption to radioactive element, zwitterion etc..
2NaOH+Al2O3·2SiO2→2NaAlSiO4+H2O
8NaOH+2Cl-+3(Al2O3·2SiO2)→Na6Al6Si6O24(2NaCl)+3H2O+2OH-
The temperature control of described multicompartment fluidized bed reactor is extremely important.If temperature is too high, on the one hand can cause to put
Penetrating property nucleic volatilizees, and causes containing effect poor, causes radioactive pollution；On the other hand, the slaine of reaction generation can be melted and led
Cause fluidized particles to reunite to lump, cause fluidized-bed reactor defluidization.If temperature is too low, cracking reaction accessory substance increases,
Coking can be caused to lump.Because mineralising reaction and cracking reaction are the endothermic reaction, need to using the combustion reaction of carbonaceous material come
Heat is provided.A kind of preferred temperature control scheme is the temperature of each bed from bottom to up in described multicompartment fluidized bed reactor
Degree is gradually reduced.It is general, it is each to adjust by the method such as feed rate, feeding temperature, gas mixing ratio for adjusting each bed
The temperature of individual bed.A kind of preferred scheme is that at least one heat-exchanger rig is set in each bed, for controlling bed temperature
Degree.The heat-exchanger rig can remove heat from bed, it is also possible to be input into heat to bed.Heat transferring medium can select commercial plant
Usually used recirculated water, the steam of different pressures grade, the gas of different temperatures, fused salt etc..Electrical heating etc. can also be used
Conventional heater meanses.
The Stress control of described multicompartment fluidized bed reactor is also extremely important, can be operated under condition of negative pressure, also may be used
Operated with normal pressure or condition of high voltage.The pressure limit of recommendation be 0.001~10MPaA, preferably 0.01~1MPaA, more preferably
0.09~0.1MPaA.Operation can avoid the leakage of radionuclide under condition of negative pressure, improve the security of system.
Described fluidizing gas is by nitrogen and/or oxygen and/or water vapour and/or CO and/or CO2And/or H2Composition.Institute
The fluidized gas stated are at least into the first bed of multicompartment fluidized bed reactor bottom.A kind of preferred intake method is part stream
Change gas and enter the first bed, partial fluidised gas enters other beds.Into the fluidized gas of each bed flow and composition according to
Reaction is required and temperature control requirement determines.
Inert particle is filled with described multicompartment fluidized bed reactor, the particle is only used as fluidizing agent, being not involved in
Learn reaction.One kind is preferred embodiment to be equipped with inert particle in each bed.Another preferred embodiment is
In addition to the first bed, inert particle is all filled with other beds.
Residence time of described spent resin, the mineralized particles in reactor needs strict control.Residence time is too short, instead
Should fully carry out；Residence time is long, and reactor efficiency is too low.The residence time of spent resin and mineralized particles be 1s~
10hr, preferably 10s~2hr, more preferably 1min~30min.
At a kind of preferred multicompartment fluidized bed steam reformer reactors preferred structure described in
The method for putting spent resin, it is characterised in that：The multicompartment fluidized bed is divided into three beds, be followed successively by from top to bottom the 3rd bed,
Second bed, the first bed.Wherein, the temperature of the first bed be 750~1000 DEG C, the temperature of the second bed be 500~750
DEG C, the temperature of the 3rd bed be 200~500 DEG C.The spent resin and catalyst add the 3rd bed, in the 3rd bed
Generation functional group elimination reaction, solid product enters the second bed through overflow pipe；There is spent resin in second bed
Skeleton cracking reaction simultaneously discharges radionuclide, zwitterion etc.；The mineralizer, additive etc. add the second bed,
There is mineralising reaction in second bed, radionuclide and zwitterion are mineralized product in mineralising reaction and are wrapped to form
Solid particle, mineralized particles enter the first bed through overflow pipe；The carbonaceous material adds the first bed, in first bed
The reaction such as middle carbonaceous material and water vapour, oxygen.At least one heat-exchanger rig is respectively provided with each bed, for controlling bed
Layer temperature.The temperature of the 3rd bed by regulation into the 3rd bed vapor (steam) temperature, may participate in the carbon dust of oxidation reaction
Amount and/or oxygen flow and/or the control of heat-exchanger rig exchange capability of heat；The temperature of the second bed by adjust feed rate and/or
The carbon dust amount control of feeding temperature and/or heat-exchanger rig exchange capability of heat and/or participation oxidation reaction；The temperature of the first bed passes through
Regulation enters carbon dust amount and/or oxygen flow and/or vapor flow and/or the heat-exchanger rig exchange capability of heat control of the 3rd bed
System.
Present invention also offers a kind of multicompartment fluidized bed reactor for the spent resin processing method, including fluid bed
Reactor tower body and the gas distribution grid and overflow pipe that are arranged in tower body：In tower body, from the bottom of towe of the tower body to tower
Top, first chamber, second chamber can be divided into by boundary of the gas distribution grid, and first chamber is distributed with second chamber by gas
Plate and the overflow pipe connection being arranged on the gas distribution grid.It is distributed by setting gas in fluidized-bed reactor tower body
Plate so that the fluidizing gas into the second bed between tower top and gas distribution grid is contacted with reactant and reacted, produces
First gas product by tower top open top discharge, the first solid product by overflow pipe enter gas distribution grid and bottom of towe
Between the first bed, and with fluidizing gas haptoreaction；The carbonaceous material added in first bed reacts life with fluidizing gas
Into gas, the first solid product can also react generating portion gas, and produced second gas product enters the second bed,
Second solid product enters bottom of towe and is reclaimed by bottom opening.So the chamber between tower top and bottom of towe can be divided at least two
The different region of temperature, by making the reaction temperature of first bed higher than the reaction temperature of second bed, and reclaims
Second solid product, can obtain that nucleic anti-leaching performance is high, the solid product that volume reduction ratio is big.
Present invention also offers the multicompartment fluidized bed reactor that another kind is used for the spent resin processing method, including fluidisation
Bed reactor tower body and the first gas distribution grid, second gas distribution grid and the dividing plate that are arranged in tower body：In tower body,
Can be divided into first as boundary from the bottom of towe of the tower body to tower top with the dividing plate, second gas distribution grid, first gas distribution grid
Chamber, second chamber, the 3rd chamber, the 4th chamber；First chamber and second chamber are isolated by dividing plate, first chamber and the 3rd
Chamber is connected by the overflow pipe being arranged on the second gas distribution grid, and second chamber passes through second gas with the 3rd chamber
Distribution grid is connected, and the 3rd chamber and the 4th chamber are by setting the first gas distribution grid and being arranged on the first gas point
Fabric swatch overflow flow tube is connected.
Although the above-mentioned form that provide only two-layer and three laminarizations bed, in fact can also be in fluidized-bed reactor tower
More beds are set in body.
The present invention has following features：Oxidation reaction, reduction reaction, cracking reaction and mineralising reaction are placed on different beds
Completed in layer, it is to avoid influencing each other between each reaction, greatly improve the controllability of course of reaction；By controlling each bed
Temperature Distribution and the product distribution of layer, it is to avoid particle agglomeration lumps, and greatly improves the operation stability of fluidized-bed reactor；Can be with
Acquisition volume reduction ratio is big, the product that radionuclide capture rate is high and nucleic anti-leaching performance is high.
Brief description of the drawings
A kind of structural representation of multicompartment fluidized bed steam reformer reactors that Fig. 1 is provided for the present invention.
The structural representation of another multicompartment fluidized bed steam reformer reactors that Fig. 2 is provided for the present invention.
Specific embodiment
The useless tree of the multicompartment fluidized bed steam reformer apparatus and treatment provided the present invention below in conjunction with Fig. 1 and Fig. 2
The method of fat is described in detail.
As shown in figure 1, multicompartment fluidized bed steam reformer apparatus of the invention include fluidized-bed reactor tower body 1 and
Gas distribution grid 2 and overflow pipe 3 in tower body 1 are arranged on, wherein, in tower body 1, from the bottom of towe of the tower body to tower top, with
The gas distribution grid 2 can be divided into first chamber, second chamber for boundary, and first chamber passes through gas distribution grid 2 with second chamber
And the overflow pipe 3 being arranged on the gas distribution grid 2 is connected.Is provided with the side wall of the tower body 1 of the second chamber
One opening the 6, second opening 7 and the 4th opening 9, are provided with the 3rd opening 8, the on the side wall of the tower body 1 of the second chamber
Five openings 10 and the 6th opening 11.Gas vent 4 is additionally provided with the top of tower body, tower body bottom is provided with solid outlet 5.
As shown in Fig. 2 a kind of preferred multicompartment fluidized bed steam reformer apparatus of the invention include：It is arranged at tower body
First gas distribution grid 2, second gas distribution grid 15, dividing plate 17 in 1, the first overflow pipe 3, the second overflow pipe 16.Wherein, from
The bottom of towe of the tower body 1 is to tower top with the dividing plate 17, second gas distribution grid 15, first gas distribution grid 2 for boundary can be divided into
First chamber, second chamber, the 3rd chamber, the 4th chamber；First chamber and second chamber are isolated by dividing plate 17, first chamber
Connected by the second overflow pipe 16 being arranged on the second gas distribution grid 15 with the 3rd chamber, second chamber and the 3rd chamber
Room is connected by second gas distribution grid 15, and the 3rd chamber and the 4th chamber are by the first gas distribution grid 2 and are arranged on
The first overflow pipe 3 on the first gas distribution grid is connected.The 7th is provided with the side wall of the tower body 1 of the second chamber
The opening 14 of the opening of opening the 12, the 8th 13 and the 9th, is provided with the second opening 7, the on the side wall of the tower body 1 of the 3rd chamber
The opening 10 of three opening the 8, the 5th and the 6th opening 11, the He of the first opening 6 is provided with the side wall of the tower body 1 of the 4th chamber
4th opening 9.Gas vent 4 is additionally provided with the top of tower body, tower body bottom is provided with solid outlet 5.
As shown in Fig. 2 in described multicompartment fluidized bed steam reformer reactors tower body 1, the tower top of tower body to the dividing plate
With diameter greater than bottom of towe to the tower body diameter between the dividing plate 17, its ratio is 1 to tower body between 17:(0.3~1.0).It is described
Aperture is provided with first gas distribution grid 2 and the second gas distribution grid 15 in tower body 1, small aperture is 0.1~5mm,
Percent opening is 1%~5%.A kind of preferred scheme is, from side hole type gas distribution grid, blast cap to be installed in the top of passage.
Can be from known cap structure.Preferred cap structure is that blast cap top is taper, and its inclination angle is more than solid accumulation
Angle.
The tower top of the tower body 1 to described first opening 6 vertical range a, tower body 1 tower top to described second be open 7
Vertical range b, tower body 1 tower top to the described 3rd opening 8 vertical range c, tower body 1 tower top to the described 4th be open 9
Vertical range d, tower body 1 tower top to the described 5th opening 10 vertical range e, tower body 1 tower top to the described 6th be open
11 vertical range f, the tower top of tower body 1 to the described 7th opening 12 vertical range g, tower body 1 tower top opened to the described 8th
13 vertical range h of mouth, the tower top of tower body 1 preferably meet between the vertical range i of the described 9th opening 14：a:b:c:d:e:
f:g:h:I=1:(2~4):(2~5):(1~1.5):(2~3):(2~4):(6~8):(6~9):(8~10).Described
The volume ratio of four chambers, the 3rd chamber, second chamber and first chamber is 1:(1~1.6):(1~1.7):(0.4~1).
The tower top of the tower body 1 to the vertical range A of the upper orifice of the overflow pipe 3, tower body 1 tower top to first gas
Meet between the vertical range B of body distribution grid 2：A:B=1:(1~1.5), the tower top of tower body 1 to the lower nozzle of the overflow pipe 3
Vertical range C, the tower top of tower body 1 meet between the vertical range D of the second gas distribution grid 15：C:D=1:(1~
1.3)；The tower top of tower body 1 is distributed to the tower top of the vertical range a of the upper orifice of the overflow pipe 16, tower body 1 to the second gas
Meet between the vertical range b of plate 15：a:B=1:(1~1.3), vertical range c, the tower of the tower top of tower body 1 to the dividing plate 17
The tower top of body 1 meets between the vertical range d of the lower nozzle of the overflow pipe 16：c:D=1:(1~1.2).
Present invention also offers a kind of method that use multicompartment fluidized bed steam reformer apparatus process spent resin, the method bag
Include with spent resin, carbonaceous material, mineralizer, additive, catalyst as raw material, with vapor and/or air and/or oxygen and/
Or nitrogen and/or CO and/or CO2And/or H2As fluidizing gas, in the fluidized-bed reactor containing inert particle bed with
And under hot conditions, spent resin occurs cracking reaction and becomes small organic molecule and discharge radioactive element, while there is ore deposit
Change the mineralized particles that zwitterion and radioactive element are contained in reaction generation, carbonaceous material occurs anti-with oxygen and/or water vapour
Heat should be provided.Wherein, steam reforming reaction equipment is multicompartment fluidized bed reactor, by setting in a fluidized bed reactor point
Fabric swatch and overflow pipe, at least two independent beds are divided into by fluidized-bed reactor；By spent resin, catalyst, additive and ore deposit
Agent adds top bed, and cracking reaction and/or mineralising reaction and/or reduction reaction occur, and generates mineralized particles and cracking gas；
Carbonaceous material reaction heat supply is added in the bed of lower section；The mineralized particles for reacting generation are downward through overflow pipe under gravity
Flowing, finally discharges from fluidized-bed reactor bottom；The gas for reacting generation is discharged from fluidized-bed reactor top, through filter
Remove dust after, feeding incinerator burn, then through alkali cleaning, dry heel row deflate or row torch.
According to the method that the present invention is provided, a kind of preferred scheme is that described carbonaceous material reacts into multicompartment fluidized bed
First bed of device bottom, reacts in the first bed with oxygen and/or water vapour.Described carbonaceous material can be with
Into other beds in addition to the first bed, as reducing agent in other beds.The raw materials such as described spent resin, catalyst
Into other beds in addition to the first bed, there is cracking reaction in other beds, generate micromolecular compound, discharge
Radioactive element, zwitterion etc..The raw materials such as described mineralizer, additive enter other beds in addition to the first bed,
There are mineralising reaction generation mineralized particles in other beds, complete the containing absorption to radioactive element, zwitterion etc..One
Kind preferred scheme is some beds that described spent resin and catalyst add the top, additive and mineralizer is added useless
Layer where resin and carbonaceous material between layers one or more layers.
According to the method that the present invention is provided, the temperature control of described multicompartment fluidized bed reactor is extremely important.If warm
Height is spent, radionuclide on the one hand can be caused to volatilize, cause containing effect poor, cause radioactive pollution；On the other hand, react
The slaine of generation can be melted causes fluidized particles reunion caking, causes fluidized-bed reactor defluidization.If temperature is too low, split
Solution byproduct of reaction increases, and also results in coking caking.Because mineralising reaction and cracking reaction are the endothermic reaction, need to utilize and contain
The combustion reaction of carbonizable substance provides heat.The temperature of each bed is gradually from bottom to up in described multicompartment fluidized bed reactor
Reduce.It is general, adjust each bed by adjusting the method such as feed rate, feeding temperature, gas mixing ratio of each bed
Temperature.A kind of preferred scheme is that at least one heat-exchanger rig is set in each bed, for controlling bed temperature.This is changed
Thermal can remove heat from bed, it is also possible to be input into heat to bed.Heat transferring medium can generally be made from commercial plant
Recirculated water, the steam of different pressures grade, the gas of different temperatures, fused salt etc..Can also be conventional using electrical heating etc.
Heater meanses.
According to the method that the present invention is provided, the Stress control of described multicompartment fluidized bed reactor is also extremely important, can be with
Operated under condition of negative pressure, it is also possible to operated under normal pressure or condition of high voltage.The pressure limit of recommendation is 0.001~10MPaA,
It is preferred that 0.01~1MPaA, more preferably 0.09~0.1MPaA.Operation can avoid the leakage of radionuclide under condition of negative pressure,
The security of raising system.
In the present invention, described fluidized gas are at least into the first bed of multicompartment fluidized bed reactor bottom.It is a kind of
Preferred intake method is that partial fluidised gas enters the first bed, and partial fluidised gas enters other beds.Into each bed
The flow and composition of fluidized gas are required according to reaction and temperature control requirement determines.
In the present invention, inert particle is filled with described multicompartment fluidized bed reactor, the particle is only used as fluidisation and is situated between
Matter, is not involved in chemical reaction.One kind is preferred embodiment to be equipped with inert particle in each bed.It is another preferred
Implementation method is in addition to the first bed, inert particle to be all filled with other beds.
In the present invention, the strict control of residence time needs of described spent resin, mineralized particles in reactor.Stop
Time is too short, and reaction can not be carried out fully；Residence time is long, and reactor efficiency is too low.The stop of spent resin and mineralized particles
Time is 1s~10hr, more preferably preferably 10s~2hr, 1min~30min.
Present invention also offers a kind of useless tree is processed using described multicompartment fluidized bed steam reformer reactors preferred structure
The method of fat, it is characterised in that：The multicompartment fluidized bed is divided into three beds, be followed successively by from top to bottom the 3rd bed, second
Layer, the first bed.Wherein, the spent resin and catalyst add the 3rd bed, functional group occurs in the 3rd bed and takes off
Except reaction, product enters the second bed through overflow pipe；There is the skeleton cracking reaction of spent resin in second bed and release
Release radionuclide, zwitterion etc.；The mineralizer, additive etc. add the second bed, are sent out in second bed
Raw mineralising reaction, radionuclide and zwitterion are mineralized product in mineralising reaction and are wrapped to form solid particle, mineralising
Grain enters the first bed through overflow pipe；The carbonaceous material adds the first bed, carbonaceous material and water in first bed
Steam, oxygen etc. react.At least one heat-exchanger rig is respectively provided with each bed, for controlling bed temperature.Described
The temperature of three beds by regulation into the 3rd bed vapor (steam) temperature, may participate in the carbon dust amount and/or oxygen stream of oxidation reaction
Amount and/or the control of heat-exchanger rig exchange capability of heat；The temperature of the second bed by adjust feed rate and/or feeding temperature and/or
Heat-exchanger rig exchange capability of heat is controlled；The temperature of the first bed enters the carbon dust amount and/or oxygen flow of the 3rd bed by adjusting
And/or vapor flow and/or the control of heat-exchanger rig exchange capability of heat.
In the present invention, the charging of the spent resin, mineralizer and carbonaceous material include but is not limited to slurries state, solid-state,
The forms such as liquid, gas entrainment；It is long that the inert bed medium includes but is not limited to aluminum oxide, dolomite, sintered bauxite, rosy clouds
The materials such as stone, sintering calcium silicates；The mineralizer includes but is not limited to the materials such as kaolin, montmorillonite, illite clay；It is described
Carbonaceous material includes but is not limited to the reducing substances such as charcoal, coke, coal dust, carbohydrate.The catalyst includes but is not limited to oxidation
The materials such as calcium, magnesia, aluminum sulfate, iron, ferric sulfate, ferric nitrate；The additive includes but is not limited to sodium chloride, hydroxide
The materials such as sodium, sodium sulphate.
Fluidized bed steam reformer apparatus according to the present invention and spent resin method of disposal, by fluidized-bed reactor
First gas distribution grid and second gas distribution grid are set in tower body so that the entered between tower top and first gas distribution grid
The fluidizing gas of three beds is contacted with reactant and reacted, and the first gas product of generation is discharged by the open top of tower top,
The second bed and fluidisation that first solid product is entered between the distribution grid of gas first and second gas distribution grid by overflow pipe
Gas haptoreaction, the second gas product of generation enters the 3rd bed, and the second solid product enters bottom of towe the bottom of by through overflow pipe
Reclaim portion opening.So the chamber between tower top and bottom of towe can be divided into the different region of at least two temperature, by making
The reaction temperature of the reaction temperature higher than the 3rd bed of the second bed is stated, and reclaims the second solid product, so as to obtain core
The solid product that plain anti-leaching performance is high, volume reduction ratio is big.
The invention will be further described by the following examples.
Embodiment 1
The present embodiment is used to illustrate the multicompartment fluidized bed steam reformer apparatus of present invention offer and the side for the treatment of spent resin
Method.
Spent resin, the fluidized bed steam reformer apparatus are processed using multicompartment fluidized bed steam reformer apparatus as shown in Figure 2
Including a fluidized-bed reactor tower body 1, tower body internal diameter 0.5m, tower body height 7m are disposed with first from tower top to bottom of towe
Gas distribution grid 2, second gas distribution grid 15 and dividing plate 17, open pore size is 1mm, perforate on the first gas distribution grid 2
Rate 2%, open pore size is 0.8mm, percent opening 2% on second gas distribution grid 15.Described in from the bottom of towe of the tower body 1 to tower top every
Plate 17, second gas distribution grid 15, first gas distribution grid 2 can be divided into first chamber, second chamber, the 3rd chamber and for boundary
Four chambers；The opening 13 of the 7th opening the 12, the 8th and the 9th opening 14 are provided with the side wall of the tower body 1 of the second chamber,
The opening 10 of the opening of the second opening the 7, the 3rd the 8, the 5th and the 6th opening are provided with the side wall of the tower body 1 of the 3rd chamber
11, the first opening 6 and the 4th opening 9 are provided with the side wall of the tower body 1 of the 4th chamber, set in the tower top of the tower body 1
Open top 4 is equipped with, the bottom of towe of the tower body 1 is provided with bottom opening 5.First chamber and second chamber by dividing plate 17 every
From first chamber is connected with the 3rd chamber by the overflow pipe 16 being arranged on the second gas distribution grid 15, second chamber
Connected by second gas distribution grid 15 with the 3rd chamber, the 3rd chamber and the 4th chamber are distributed by setting the first gas
Plate 2 is connected with the first gas distribution grid overflow flow tube 3 is arranged on.The internal diameter of the overflow pipe 3 is 0.08m, the overflow pipe
16 internal diameters are 0.08m.The tower top of tower body 1 is to the tower body diameter and bottom of towe between the dividing plate 17 to the tower between the dividing plate 17
The ratio of body diameter is 1:0.5, the vertical range a of the tower top of tower body 1 to the described first opening 6, the tower top of tower body 1 to described the
The vertical range b of two openings 7, the tower top of tower body 1 to the described 3rd are open 8 vertical range c, the tower top of tower body 1 to described the
The vertical range d of four openings 9, the tower top of tower body 1 to the described 5th are open 10 vertical range e, the tower top of tower body 1 to described the
The vertical range f of six openings 11, the tower top of tower body 1 to the described 7th are open 12 vertical range g, the tower top of tower body 1 described in
The vertical range h of the 8th opening 13, the tower top of tower body 1 meet between the vertical range i of the described 9th opening 14：a:b:c:d:
e:f:g:h:I=1:2:3:1:3:3:6:7:9, the volume ratio of the 4th chamber, the 3rd chamber, second chamber and first chamber
It is 1:1.3:1.5:0.7, the vertical range A of the tower top of tower body 1 to the upper orifice of the overflow pipe 3, the tower top of tower body 1 to described
Meet between the vertical range B of one gas distribution grid 2：A:B=1:1.2, the tower top of tower body 1 to the lower nozzle of the overflow pipe 3
Vertical range C, the tower top of tower body 1 meet between the vertical range D of the second gas distribution grid 15：C:D=1:1.2；Tower
The tower top of body 1 to the vertical range a of the upper orifice of the overflow pipe 16, tower body 1 tower top to the second gas distribution grid 15
Meet between vertical range b：a:B=1:1.1, the vertical range c of the tower top of tower body 1 to the dividing plate 17, the tower top of tower body 1 are arrived
Meet between the vertical range d of the lower nozzle of the overflow pipe 16：c:D=1:1.05.
Using the method for present invention treatment radioactive spent resin, non-reactive fluidizing medium is respectively charged into the 3rd bed and second
Bed, filling height is 1.5 times of fluid bed internal diameter.By containing spent resin, (content of Cs and Co is respectively：0.1g/kg resins,
Cationic ion-exchange resin be Amberlite IRN-77, anion exchange resin be Amberlite IRN-78) slurries state it is anti-
Answer thing to pass through the described first opening and be passed through the 3rd bed, catalyst is passed through the carbon containing thing such as the 3rd bed, charcoal by the 4th opening
Matter each leads into the second bed and the first bed by the 3rd opening and the 7th opening, and kaolin is passed through second by the second opening
Bed, oxygen each leads into the second bed and the first bed by the 6th opening and the 9th opening, and water vapour is by the 5th opening
The second bed and the first bed are each led into the 8th opening.Wherein, the charging mass ratio of mineralizer kaolin and spent resin is
2:1, the charging mass ratio of mineralizer kaolin and additive NaOH is 1.7:1, the charging matter of catalyst iron and spent resin
Amount is than being 0.05:1, the charging mass ratio of oxygen and carbonaceous material is 2:1.By the flow, the oxygen flow that adjust carbonaceous material
Three temperature of bed are controlled with inlet steam temperature.In the 3rd bed, spent resin enters the 3rd through by gas distribution grid
The fluidizing gas of bed is together fluidized with non-reactive fluidizing medium and contacted, and functional group's cracking reaction occurs, and reaction temperature is 350 DEG C,
Pressure 68KPaA, the reaction time is 2 minutes, and the solid product of generation flows into the second bed through overflow pipe, and gas is by tower top outlet
Discharge.In the second bed, solid product and mineralizer that the 3rd bed is flowed into enter the stream of the second bed through gas distribution grid
Change gas is together fluidized with non-reactive fluidizing medium and contacted, and skeleton cracking occurs and discharges nucleic, while there is mineralising reaction capture
Nucleic forms mineralized particles, and reaction temperature is 725 DEG C, and pressure 84KPaA, the reaction time is 5 minutes.In the first bed, it is passed through
Carbonaceous material and oxygen there is the reaction release heat such as burning, reaction temperature is 900 DEG C, and pressure is 100KPaA.
The solid product that above-mentioned course of reaction is obtained is done into volume test, nuclide concentration test and the test of nucleic anti-leaching,
Result shows, compared with feed reactants, product volume reduction is the 1/9 of reactant, and nucleic wraps up efficiency up to 99.99%, and nucleic resists
Leaching efficiency is up to 99.9%.Parking situation device occurs caused by soilless sticking caking within three months experimental periods.
Embodiment 2
The present embodiment is used to illustrate multicompartment fluidized bed steam reformer apparatus and the treatment Spent Radioactive tree of present invention offer
The method of fat.
Spent resin is processed using multicompartment fluidized bed steam reformer apparatus same as Example 1, its processing procedure includes：Will
Non-reactive fluidizing medium is respectively charged into the 3rd bed and the second bed, and filling height is 1.5 times of fluid bed internal diameter.Useless tree will be contained
(content of Cs and Co is respectively fat：0.1g/kg resins, cationic ion-exchange resin is Amberlite IRN-77, anion exchange
Resin be Amberlite IRN-78) slurry liquid reactant by described first opening be passed through the 3rd bed, catalyst passes through
4th opening is passed through the carbonaceous materials such as the 3rd bed, charcoal and each leads into the second bed and the by the 3rd opening and the 7th opening
One bed, mineralizer is passed through the second bed by the second opening, and oxygen each leads into second by the 6th opening and the 9th opening
Bed and the first bed, steam each lead into the second bed and the first bed by the 5th opening and the 8th opening.Wherein, mineralising
The charging mass ratio of agent kaolin and spent resin is 2:1, the charging mass ratio of mineralizer kaolin and additive NaOH is
1.7:1, the charging mass ratio of catalyst iron and spent resin is 0.05:1, the charging mass ratio of oxygen and carbonaceous material is 2:1.It is logical
Flow, oxygen flow and the inlet steam temperature for overregulating carbonaceous material control three temperature of bed.In the 3rd bed, give up
Resin is contacted through together being fluidized with non-reactive fluidizing medium into the fluidizing gas of the 3rd bed by gas distribution grid, and function occurs
Group's cracking, reaction temperature is 300 DEG C, pressure 65KPaA, and the reaction time is 30 seconds, and the solid product of generation flows into the through overflow pipe
Two beds, gas is discharged by tower top outlet.In the second bed, the solid product and mineralizer that the 3rd bed is flowed into divide through gas
Fabric swatch is together fluidized with non-reactive fluidizing medium into the fluidizing gas of the second bed and contacted, and skeleton cracking occurs and discharges nucleic,
There is mineralising reaction capture nucleic simultaneously and form mineralized particles, reaction temperature is 600 DEG C, and pressure 85KPaA, the reaction time is 2 points
Clock.In the first bed, there is the reaction release heat such as burning in the carbonaceous material being passed through, reaction temperature is 900 DEG C, pressure with oxygen
Power is 101KPaA.
The solid product that above-mentioned course of reaction is obtained is done into volume test, nuclide concentration test and the test of nucleic anti-leaching,
Result shows, compared with feed reactants, product volume reduction is the 1/8 of reactant, and nucleic wraps up efficiency up to 99.87%, and nucleic resists
Leaching efficiency is up to 99.5%.Parking situation device occurs caused by soilless sticking caking within three months experimental periods.Contrast two, example
Second bed temperature is less than temperature in example 1 in 2, and the not thorough nucleic release of resin matrix cracking is incomplete, and mineralising reaction is absorbed heat
Deficiency causes product grain structural stability relatively low, causes the reduction of product volume reduction ratio, nucleic parcel efficiency and anti-leaching to be imitated
Rate reduction, is consistent with result of the test.
Embodiment 3
The device that the present embodiment is used is identical with precedent, and difference is that mineralizer montmorillonite and spent resin add in device
Material mass ratio is 1.5:1, the charging mass ratio of mineralizer montmorillonite and additive sodium chloride is 0.8:1, catalyst sulfuric acid iron and
The charging mass ratio of spent resin is 0.07:1, the charging mass ratio of oxygen and carbonaceous material is 3:1.The solid product for obtaining does
Test, its effect is substantially the same manner as Example 2.
Embodiment 4
The device that the present embodiment is used is identical with precedent, and difference is that mineralizer illite and spent resin add in device
Material mass ratio is 1:1, the charging mass ratio of mineralizer illite and additive sodium sulphate is 1:1, catalyst magnesia is set with useless
The charging mass ratio of fat is 0.02:1, the charging mass ratio of oxygen and carbonaceous material is 3:2.The solid product for obtaining is surveyed
Examination, its effect is substantially the same manner as Example 2.
Embodiment described above is a kind of preferably scheme of the invention, and so it is not intended to limiting the invention.Have
The those of ordinary skill for closing technical field, without departing from the spirit and scope of the present invention, can also make various changes
Change and modification.Therefore the technical scheme that all modes for taking equivalent or equivalent transformation are obtained, all falls within guarantor of the invention
In the range of shield.
Claims (10)
1. a kind of method that use multicompartment fluidized bed steam reformer apparatus process spent resin, it is characterised in that：Described steam weight
Whole consersion unit is multicompartment fluidized bed reactor, by setting distribution grid and overflow pipe in a fluidized bed reactor, by fluid bed
Reactor is divided at least two independent beds；Spent resin, catalyst, additive and mineralizer are added into top bed, is occurred
Cracking reaction and/or mineralising reaction and/or reduction reaction, generate mineralized particles and cracking gas；Added in the bed of lower section carbon containing
Substance reaction heat supply；The mineralized particles for reacting generation flow downward through overflow pipe under gravity, finally anti-from fluid bed
Device bottom is answered to discharge；The gas for reacting generation is discharged from fluidized-bed reactor top.
2. it is according to claim 1 treatment spent resin method, it is characterised in that：Described carbonaceous material enters many laminar flows
First bed of fluidized bed reactor bottom, reacts in the first bed with oxygen and/or water vapour.
3. it is according to claim 1 treatment spent resin method, it is characterised in that：Described spent resin and catalyst are added
Some beds of the top, by additive and mineralizer add layer where spent resin and carbonaceous material between layers one layer or
In multilayer.
4. according to the method for any described treatment spent resins of claim 1-3, it is characterised in that：Described multicompartment fluidized bed is anti-
Answer in device that the temperature of each bed is gradually reduced from bottom to up.
5. according to the method for any described treatment spent resins of claim 1-3, it is characterised in that：Fluidized gas at least enter multilayer
First bed of fluidized-bed reactor bottom.
6. according to the method for any described treatment spent resins of claim 1-3, it is characterised in that：The multicompartment fluidized bed is divided into
Three beds, are followed successively by the 3rd bed, the second bed, the first bed from top to bottom；Wherein, the temperature of the first bed be 750~
1000 DEG C, the temperature of the second bed is 500~750 DEG C, and the temperature of the 3rd bed is 200~500 DEG C.
7. it is according to claim 6 treatment spent resin method, it is characterised in that：The spent resin and catalyst add the
, there is functional group's elimination reaction in three beds, the skeleton that spent resin occurs in second bed splits in the 3rd bed
Solution reaction；The mineralizer and additive add the second bed, mineralising reaction occurs in second bed and completes to the moon
The absorption of cation, radioactive element, generates mineralized particles；The carbonaceous material adds the first bed, in first bed
Middle carbonaceous material and water vapour and/or oxygen reaction.
8. according to the method for any described treatment spent resins of claim 1-7, it is characterised in that：Set respectively in each bed
At least one heat-exchanger rig is put, for controlling bed temperature.
9. a kind of multicompartment fluidized bed steam reformer apparatus for realizing claim 1 methods described, including fluidized-bed reactor tower body
And it is arranged on gas distribution grid and overflow pipe in tower body, it is characterised in that：In tower body, from the bottom of towe of the tower body to tower
Top, first chamber, second chamber are at least divided into as boundary with the gas distribution grid, and first chamber is with second chamber by gas point
Fabric swatch and the overflow pipe connection being arranged on the gas distribution grid.
10. multicompartment fluidized bed steam reformer apparatus according to claim 9, it is characterised in that：Including fluidized-bed reactor
Tower body and the first gas distribution grid being arranged in tower body, second gas distribution grid and dividing plate, in tower body, from the tower
The bottom of towe of body is divided into first chamber, with the dividing plate, second gas distribution grid, first gas distribution grid as boundary successively to tower top
Two chambers, the 3rd chamber, the 4th chamber；First chamber and second chamber are isolated by dividing plate, and first chamber is led to the 3rd chamber
The overflow pipe connection being arranged on the second gas distribution grid is crossed, second chamber passes through second gas distribution grid with the 3rd chamber
Connection, the 3rd chamber and the 4th chamber are by setting the first gas distribution grid and being arranged on the first gas distribution grid
Overflow pipe is connected.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611192421.4A CN106732306A (en) | 2016-12-21 | 2016-12-21 | The method of multicompartment fluidized bed steam reformer apparatus and treatment spent resin |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611192421.4A CN106732306A (en) | 2016-12-21 | 2016-12-21 | The method of multicompartment fluidized bed steam reformer apparatus and treatment spent resin |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106732306A true CN106732306A (en) | 2017-05-31 |
Family
ID=58894004
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201611192421.4A Withdrawn CN106732306A (en) | 2016-12-21 | 2016-12-21 | The method of multicompartment fluidized bed steam reformer apparatus and treatment spent resin |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106732306A (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109273129A (en) * | 2018-11-01 | 2019-01-25 | 深圳中广核工程设计有限公司 | The cracking of nuclear power station radioactivity debirs and mineralising treatment reactor |
| CN109346204A (en) * | 2018-09-29 | 2019-02-15 | 深圳中广核工程设计有限公司 | Radioactive spent resin treatment formulations |
| CN110634586A (en) * | 2019-09-23 | 2019-12-31 | 中国核动力研究设计院 | Method and system for treating radioactive organic waste by using three-phase fluidized bed |
| CN110639352A (en) * | 2019-11-02 | 2020-01-03 | 孙发喜 | Vertical multi-stage absorption tower |
| CN111854477A (en) * | 2019-04-28 | 2020-10-30 | 航天长征化学工程股份有限公司 | Cooling device |
| CN112700901A (en) * | 2019-10-23 | 2021-04-23 | 杭州双安科技有限公司 | Method for treating radioactive waste resin |
| CN112813504A (en) * | 2021-02-02 | 2021-05-18 | 北京绿清科技有限公司 | Single-furnace multilayer fluidized melting furnace |
| CN112973584A (en) * | 2021-02-07 | 2021-06-18 | 中国科学院过程工程研究所 | Fluidized bed reaction device and application thereof |
| CN114907884A (en) * | 2022-06-21 | 2022-08-16 | 山东省科学院能源研究所 | Multi-layer fluidized bed calcium chemical looping gasification hydrogen production device and method |
-
2016
- 2016-12-21 CN CN201611192421.4A patent/CN106732306A/en not_active Withdrawn
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109346204A (en) * | 2018-09-29 | 2019-02-15 | 深圳中广核工程设计有限公司 | Radioactive spent resin treatment formulations |
| CN109273129A (en) * | 2018-11-01 | 2019-01-25 | 深圳中广核工程设计有限公司 | The cracking of nuclear power station radioactivity debirs and mineralising treatment reactor |
| CN111854477A (en) * | 2019-04-28 | 2020-10-30 | 航天长征化学工程股份有限公司 | Cooling device |
| CN110634586A (en) * | 2019-09-23 | 2019-12-31 | 中国核动力研究设计院 | Method and system for treating radioactive organic waste by using three-phase fluidized bed |
| CN112700901A (en) * | 2019-10-23 | 2021-04-23 | 杭州双安科技有限公司 | Method for treating radioactive waste resin |
| CN110639352A (en) * | 2019-11-02 | 2020-01-03 | 孙发喜 | Vertical multi-stage absorption tower |
| CN110639352B (en) * | 2019-11-02 | 2023-10-20 | 孙发喜 | Vertical multistage absorption tower |
| CN112813504A (en) * | 2021-02-02 | 2021-05-18 | 北京绿清科技有限公司 | Single-furnace multilayer fluidized melting furnace |
| CN112973584A (en) * | 2021-02-07 | 2021-06-18 | 中国科学院过程工程研究所 | Fluidized bed reaction device and application thereof |
| CN114907884A (en) * | 2022-06-21 | 2022-08-16 | 山东省科学院能源研究所 | Multi-layer fluidized bed calcium chemical looping gasification hydrogen production device and method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106732306A (en) | The method of multicompartment fluidized bed steam reformer apparatus and treatment spent resin | |
| CN106683734A (en) | Method for processing waste resin by using dual-zone fluidized bed steam reforming device | |
| CN208622447U (en) | Nuclear power station radioactive spent resin processing unit | |
| CN1059753A (en) | Gasification substance gasification and/or gas conversion process and device and the high-temperature heat-exchanging of implementing this method | |
| CN106531274A (en) | Radioactive waste treatment system and treatment method including same | |
| WO2010025620A1 (en) | Method and device for producing yellow phosphorus or phosphoric acid by vertical airtight smoke-baffle kiln | |
| CA1196509A (en) | Method for final treatment of radioactive organic material | |
| CN106479541A (en) | A kind of system and method for processing coal dust and living beings | |
| CN110431639A (en) | The hot volume reduction of radioactive waste | |
| CN205974428U (en) | Step combination bed gasification system | |
| WO2010006464A1 (en) | A process for producing carbon disulfide by circulating fluid bed | |
| CN106118750A (en) | Step combination cot gasification system | |
| US3852216A (en) | Process for producing coarse particles of active carbon in a fluidized bed with added inert particles | |
| CN209343792U (en) | Handle the process system of radioactivity debirs | |
| CN205295251U (en) | Two sections pyrolysis gasification system of solid waste | |
| US4202861A (en) | Method for dry reprocessing of irradiated nuclear fuels | |
| CN206340352U (en) | A kind of processing system of radwaste | |
| CN205990416U (en) | A kind of utilization body of heater fume afterheat the system of high efficiente callback iron-containing resource | |
| CN107555479B (en) | A kind of chloridising prepares the system and method for high-purity low price barium oxide | |
| CN105753016B (en) | The multitube moving bed reaction device of ammonium chloride pyrolysis separation preparing ammonia and hydrogen chloride | |
| CN112700901B (en) | Method for treating radioactive waste resin | |
| CN108358204B (en) | Double-bed activated carbon activation system and activation method | |
| CN207811689U (en) | A kind of knockdown pyrolysis gasifying device | |
| CN105836758B (en) | A kind of monoblock type ammonium chloride pyrolysis installation and pyrolytic process based on cross-flow heat exchange | |
| CN100439295C (en) | A process for manufacturing potassium sulfate fertilizer and other metal sulfates |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WW01 | Invention patent application withdrawn after publication |
Application publication date: 20170531 |
|
| WW01 | Invention patent application withdrawn after publication |