CN207996670U - A kind of fluidization gas-solid heat exchange device and sorbent reactions also original system - Google Patents
A kind of fluidization gas-solid heat exchange device and sorbent reactions also original system Download PDFInfo
- Publication number
- CN207996670U CN207996670U CN201721586332.8U CN201721586332U CN207996670U CN 207996670 U CN207996670 U CN 207996670U CN 201721586332 U CN201721586332 U CN 201721586332U CN 207996670 U CN207996670 U CN 207996670U
- Authority
- CN
- China
- Prior art keywords
- gas
- heat exchange
- fluidization
- exchange device
- solid heat
- 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.)
- Active
Links
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model is related to a kind of fluidization gas-solid heat exchange devices and sorbent reactions also original system, the fluidization gas-solid heat exchange device includes the heat exchanging segment (12) on top, the burning zone (8) of lower part and the outer fluidization regions (6) outside the heat exchanging segment, the heat exchanging segment (12) includes particle flow area and thermal current area (5), setting particulate matter flows into mouth (2) and loosens gas outlet (1) at the top of the particle flow area, the particle flow area bottom is communicated with the outer fluidization regions (6), the outer fluidization regions (6), which are equipped with, loosens gas import (9) and particle stream outlet (7), thermal current area (5) top setting combustion tail gas exports (10), the burning zone (8) is provided with fuel gas entrance.Heat exchanger provided by the utility model can directly utilize heat caused by burning, improve the efficiency of heating surface.
Description
Technical field
The utility model is related to a kind of from pre- thermal fluidization gas-solid heater and sorbent reactions also original system.
Background technology
In the gas-solid fluidized bed type reaction system continuously recycled, it is necessary to which reaching certain temperature goal response could occur.
Different measure can be taken to meet differential responses potential temperature, such as passes through high-temperature medium heat exchange, the exothermic heat of reaction of itself, external heat
Mode.
CN200810113392.7 and CN200910162162.4 is directed to the gas-solid fluidized bed type reaction system continuously recycled
It proposes using the high-temperature regenerated catalyst in catalytic cracking regenerator as heat source, is heated by the way of directly or indirectly contacting
The particulate matter of relative low temperature.
CN201010267428.4, CN201010267743.9 and CN201010283120.9 are directed to the gas-solid continuously recycled
Fluidized bed type reaction system proposes the high-temperature mixed gas generated using the burning of imflammable gas part and another stock also Primordial Qi
Body enters adsorbent regenerator together, and adsorbent to be generated is heated using direct-fired mode and is desorbed at high temperature again
It is raw.
In addition Electric heating (such as electrically heated rod or electric furnace) may be used to heat fluidised particulate matter, but adopt
Electric energy is lost with electrical heating, heating load is limited in a way, it is difficult to meet the changeable situation of commercial operating conditions.
Utility model content
The purpose of this utility model is to provide a kind of fluidization gas-solid heat exchange device and sorbent reactions also original system, this practicality
The fluidization gas-solid heat exchange device of novel offer can directly utilize heat caused by burning, improve the efficiency of heating surface.
To achieve the goals above, a kind of fluidization gas-solid heat exchange device provided by the utility model, includes the heat exchange on top
Section 12, the burning zone 8 of lower part and the outer fluidization regions 6 outside the heat exchanging segment, the heat exchanging segment 12 include particle flow area
With thermal current area 5, setting particulate matter in particle flow area top flows into mouth 2 and loosens gas outlet 1, the particle flow
Area bottom is communicated with the outer fluidization regions 6, and the outer fluidization regions 6, which are equipped with, loosens gas import 9 and particle stream outlet 7, institute
5 top of the thermal current area setting combustion tail gas stated exports 10, and the burning zone 8 is provided with fuel gas entrance.
Preferably, the loosening gas exports 1 lower part setting filter 11, and the particle flow area connects through filter 11
Lead to the loosening gas outlet 1.
Preferably, the filter 11 is porous ceramics or porous sintered metal pipe.
Preferably, the loosening gas exports 1 lower part setting filter 11, and the particle flow area connects through filter 11
Lead to the loosening gas outlet 1.
Preferably, the bottom of the outer fluidization regions 6 surrounds 12 bottom of heat exchanging segment, and the burning zone 8 passes through outer
Fluidization regions 6 are communicated with the thermal current area 5.
Preferably, the top of the outer fluidization regions 6 and 12 closed front of heat exchanging segment are located at closing described
The position of heat exchanging segment 0-80% from top to bottom.
Preferably, the particle dispersion area 3 and an at least heating tube 4 that the particle flow area includes top, it is described
3 heated pipe 4 of particle dispersion area is communicated with the outer fluidization regions 6, and the particulate matter flows into mouth 2 and loosens gas outlet 1 and sets
It is placed in the top of the particle dispersion area 3.
Preferably, the internal diameter of the heating tube is 5~200mm, preferably 10~150mm.
Preferably, reclinate arc is formed on the bottom of the outer fluidization regions 6, more preferable 6 ground bottom of outer fluidization regions
For spherical surface.
It includes the adsorptive reactor being sequentially communicated that the utility model, which also provides a kind of sorbent reactions also original system, system,
14, above-mentioned fluidization gas-solid heat exchange device and reducing/regenerating device 15,14 bottom of the adsorptive reactor are provided with regenerated flue gas and enter
Mouthfuls 16, adsorbent entrance 17,14 top of the adsorptive reactor are provided with adsorbent outlet 18 to be generated, regenerated flue gas outlet 19,
The reducing/regenerating device 15 is provided with also Primordial Qi entrance 20, reduction offgas outlet 21, adsorbent entrance 22 to be generated and regenerative adsorption
Agent outlet 26, the particulate matter of the adsorbent outlet to be generated 18 of the adsorptive reactor 14 and the fluidization gas-solid heat exchange device
Flow into the connection of mouth 2, the suction to be generated of the particle stream outlet 7 of the fluidization gas-solid heat exchange device and the reducing/regenerating device 15
Attached dose of entrance 22 is connected to, the adsorbent of the reproducing adsorbent outlet 26 and the adsorptive reactor 14 of the reducing/regenerating device 15
Entrance 17 is connected to.
Preferably, the reducing/regenerating device 15, which is additionally provided with, loosens gas entrance, the pine of the fluidization gas-solid heat exchange device
Outlet of taking offence 25 is connected to the loosening gas entrance 25 of the reducing/regenerating device 15.
Preferably, the system is additionally provided with adsorbent cooler 24, and the reproducing adsorbent of the reducing/regenerating device 15 goes out
Mouth is connected to by the adsorbent cooler 24 with the adsorbent entrance of the adsorptive reactor 14.
Fluidization gas-solid heat exchange device and sorbent reactions also original system provided by the utility model have the beneficial effect that:
Fluidization gas-solid heat exchange device provided by the utility model is simple in structure, and burning zone and heat exchanging segment are combined into one, drop
Low energy consumption, saves equipment investment;Spent agent preheating section is arranged in heater top, realizes the recycling of heat, improves
The utilization ratio of heat.Meanwhile spent agent can be loosened by loosening gas and be operated using fluidisation state, and the heat exchange effect between gas-solid is improved
Rate is that the mode of heating of solid particulate matter increases a feasible route.
Fluidization gas-solid heat exchange device provided by the utility model is not limited to the heating of adsorbent, can be widely used in oil
The heat exchange demand of particulate solid present in chemical field and environmental protection industry (epi), imflammable gas burn in fluidization gas-solid heat exchange device
Completely burned occurs in section, 700~900 DEG C of combustion tail gas can be generated, particulate solid is heated so that solid granulates
The temperature of object reaches 500~600 DEG C.
Other feature and advantage of the utility model will be described in detail in subsequent specific embodiment part.
Description of the drawings
Attached drawing is to be used to provide a further understanding of the present invention, an and part for constitution instruction, and following
Specific implementation mode be used to explain the utility model together, but do not constitute limitations of the present invention.
Fig. 1 is a kind of structural schematic diagram of embodiment of fluidization gas-solid heat exchange device;
Fig. 2 is the structural schematic diagram of second of embodiment of fluidization gas-solid heat exchange device;
Fig. 3 is the flow diagram of sorbent reactions also original system.
Wherein:
1- loosens gas outlet;2- particulate matters flow into mouth;3- particles dispersion area;
4- heating tubes;5- thermal currents area;The outer fluidization regions 6-;
7- particle stream outlets;8- burning zones;9- loosens gas import;
10- combustion product gases export;11- filters;12- heat exchanging segments;
13- fuel gas entrances;14- adsorptive reactors;15- reducing/regenerating devices;
16- smoke inlets;17- adsorbent entrances;18- adsorbent outlets to be generated;
19- exhanst gas outlets;20- also Primordial Qi entrances;21- restores offgas outlet;
22- adsorbent entrances to be generated;23- reproducing adsorbents export;
24- adsorbent coolers;25- regenerators loosen gas entrance;
26- reproducing adsorbents export;27~31 be pipeline.
Specific implementation mode
Specific embodiment of the present utility model is described in detail below in conjunction with attached drawing.It should be understood that herein
Described specific implementation mode is only used for describing and explaining the present invention, and is not intended to restrict the invention.
In the utility model, if without specified otherwise, the top of container refers to the position of the 0-50% of container from top to bottom, is held
The lower part of device refers to the position of the 50-100% of container from top to bottom, refers to the 0-10% of container from top to bottom at the top of container
Position, the bottom of container refer to the position of the 90-100% of container from top to bottom.
Attached drawing 1 is a kind of structural schematic diagram of embodiment of fluidization gas-solid heat exchange device provided by the utility model, such as
Shown in attached drawing 1, fluidization gas-solid heat exchange device includes outside the heat exchanging segment 12 on top, the burning zone 8 of lower part and the circular heat exchanging segment
Outer fluidization regions 6, the heat exchanging segment 12 includes particle flow area and thermal current area 5, setting at the top of the particle flow area
Particulate matter flows into mouth 2 and loosens gas outlet 1, and the particle flow area bottom is communicated with the outer fluidization regions 6, and described is outer
Fluidization regions 6, which are equipped with, loosens gas import 9 and particle stream outlet 7, and 5 top of thermal current area is arranged combustion tail gas and exports 10,
The burning zone 8 is provided with fuel gas entrance 13.The bottom of the outer fluidization regions 6 surrounds 12 bottom of heat exchanging segment,
The burning zone 8 is communicated across outer fluidization regions 6 with the thermal current area 5.The top of outer fluidization regions 6 and the heat exchanging segment
12 closed fronts are located at the top of the heat exchanging segment at closing.The loosening gas exports 1 lower part and filter 11 is arranged, described
Particle flow area the loosening gas outlet 1 is connected to through filter 11.The filter can be porous ceramics, can also
It is porous sintered metal pipe, to this utility model, there is no limit.
The carrying out practically flow of heat exchanger provided by the utility model is as follows:
Adsorbent to be generated flows into mouth 2 by particulate matter and enters heat exchanging segment 12 in heat exchanger from fluidization gas-solid heat exchange device top
Particle flow area in.Air and fuel enter 8 lower part of burning zone from fuel gas entrance 13, and combustion reaction occurs in burning zone
The temperature of the combustion product gases of generation can be 700-900 DEG C, enter thermal current area 5 from the combustion product gases outlet at 8 top of burning zone
In the spent agent that is fluidized with the loosening gas in particle flow area exchange heat, heat exchange to 500-600 DEG C of spent agent is from particle logistics
Outlet 7 is sent out, and which part adsorbent to be generated is full of outer fluidization regions 6 under the advertising for loosening gas, the combustion product gases warp after heat exchange
It is handled through pipeline to follow-up desulphurization denitration after 10 discharge of combustion product gases outlet.
In attached embodiment shown in FIG. 1, the tube side that the heating tube 4 provides is for solid particle flow to be heated
By particle flow area, the shell side that the heating tube 4 and heat exchanging segment outer wall surround is thermal current area 5, the particle point
It is a round-like structure to dissipate area 3, and being uniformly distributed in shell side or tube side is flowed to for particulate matter.
In fluidization gas-solid heat exchange device provided by the utility model, when heating tube is arranged in heat exchanging segment, the heating
Pipe can be single heating tube, can also be more heating tubes arranged side by side.Cold medium can select heat to fluidize state formal operations
Carrier walks shell side, and solid particulate matter to be heated walks tube side, and heat carrier can also be selected to walk tube side, solid particulate matter to be heated
Walk shell side.It when solid particulate matter walks tube side, is preferably fluidized for convenience of particulate matter, enters conducive to particulate matter after heating and converged by particle
Collect area 6, preferably tube side uses one-pass operation, and heat smoke walks shell side, to make full use of heat, it is proposed that uses Multiple Pass Operation.
The internal diameter of the heat exchanger single tube is 5~200mm, more preferable 10~150mm, and specific single tube internal diameter is according to industry
Interior well known knowledge and specific industrial fact are determined.
In fluidization gas-solid heat exchange device provided by the utility model, preferably 6 bottom of outer fluidization regions forms and is turned under
Bent arc, more preferable outer fluidization regions bottom are spherical surface, are conducive to particulate matter storage, conveying after heating.
In use, the loosening gas is reducibility gas to fluidization gas-solid heat exchange device provided by the utility model
Or inert gas, one kind in hydrogen, carbon monoxide and hydro carbons containing 1-5 carbon atom of the reducibility gas or
It is several.The inert gas one or more of group 0 element, nitrogen, carbon dioxide and vapor in periodic table.
The spent agent promotes the preferred inert gas of gas.
The burning zone 8 is set to fluidization gas-solid heat exchange device lower part, is reacted for gas fuel burning, and described can
Combustion property gas can be the dry gas in natural gas, liquefied petroleum gas and oil plant.Heat smoke after burning enters shell side or tube side
Spent agent is heated, is exported and is discharged by combustion product gases after heating.The fuel gas entrance of burning zone setting can be one
Or multiple entrances, when using multiple fuel gas entrances, fuel and air can introduce burning zone through different entrances respectively
Inside reacted.
The loosening gas gas flow rate, particle density of the particulate matter in heat exchanger is according to row knowledge known in the industry
It is determined with specific industrial fact.
Attached drawing 2 is the structural schematic diagram of second of embodiment of fluidization gas-solid heat exchange device provided by the utility model,
Unlike attached drawing 1, the top of outer fluidization regions 6 and 12 closed front of heat exchanging segment are located at the heat exchange at closing
Section is from top to bottom at 70% position.
Attached drawing 3 is the flow diagram of sorbent reactions also original system.By attached drawing 3 as it can be seen that sorbent reactions also original system
Including the adsorptive reactor 14, above-mentioned fluidization gas-solid heat exchange device and reducing/regenerating device 15 being sequentially communicated, the adsorption reaction
14 bottom of device is provided with regenerated flue gas entrance 16, adsorbent entrance 17, and top is provided with adsorbent outlet 18 to be generated, regenerated flue gas
Outlet 19, the reducing/regenerating device 15 are provided with also Primordial Qi entrance 20, reduction offgas outlet 21, adsorbent entrance 22 to be generated and again
Raw adsorbent outlet 26, the adsorbent outlet to be generated 18 of the adsorptive reactor 14 and the fluidization gas-solid heat exchange device
Particulate matter flows into the connection of mouth 2, the particle stream outlet 7 of the fluidization gas-solid heat exchange device and the reducing/regenerating device 15
Adsorbent entrance 22 to be generated is connected to, reproducing adsorbent outlet 26 and the adsorptive reactor 14 of the reducing/regenerating device 15
Adsorbent entrance 17 is connected to.
Reducing gas may be used due to loosening gas (being referred to as promoting gas or fluidized gas) in heat exchanger, such as Fig. 3 institutes
Show, the reducing/regenerating device 15, which is also provided with, loosens gas entrance 25, and the loosening gas outlet 1 at the top of the heat exchanger can be with
The loosening gas entrance 25 of the reducing/regenerating device 15 is connected to, to improve the utilization rate for loosening gas.
Reduction adsorption agent (or being reproducing adsorbent) temperature after reduction is higher than the reaction temperature of adsorptive reactor, such as schemes
Shown in 3, the system is also provided with adsorbent cooler 24, and the reduction adsorption agent outlet 26 of the reducing/regenerating device 15 can
To be connected to the reduction adsorption agent entrance 17 of the adsorptive reactor 14 by the adsorbent cooler 24, thus by reducing agent
It is re-fed into adsorptive reactor 14 after being cooled to suitable temperature.
Illustrate the use of gas-solid heat exchange device in systems by taking flue gas desulfurization and denitrification reacts as an example below:
As shown in Fig. 3, adsorbent is added in the adsorptive reactor 14 of recirculating fluidized bed, pending flue gas is by inhaling
14 bottom of reaction enclosure device enters reactor, and adsorbent bed haptoreaction, the SO contained in adsorbing and removing flue gasXAnd NOX, only
Adsorptive reactor 14 is discharged in tail gas after change after conventional dedirt, and the operation temperature of adsorptive reactor 14 is at 200 DEG C or so.Absorption
Adsorbent to be generated afterwards, which is entered by pipeline 29 in heat exchanger, to be heated, and is loosened gas and is carried to spent agent by loosening gas entrance
It rises, forms fluidisation state operation, improve heat exchange efficiency.Gas is loosened by being delivered to reduction reaction by pipeline 31 after filter 11 leaves
15 bottom of device.The temperature of 2 bottom of heat exchanging segment and reduction reactor 15 is same or similar, at 500-600 DEG C.After heating
High-temperature adsorbing agent, which enters via pipeline 30 in reduction reactor 15, carries out reducing/regenerating, and reducibility gas is gone back by regenerator bottoms
Raw-gas entrance 20 is passed through, and reduction tail gas is after discharge reduction reactor 15 carries out after reducing gas outlet 21 carries out conventional dedirts
Continuous processing.Adsorbent after reduction is delivered to after adsorbent cooler 24 is cooled to adsorption reaction temperature and is delivered to absorption
Reactor 14 completes a cyclic process.
Claims (12)
1. a kind of fluidization gas-solid heat exchange device, which is characterized in that the burning zone (8) of heat exchanging segment (12), lower part including top and
Outer fluidization regions (6) outside the heat exchanging segment, the heat exchanging segment (12) includes particle flow area and thermal current area (5), institute
Setting particulate matter flows into mouth (2) and loosens gas outlet (1), the particle flow area bottom and institute at the top of the particle flow area stated
The outer fluidization regions (6) stated communicate, and the outer fluidization regions (6), which are equipped with, loosens gas import (9) and particle stream outlet (7), described
Thermal current area (5) top setting combustion tail gas export (10), the burning zone (8) is provided with fuel gas entrance (13).
2. fluidization gas-solid heat exchange device described in accordance with the claim 1, which is characterized in that the loosening gas exports (1) lower part
Filter (11) is set, and the particle flow area exports (1) through filter (11) the connection loosening gas.
3. fluidization gas-solid heat exchange device described in accordance with the claim 1, which is characterized in that the bottom of the outer fluidization regions (6)
The heat exchanging segment (12) bottom is surrounded, the burning zone (8) is communicated across outer fluidization regions (6) with the thermal current area (5).
4. according to any fluidization gas-solid heat exchange device in claim 1-3, which is characterized in that the outer fluidization regions
(6) top and described heat exchanging segment (12) closed front are located at the position of heat exchanging segment 0-80% from top to bottom at closing
It sets.
5. fluidization gas-solid heat exchange device according to claim 2, which is characterized in that the particle flow area includes top
Particle dispersion area (3) and an at least heating tube (4), particle dispersion area (3) the heated pipe (4) and the outflow
Change area (6) to communicate, the particulate matter flows into mouth (2) and loosens the top that gas outlet (1) is set to the particle dispersion area (3)
Portion.
6. fluidization gas-solid heat exchange device according to claim 5, which is characterized in that the internal diameter of the heating tube be 5~
200mm。
7. fluidization gas-solid heat exchange device according to claim 6, which is characterized in that the internal diameter of the heating tube be 10~
150mm。
8. fluidization gas-solid heat exchange device described in accordance with the claim 3, which is characterized in that the bottom of the outer fluidization regions (6)
For spherical surface.
9. fluidization gas-solid heat exchange device according to claim 2, which is characterized in that the filter (11) is porous ceramics
Or porous sintered metal pipe.
10. a kind of sorbent reactions also original system, which is characterized in that the system include the adsorptive reactor (14) being sequentially communicated,
Fluidization gas-solid heat exchange device described in any one of claim 1-8 and reducing/regenerating device (15), the adsorptive reactor
(14) bottom is provided with regenerated flue gas entrance (16), adsorbent entrance (17), and top is provided with adsorbent outlet to be generated (18), again
Raw exhanst gas outlet (19), the reducing/regenerating device (15) are provided with also Primordial Qi entrance (20), reduction offgas outlet (21), suction to be generated
Attached dose of entrance (22) and reproducing adsorbent outlet (26), the adsorbent outlet to be generated (18) of the adsorptive reactor (14) and institute
The particulate matter for the fluidization gas-solid heat exchange device stated flows into mouth (2) connection, the particulate matter outflow of the fluidization gas-solid heat exchange device
Mouth (7) is connected to the adsorbent entrance (22) to be generated of the reducing/regenerating device, and the regeneration of the reducing/regenerating device (15) is inhaled
Attached dose of outlet (26) is connected to the adsorbent entrance (17) of the adsorptive reactor (14).
11. sorbent reactions also original system according to claim 10, which is characterized in that the reducing/regenerating device (15) is also
It is provided with and loosens gas entrance (25), loosening gas outlet (1) and the reducing/regenerating device of the fluidization gas-solid heat exchange device
(15) loosening gas entrance (25) connection.
12. sorbent reactions also original system according to claim 10, which is characterized in that the system is additionally provided with absorption
The reproducing adsorbent outlet of agent cooler (24), the reducing/regenerating device (15) passes through the adsorbent cooler (24) and institute
State the adsorbent entrance connection of adsorptive reactor (14).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721586332.8U CN207996670U (en) | 2017-11-23 | 2017-11-23 | A kind of fluidization gas-solid heat exchange device and sorbent reactions also original system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721586332.8U CN207996670U (en) | 2017-11-23 | 2017-11-23 | A kind of fluidization gas-solid heat exchange device and sorbent reactions also original system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN207996670U true CN207996670U (en) | 2018-10-23 |
Family
ID=63836235
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201721586332.8U Active CN207996670U (en) | 2017-11-23 | 2017-11-23 | A kind of fluidization gas-solid heat exchange device and sorbent reactions also original system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN207996670U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2023226337A1 (en) * | 2022-05-23 | 2023-11-30 | 东南大学 | Oil-gas outlet anti-coking device and method for adsorption medium self-circulation regeneration |
-
2017
- 2017-11-23 CN CN201721586332.8U patent/CN207996670U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2023226337A1 (en) * | 2022-05-23 | 2023-11-30 | 东南大学 | Oil-gas outlet anti-coking device and method for adsorption medium self-circulation regeneration |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105727708B (en) | A kind of multicompartment fluidized bed two-part activated carbon/coke flue gas and desulfurizing and denitrifying system and method | |
| JP3742657B2 (en) | Fuel gas desulfurization method and apparatus | |
| CN101592449B (en) | Heat exchange method in reactivation process of flue gas desulfuration and denitrification adsorbent | |
| CN102580706A (en) | Heat exchange type active coke purifying and generating process system and heat exchange type active coke purifying and generating process method | |
| EP2902088B1 (en) | Carbon dioxide capturing apparatus | |
| CN102397784B (en) | Method for regenerating flue gas desulphurization and denitrification adsorbent by hydrogen sulfide-containing regeneration gas | |
| CN104039990A (en) | Process for producing direct reduced iron (DRI) utilizing gases derived from coal | |
| CN105316014A (en) | Method and system for pyrolyzing biomass | |
| CN101987295B (en) | Heat exchange method in regenerating process of flue gas desulfurization and denitrification adsorbent | |
| CN105944499B (en) | A kind of method that temp.-changing adsorption removes sulfur dioxide in industrial tail gas | |
| EP2954942B1 (en) | Carbon dioxide collection device | |
| CN205199299U (en) | Active burnt gas cleaning system | |
| JP2012030135A (en) | Regeneration tower for apparatus for dry discharge-gas treatment | |
| CN207996670U (en) | A kind of fluidization gas-solid heat exchange device and sorbent reactions also original system | |
| CN102316985B (en) | Apparatus for regenerating catalyst | |
| US10166502B2 (en) | Single compression system and process for capturing carbon dioxide | |
| CN105536515A (en) | Two-stage flue gas desulphurization and denitration system and treating method | |
| CN207872186U (en) | A kind of fluidization gas-solid heat exchange device and sorbent reactions also original system | |
| WO2022029887A1 (en) | Ironmaking system and ironmaking method | |
| CN202438327U (en) | Heat-exchange type active coke purification and regeneration system | |
| CN207872185U (en) | Fluidization gas-solid heat exchange device and sorbent reactions also original system | |
| CN102380360B (en) | Adsorption and regeneration method of flue gas desulfurization and denitrification adsorbent | |
| CN207478600U (en) | It is a kind of from pre- thermal fluidization gas-solid heater and sorbent reactions also original system | |
| CN106732822A (en) | A kind of catalyst regeneration device, method and system | |
| CN102380369B (en) | Method for exchanging heat in regenerating process of flue gas desulfurization and denitrification adsorbent |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |