CN106435077B - Blast furnace gas dry purification method and system - Google Patents
Blast furnace gas dry purification method and system Download PDFInfo
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- CN106435077B CN106435077B CN201611154112.8A CN201611154112A CN106435077B CN 106435077 B CN106435077 B CN 106435077B CN 201611154112 A CN201611154112 A CN 201611154112A CN 106435077 B CN106435077 B CN 106435077B
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- 238000000034 method Methods 0.000 title claims abstract description 124
- 238000000746 purification Methods 0.000 title claims abstract description 48
- 239000007789 gas Substances 0.000 claims abstract description 181
- 238000001179 sorption measurement Methods 0.000 claims abstract description 167
- 239000003463 adsorbent Substances 0.000 claims abstract description 68
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 57
- 239000001301 oxygen Substances 0.000 claims abstract description 57
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 57
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 49
- 230000003647 oxidation Effects 0.000 claims abstract description 48
- 230000008929 regeneration Effects 0.000 claims abstract description 45
- 238000011069 regeneration method Methods 0.000 claims abstract description 45
- 239000012159 carrier gas Substances 0.000 claims abstract description 42
- 238000003795 desorption Methods 0.000 claims abstract description 35
- 238000006243 chemical reaction Methods 0.000 claims abstract description 29
- 230000008569 process Effects 0.000 claims abstract description 25
- 238000006722 reduction reaction Methods 0.000 claims abstract description 23
- 238000002485 combustion reaction Methods 0.000 claims abstract description 17
- 239000012535 impurity Substances 0.000 claims abstract description 12
- 238000003860 storage Methods 0.000 claims description 35
- 238000010438 heat treatment Methods 0.000 claims description 21
- 239000003034 coal gas Substances 0.000 claims description 19
- 238000009825 accumulation Methods 0.000 claims description 17
- 238000010410 dusting Methods 0.000 claims description 15
- 230000005611 electricity Effects 0.000 claims description 11
- 238000010521 absorption reaction Methods 0.000 claims description 9
- 238000012545 processing Methods 0.000 claims description 9
- 239000012495 reaction gas Substances 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 8
- 239000012716 precipitator Substances 0.000 claims description 7
- 239000002594 sorbent Substances 0.000 claims description 7
- 239000011261 inert gas Substances 0.000 claims description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 5
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 5
- 238000005108 dry cleaning Methods 0.000 claims description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 4
- 239000002184 metal Substances 0.000 claims description 4
- 229910052751 metal Inorganic materials 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 239000002808 molecular sieve Substances 0.000 claims description 4
- 239000000741 silica gel Substances 0.000 claims description 4
- 229910002027 silica gel Inorganic materials 0.000 claims description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 4
- 238000010248 power generation Methods 0.000 claims description 3
- 238000012546 transfer Methods 0.000 claims description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 23
- 229910000069 nitrogen hydride Inorganic materials 0.000 abstract description 16
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 abstract description 10
- 239000000460 chlorine Substances 0.000 abstract description 10
- 229910052801 chlorine Inorganic materials 0.000 abstract description 10
- 229910021529 ammonia Inorganic materials 0.000 abstract description 9
- 239000000126 substance Substances 0.000 abstract description 9
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 8
- 238000011049 filling Methods 0.000 abstract description 3
- 230000009467 reduction Effects 0.000 abstract description 3
- 230000001172 regenerating effect Effects 0.000 abstract 1
- 229910052717 sulfur Inorganic materials 0.000 abstract 1
- 239000011593 sulfur Substances 0.000 abstract 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 21
- 239000002585 base Substances 0.000 description 19
- 229910002092 carbon dioxide Inorganic materials 0.000 description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 10
- 238000006298 dechlorination reaction Methods 0.000 description 9
- 239000000428 dust Substances 0.000 description 8
- 239000007921 spray Substances 0.000 description 8
- 239000005864 Sulphur Substances 0.000 description 7
- 239000003795 chemical substances by application Substances 0.000 description 7
- 238000005406 washing Methods 0.000 description 7
- 238000005530 etching Methods 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- 229910000831 Steel Inorganic materials 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000010959 steel Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 229910052742 iron Inorganic materials 0.000 description 3
- 230000007420 reactivation Effects 0.000 description 3
- 238000005200 wet scrubbing Methods 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 238000007605 air drying Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 229910052681 coesite Inorganic materials 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 229910052906 cristobalite Inorganic materials 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 150000002927 oxygen compounds Chemical class 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 229910052682 stishovite Inorganic materials 0.000 description 1
- 229910052905 tridymite Inorganic materials 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B7/00—Blast furnaces
- C21B7/22—Dust arresters
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B5/00—Making pig-iron in the blast furnace
- C21B5/06—Making pig-iron in the blast furnace using top gas in the blast furnace process
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Treating Waste Gases (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Industrial Gases (AREA)
Abstract
The invention provides a dry purification method and a dry purification system for blast furnace gas. The method adopts a chemical looping combustion reactor and two adsorption towers, heats carrier gas through heat release of chemical looping combustion reaction, further uses high-temperature carrier gas to desorb and regenerate adsorbent, and desorbed NH3And introducing the air into the chemical looping combustion reactor to perform reduction reaction with the oxidation state oxygen carrier, introducing the air into the chemical looping combustion reactor to perform oxidation regeneration process of the reduction state oxygen carrier after the desorption of the adsorbent in the adsorption tower is completed, and alternately adsorbing and regenerating by adopting two parallel adsorption towers to realize high-efficiency dry purification of the blast furnace gas. The invention can thoroughly remove harmful impurities such as ammonia, chlorine, sulfur and the like in blast furnace gas by filling basic oxide serving as an adsorbent in the adsorption tower, and can remove desorbed NH by additionally arranging a chemical-looping combustion reactor3Advanced treatment is carried out, and the reaction heat released by the reaction in the chemical-looping combustion reactor can provide heat for desorption and regeneration of the adsorbent.
Description
Technical field
The present invention relates to a kind of blast furnace gas dry purification method and system, belongs to smelting iron and steel and environmental protection technology is led
Domain.
Background technique
In recent years, the blast furnace gas of domestic iron and steel enterprises has generallyd use dry type dust settling pocket technique, brings greatly
Economic benefit and social benefit.But with the continuous accumulation of knowhow, discovery is when blast furnace gas is using dry type cloth successively
After bag dedusting, because containing the impurity such as ammonia, chlorine, sulphur in coal gas, there is a large amount of product in TRT system, pipe-line system and auxiliary device
Salt and etching problem, have brought tremendous economic losses to enterprise, while also significantly increasing the work of production maintenance personnel
Amount.Therefore, how the impurity such as ammonia in blast furnace gas, chlorine, sulphur efficiently to be removed, so slow down or solve salification and etching problem at
The problem of for iron and steel enterprise's urgent need to resolve.
Currently, industry mainly has wet scrubbing and dry adsorption agent using the scheme of the media such as more removing ammonia, chlorine, sulphur
Absorption.Wet scrubbing can only handle the gas after TRT, cause the salification problem of TRT serious, simultaneously as many steel enterprises
Industry send the impurity such as ammonia, chlorine contained by the blast furnace gas of hot-blast stove, sulphur unprocessed, leads to the blast furnace gas pipeline for sending hot-blast stove and sets
Have salification and corrosion phenomenon.Compared with wet scrubbing, dry adsorption agent adsorption and purification technology, which has, does not spray water, does not cool down, no
Generate the advantage in terms of the environmental protection and energy saving such as new pollution sources.However, dry adsorption agent at present mostly based on basic oxide, is adsorbed
Capacity is limited, and operation a period of time can fail, and external offer big energy is needed when cannot regenerate or regenerate.
Existing blast furnace gas dry dusting process flow as shown in Figure 1,1 stock gas of blast furnace through pipeline to enter dry method thick
Dust-extraction unit 2 and dry method refined dedusting device 3, the blast furnace gas after dry method dust are incorporated to purified gas after the power generation of power generator 7
Pipe network, if power generator (TRT) 7 is not run, then by being incorporated to clean coal gas pipe network after pressure regulation valve group 6.The existing blast furnace gas
Dry dedusting technology has the following disadvantages: (1) because containing the impurity such as ammonia, chlorine, sulphur, dry method rough dedusting and refined dedusting dress in coal gas
The above impurity component cannot be removed by setting, and there are a large amount of salifications and corrosion to ask in TRT system, pipe-line system and auxiliary device
Topic；(2) salification problem is due to NH3It is combined with HCl and generates NH4Cl, when temperature is reduced to 80 DEG C or so, ammonia salt is precipitated.
The dechlorination process flow of existing blast furnace gas dry dusting wet process as shown in Fig. 2, 1 stock gas of blast furnace through pipeline into
Enter dry method rough dedusting device 2 and dry method refined dedusting device 3, after the blast furnace gas after dry method dust is generated electricity by power generator 7
Into spray washing tower (for removing CO2) 5, spray removing is carried out to acid impurities in spray washing tower (for removing CO2) 5, the clear height producer gas by spraying washing tower (for removing CO2) 5 is incorporated to clean coal
Gas pipe network then sprays washing tower (for removing CO2) 5 by entering after pressure regulation valve group 6, then be incorporated to clean coal gas pipe network if power generator (TRT) 7 is not run.
The existing blast furnace gas dry dusting wet process dechlorination technique has the following disadvantages: (1) spraying washing tower (for removing CO2) and need to consume largely
Water and lye；(2) a large amount of brine waste can be generated, new pollution sources are generated；(3) because spray can reduce gas temperature, therefore
Spray washing tower (for removing CO2) purifies coal gas after can be only placed at TRT, causes TRT because not to NH3, chlorine is handled and salification problem is tight
Weight；In many enterprises, the impurity such as ammonia, chlorine as contained by the blast furnace gas for sending hot-blast stove, sulphur are unprocessed, cause to send hot-blast stove
Blast furnace gas pipeline and equipment have salification and corrosion phenomenon.
The dechlorination process flow of existing blast furnace gas dry dusting dry method as shown in figure 3,1 stock gas of blast furnace through pipeline into
Enter dry method rough dedusting device 2 and dry method refined dedusting device 3, the blast furnace gas after dry method dust is passed through adsorption tower 4, in adsorption tower
Fill adsorbent, adsorbent by 20% basic activated group below be grouped as, the purified gas after being adsorbed by adsorbent passes through hair
Electric installation 7 enters purified gas pipe network after generating electricity, if power generator (TRT) 7 is not run, then by being incorporated to clean coal after pressure regulation valve group 6
Gas pipe network.The existing blast furnace gas dry dusting dry method dechlorination technique has the following disadvantages: the dry adsorption agent of filling
Adsorption capacity is limited, can fail after running a period of time, such as abandons or fills spent sorbent, replacement novel sorbents, will cause
The secondary pollution of environment, and purification device operation expense can be greatly improved.
Existing blast furnace gas dry dusting dry method dechlorination technique-reproducible process flow of adsorbent is as shown in figure 4, height
1 stock gas of furnace enters dry method rough dedusting device 2 and dry method refined dedusting device 3 through pipeline, the blast furnace gas after dry method dust
Be passed through adsorption tower 4, fill adsorbent in adsorption tower, adsorbent by 20% basic activated group below be grouped as, pass through adsorbent
Purified gas after absorption enters purified gas pipe network after generating electricity by power generator 7 and then passes through if power generator (TRT) 7 is not run
Clean coal gas pipe network is incorporated to after pressure regulation valve group 6.After adsorbent adsorption saturation, pass through generate regeneration carrier gas heating device 8
100~500 DEG C of superheated steams or 300~700 DEG C of high-temperature flue gas/coal gas are passed through in adsorption tower 4 as high temperature carrier gas, high temperature carrier gas
Can by dry adsorption agent acidic materials and dust etc. separate, regenerate dry adsorption agent and reuse.This is existing
Blast furnace gas dry dusting dry method dechlorination technique-reproducible technique of adsorbent have the following disadvantages: select alkali formula oxygen
Compound is as adsorbent, after adsorbent adsorption saturation, need to generate 100~500 DEG C of superheated steams or 300 with carrier gas heating device
~700 DEG C of high-temperature flue gas/coal gas is passed through in adsorption tower as high temperature carrier gas, by the foreign gas and dust in dry adsorption agent
Etc. separating, make adsorbent reactivation and reuse.Therefore, larger energy is needed during the adsorbent reactivation in this technology
Consumption.
Since current blast furnace gas dry purification process is there are above-mentioned various defects, this field is badly in need of grinding
Issue a kind of novel blast furnace gas dry purification method and system.
Summary of the invention
To solve the above-mentioned problems of the prior art, the purpose of the present invention is to provide a kind of purifications of blast furnace gas dry
Method and system.
In order to achieve the above objectives, present invention firstly provides a kind of blast furnace gas dry purification methods comprising following step
It is rapid:
(1) make from blast furnace roof be discharged blast furnace gas sequentially enter dry method rough dedusting device and dry method refined dedusting device into
After row dust removal process；Making the foreign gas in the coal gas after dedusting into the first adsorption tower (mainly includes NH3, HCl etc.) by
Adsorbent absorption in one adsorption tower；Then enter gas pipe after so that the gas after adsorption-edulcoration is generated electricity by power generator
Net, by entering gaspipe network after pressure regulation valve group if power generator is not run；
(2) when the adsorbent adsorption saturation in the first adsorption tower, make from blast furnace roof be discharged blast furnace gas successively into
Enter dry method rough dedusting device and after dry method refined dedusting device is dusted processing；Into second absorption in parallel with the first adsorption tower
Tower makes the foreign gas in the coal gas after dedusting (mainly include NH3, HCl etc.) adsorbed by the adsorbent in the second adsorption tower；So
Enter gaspipe network after so that the gas after adsorption-edulcoration is generated electricity by power generator afterwards, passes through if power generator is not run
Enter gaspipe network after pressure regulation valve group；
High temperature carrier gas is set to enter the first adsorption tower of adsorption saturation for adsorbent NH simultaneously3Desorption comes out, and makes to take off
The attached NH come out3Reduzate is generated into reduction reaction is carried out with oxidation state oxygen carrier therein in burning chemistry chains reactor
Gas (mainly including nitrogen, vapor and carbon dioxide) simultaneously releases heat；
(3) after the adsorbent wholly or largely desorption and regeneration in the first adsorption tower, stopping is passed through high temperature load thereto
Gas, the cooling of the first adsorption tower natural cooling；Make air or oxygen-enriched air enter in burning chemistry chains reactor with reduction therein
State oxygen carrier carries out oxidation regeneration reaction and generates oxidation product gas and release heat；
When the reduction-state oxygen carrier in burning chemistry chains reactor is wholly or largely oxidized regeneration, stop thereto
It is passed through air or oxygen-enriched air；
(4) when the adsorbent adsorption saturation in the second adsorption tower, make from blast furnace roof be discharged blast furnace gas successively into
Enter dry method rough dedusting device and after dry method refined dedusting device is dusted processing；It is again introduced into the first adsorption tower to be adsorbed, make
After gas after adsorption-edulcoration is generated electricity by power generator or by entering gaspipe network after pressure regulation valve group；
Desorption and regeneration is carried out to the adsorbent in the second adsorption tower simultaneously, the step of the desorption and regeneration and the step is related to
Reduction reaction process and oxidation regeneration reaction process in burning chemistry chains reactor is and to the adsorbent in the first adsorption tower
The step of carrying out desorption and regeneration is identical；
Make the first adsorption tower and the second adsorption tower alternating sorbent and regeneration, realizes the dry cleaning of blast furnace gas.
In above-mentioned blast furnace gas dry purification method, it is preferable that the high temperature carrier gas be make carrier gas by storage heater into
Obtained from row heating, the temperature of the high temperature carrier gas is 350~450 DEG C；And the reduction of the burning chemistry chains reactor
Product gas after the storage heater accumulation of heat with oxidation product gas by emptying, and the burning chemistry chains reactor is at the 1st time
It is set to be heated to 300~450 DEG C (first as a heat transfer medium and by heating device with inert gas (such as nitrogen) when operation
Heating temperature can be relatively low when secondary operation, has exothermic heat of reaction during subsequent reactions and elevates the temperature), the indifferent gas after heating
Body after the storage heater accumulation of heat by emptying.The present invention no setting is required carrier gas heating device, but burning chemistry chains is used to react
The reaction heat that combustion reaction in device releases comes for storage heater accumulation of heat, and then heats carrier gas；In burning chemistry chains reactor the 1st
When secondary operation, first it is passed through inert gas thereto while passing through heating device, it is heated, and then make the inert gas after heating
Pass through storage heater accumulation of heat；High temperature carrier gas after being heated by storage heater is desorbed adsorbent to obtain NH3, the NH3Entering
It learns in chain combustion reactor, at this time without being heated to burning chemistry chains reactor, the NH3Included temperature and oxidation therein
State oxygen carrier carries out reduction reaction and generates reduzate gas and release heat；In the burning chemistry chains reactor carried out later
The desorption and regeneration process of adsorbent is not necessarily to additionally heat again in oxidation regeneration reaction process and two adsorption towers.
In above-mentioned blast furnace gas dry purification method, it is preferable that into the dedusting of the first adsorption tower or the second adsorption tower
The temperature of coal gas afterwards is 90~200 DEG C；It is highly preferred that into the coal gas after the dedusting of the first adsorption tower or the second adsorption tower
Temperature is 90~120 DEG C.That is, the temperature adsorbed in adsorption tower is 90~200 DEG C, preferably 90~120 DEG C.
In above-mentioned blast furnace gas dry purification method, it is preferable that in first adsorption tower and second adsorption tower
Adsorbent respectively include in basic oxide or basic oxide and active carbon, silica gel, activated alumina and molecular sieve etc.
One or more of mixtures.First adsorption tower can be identical with the adsorbent in the second adsorption tower, can also slightly not
Together, as long as containing basic oxide.
In above-mentioned blast furnace gas dry purification method, it is preferable that in first adsorption tower and second adsorption tower
Adsorbent desorption and regeneration be 300~400 DEG C carry out.
In above-mentioned blast furnace gas dry purification method, it is preferable that the oxygen carrier packet in the burning chemistry chains reactor
Include the combination of one or more of Cu base load oxysome, Fe base load oxysome and Ni base load oxysome etc..Oxygen carrier is defined as: changing
It learns in chain combustion reaction, is known as oxygen carrier for transmitting the soild oxide of oxygen；Mainly there is the load such as Cu base, Ni base, Fe base, Ca base
Oxysome.By taking Cu base load oxysome as an example, generally CuO is active component, with Al2O3、SiO2It is prepared Deng for inert carrier.More
Preferably, the oxygen carrier in the burning chemistry chains reactor is Cu base load oxysome, the oxidation state oxygen carrier of Cu base load oxysome
The reaction of the oxidation regeneration of reduction reaction and reduction-state oxygen carrier is exothermic reaction, this is advantageous to come with the reaction heat of itself
Reaction temperature needed for maintaining reduction process and oxidative regeneration process, and to provide continuous heat when adsorbent desorption and regeneration
Amount.In processing NH3Reaction in, the oxidation state and NH of Cu base load oxysome3Reduction reaction and reduction-state and O2Oxidation again
The reaction equation and reaction heat of raw reaction are as follows:
3CuO+2NH3(g)=3Cu+N2(g)+3H2O (g) △ H=-40.81kcal/mol；
2Cu+O2(g)=2CuO △ H=-73.41kcal/mol.
In above-mentioned blast furnace gas dry purification method, it is preferable that the oxidation state in the burning chemistry chains reactor carries
The reduction reaction of oxysome is carried out at 400~500 DEG C, the reaction of the oxidation regeneration of reduction-state oxygen carrier be 450~500 DEG C into
Capable.
In above-mentioned blast furnace gas dry purification method, it is preferable that the reduction-state oxygen carrier in burning chemistry chains reactor
When 2% can be reached for the oxygen volumetric concentration in oxidation product gas by being wholly or largely oxidized regenerated judgment criteria.
In above-mentioned blast furnace gas dry purification method, it is preferable that the dry method rough dedusting device and the dry method essence are removed
Dirt device is respectively bag filter, electric precipitator, metal dusting device or sinter-plate precipitator.
The present invention provides a kind of novel blast furnace gas dry purification methods.This method will contain the impurity such as ammonia, chlorine first
Dedusting after blast furnace gas be passed through in adsorption tower, so that adsorbent is adsorbed NH therein3With the impurity such as HCl, to realize blast furnace coal
The purification of gas；Then carrier gas is heated by the heat release of combustion process in burning chemistry chains reaction, and then is carried using high temperature
The attached reproducing adsorbent of qi exhaustion；NH after desorption3It is passed into burning chemistry chains reactor and is restored with oxidation state oxygen carrier
Reaction generates N2、H2O and CO2, because the oxidability of oxidation state oxygen carrier is markedly less than O2, and reduction reaction temperature control exists
400~500 DEG C, therefore NO or NO is not had2Reaction；When completion is wholly or largely desorbed in the adsorbent in adsorption tower
Afterwards, air or oxygen-enriched air are passed through in burning chemistry chains reactor by the switching of valve group, carry out the oxygen of reduction-state oxygen carrier
Change regenerative process；And two adsorption tower alternating sorbents in parallel and regeneration are used, realizes the efficient dry cleaning of blast furnace gas.
The present invention also provides a kind of blast furnace gas dry purification system, which is included at least: dry method rough dedusting device,
Dry method refined dedusting device, the first adsorption tower, the second adsorption tower and burning chemistry chains reactor；
The blast furnace gas outlet of blast furnace roof is sequentially connected to dry method rough dedusting device by pipeline and dry method refined dedusting fills
It sets, the gas exit after the dedusting of dry method refined dedusting device passes through pipeline respectively and is connected to the first adsorption tower and the second adsorption tower tower
The gas entry at bottom；The tower top of first adsorption tower and the second adsorption tower passes through pipeline respectively and is connected to power generator and tune in parallel
Pressure valve group connects gaspipe network in turn；
The tower top of first adsorption tower and the second adsorption tower is also respectively provided with high temperature carrier gas and enters pipeline, the first adsorption tower and
The tower bottom of second adsorption tower is also respectively provided with desorption NH3Outlet conduit；Two desorption NH3Outlet conduit is all connected to chemical chain
The reduction reaction gas access of combustion reactor is additionally provided with reduzate gas vent on burning chemistry chains reactor, should be also
It is connected with air on the pipeline of former product gas outlet or oxygen-enriched air enters pipeline, i.e., burning chemistry chains reactor is also original
Object gas vent is also oxidation regeneration reaction gas inlet, and the reduction reaction gas access of burning chemistry chains reactor is also
Oxidation product gas outlet；And heating device is provided on burning chemistry chains reactor；
Adsorbent is filled in first adsorption tower and the second adsorption tower；Oxygen carrier is filled in burning chemistry chains reactor
Body.
Blast furnace gas dry purification system of the invention is the system that above-mentioned blast furnace gas dry purification method uses.
Specific embodiment according to the present invention, it is preferable that above-mentioned blast furnace gas dry purification system further includes storage heater,
It is provided with carrier gas on the storage heater and enters pipeline, and the oxidation product gas of the burning chemistry chains reactor is exported and gone back
Former product gas outlet is connected to the storage heater by pipeline come for its accumulation of heat, the high temperature after storage heater heating is carried
Gas enters pipeline by the high temperature carrier gas that high temperature carrier gas outlet is connected to the first adsorption tower and the second absorption column overhead, and
Product gas outlet pipeline is additionally provided on the storage heater for emptying as the oxidation product gas after its accumulation of heat and also originating in
Object gas.
In a specific embodiment of the invention, above-mentioned blast furnace gas dry purification system can also include motor-driven valve and/
Or electronic valve group, these motor-driven valves and/or electronic valve group can be separately positioned on the first adsorption tower, the second adsorption tower, chemical chain
On the entrance and/or outlet conduit of one or several devices in combustion reactor and storage heater etc., in order to switch adsorption tower
In adsorption process and reduction reaction process and oxidation regeneration reaction process in desorption and regeneration process, burning chemistry chains reactor
Deng.
In above-mentioned blast furnace gas dry purification system, it is preferable that in first adsorption tower and second adsorption tower
Adsorbent respectively include in basic oxide or basic oxide and active carbon, silica gel, activated alumina and molecular sieve etc.
One or more of mixtures.First adsorption tower can be identical with the adsorbent in the second adsorption tower, can also slightly not
Together, as long as containing basic oxide.
In above-mentioned blast furnace gas dry purification system, it is preferable that the oxygen carrier packet in the burning chemistry chains reactor
Include the combination of one or more of Cu base load oxysome, Fe base load oxysome and Ni base load oxysome etc.；It is highly preferred that the chemical chain
Oxygen carrier in combustion reactor is Cu base load oxysome.
In above-mentioned blast furnace gas dry purification system, it is preferable that the dry method rough dedusting device and the dry method essence are removed
Dirt device is respectively bag filter, electric precipitator, metal dusting device or sinter-plate precipitator.
Blast furnace gas dry purification method and system provided by the invention can mainly be brought following the utility model has the advantages that (1) sheet
Invention in adsorption tower by filling the meetings such as ammonia, chlorine, sulphur that basic oxide can be removed thoroughly as adsorbent in blast furnace gas
To the objectionable impurities for causing equipment salification and etching problem, and specific embodiment according to the present invention, pass through test purification
The pH value of blast furnace gas condensate water afterwards finds that its pH value is 6~8, it was demonstrated that chlorinity < 5mg/Nm in purified blast furnace gas3,
Fundamentally solve the salification and etching problem of TRT device, pipe-line system and equipment etc.；(2) present invention has installed chemical chain additional
Combustion reactor, can be by the NH of desorption3Advanced treating, and no setting is required carrier gas heating device are carried out, it is anti-in burning chemistry chains
Answer the oxygen carrier and NH in device3Reduction reaction process and the oxidation regeneration reaction process of oxygen carrier be exothermal reaction process,
The reaction heat released can provide heat for the desorption and regeneration of adsorbent, significantly reduce the energy of adsorbent reactivation process
Consumption；(3) present invention uses two adsorption tower alternating sorbents and regeneration, realizes the efficient dry cleaning of blast furnace gas.
Detailed description of the invention
Fig. 1 is existing blast furnace gas dry dusting process flow chart；
Fig. 2 is existing blast furnace gas dry dusting wet process dechlorination process flow chart；
Fig. 3 is existing blast furnace gas dry dusting dry method dechlorination process flow chart；
Fig. 4 is existing blast furnace gas dry dusting dry method dechlorination technique-reproducible process flow chart of adsorbent；
Fig. 5 is the process flow of blast furnace gas dry purification method and system that the embodiment of the invention provides
Figure；
Primary clustering symbol description:
Blast furnace 1, dry method rough dedusting device 2, dry method refined dedusting device 3, adsorption tower 4, spray washing tower (for removing CO2) 5, pressure regulation valve group 6, power generation
Device 7, heating device 8, the first adsorption tower 401, the second adsorption tower 402, the first adsorbent 410, the second adsorbent 420, first
Motor-driven valve 501, the second motor-driven valve 502, third motor-driven valve 503, the 4th motor-driven valve 504, the 5th motor-driven valve 505, the 6th motor-driven valve
506, the 7th motor-driven valve 507, the 8th motor-driven valve 508, the 9th motor-driven valve 509, the tenth motor-driven valve 510, the 11st motor-driven valve 511,
Burning chemistry chains reactor 9, oxygen carrier 901, storage heater 10, first circulation blower 11, second circulation blower 12.
Specific embodiment
In order to which technical characteristic of the invention, purpose and beneficial effect are more clearly understood, now to skill of the invention
Art scheme carries out described further below, but should not be understood as that limiting the scope of the invention.
Embodiment 1
A kind of blast furnace gas dry purification system is present embodiments provided, as shown in figure 5, the system includes: that dry method is slightly removed
Dirt device 2, dry method refined dedusting device 3, the first adsorption tower 401, the second adsorption tower 402, burning chemistry chains reactor 9, storage heater
10, first circulation blower 11 and second circulation blower 12；
The blast furnace gas of 1 furnace roof of blast furnace, which is exported, is sequentially connected to dry method rough dedusting device 2 and dry method refined dedusting by pipeline
Device 2, the gas exit after the dedusting of dry method refined dedusting device 3 pass through pipeline respectively and are connected to the first adsorption tower 401 and second
The gas entry of 402 tower bottom of adsorption tower；The tower top of first adsorption tower 401 and the second adsorption tower 402 is connected to by pipeline respectively
Power generator 7 and pressure regulation valve group 6 in parallel connects gaspipe network in turn；And the gas entry pipe of 401 tower bottom of the first adsorption tower
The first motor-driven valve 501 is provided on road, 401 tower top of the first adsorption tower is connected to the pipe of power generator 7 and pressure regulation valve group 6 in parallel
The second motor-driven valve 502 is provided on road；It is provided with the 5th motor-driven valve 505 on the gas entry pipeline of second adsorption tower, 402 tower bottom,
Second adsorption tower, 402 tower top is connected on the pipeline of power generator 7 and pressure regulation valve group 6 in parallel and is provided with the 6th motor-driven valve 506；
The tower bottom of first adsorption tower 401 and the second adsorption tower 402 is also respectively provided with desorption NH3Outlet conduit, and the
The desorption NH of one adsorption tower, 401 tower bottom3The 4th motor-driven valve 504, the desorption of 401 tower bottom of the second adsorption tower are provided on outlet conduit
NH3The 8th motor-driven valve 508 is provided on outlet conduit；Two desorption NH3Outlet conduit is all connected to burning chemistry chains reactor 9
Reduction reaction gas access, be additionally provided with reduzate gas vent on burning chemistry chains reactor 9, the reduzate gas
Outlet is connected to storage heater 10 by pipeline, and the position on the pipeline close to storage heater 10 is provided with the 11st motor-driven valve
511；And air or oxygen-enriched air enter pipeline and are connected to the pipeline by threeway, i.e., burning chemistry chains reactor is also original
Object gas vent is also oxidation regeneration reaction gas inlet, enters on pipeline that be provided with the 9th electronic in the air or oxygen-enriched air
Valve 509 and second circulation blower 12, and the reduction reaction gas access of burning chemistry chains reactor is also oxidation product gas
Outlet, oxidation product gas outlet are connected by the pipeline that pipeline and threeway are connect with reduzate gas vent and storage heater 10
It is logical, and the tenth motor-driven valve 510 is provided on the pipeline that oxidation product gas outlet is connect with storage heater 10；
The tower top of first adsorption tower 401 and the second adsorption tower 402 is also respectively provided with high temperature carrier gas and enters pipeline；Storage heater
It is additionally provided with carrier gas on 10 and enters pipeline, and enters on pipeline in the carrier gas and is provided with first circulation blower 11；Burning chemistry chains
The oxidation product gas outlet of reactor 9 and reduzate gas vent are connected to storage heater 10 by pipeline to store for it
Heat, the high temperature carrier gas after the heating of storage heater 9 are connected to the first adsorption tower 401 and the second absorption by high temperature carrier gas outlet
The high temperature carrier gas of 402 tower top of tower enters pipeline, and the high temperature carrier gas of 401 tower top of the first adsorption tower enters on pipeline and is provided with
Three motor-driven valves 503, the high temperature carrier gas of 402 tower top of the second adsorption tower, which enters on pipeline, is provided with the 7th motor-driven valve 507；The accumulation of heat
Product gas outlet pipeline is additionally provided on device to be used to empty as the oxidation product gas and reduzate gas after its accumulation of heat；
It is filled with the first adsorbent 410 in first adsorption tower 401, is filled with the second adsorbent in the second adsorption tower 402
420；It is provided with heating device 8 on burning chemistry chains reactor 9, oxygen carrier 901 is filled in burning chemistry chains reactor 9.
In the blast furnace gas dry purification system of the present embodiment, in first adsorption tower and second adsorption tower
Adsorbent respectively includes one in basic oxide or basic oxide and active carbon, silica gel, activated alumina and molecular sieve etc.
Kind or several mixtures.First adsorption tower can be identical with the adsorbent in the second adsorption tower, also can be somewhat different from that,
As long as containing basic oxide；Preferably, the adsorbent in the first adsorption tower and the second adsorption tower is the oxidation of alkali formula
Object.Oxygen carrier in the burning chemistry chains reactor includes in Cu base load oxysome, Fe base load oxysome and Ni base load oxysome etc.
One or more of combinations；Preferably, the oxygen carrier in the burning chemistry chains reactor is Cu base load oxysome.The dry method is thick
Dust-extraction unit and the dry method refined dedusting device are respectively bag filter, electric precipitator, metal dusting device or sintered plate dedusting
Device.
Embodiment 2
Present embodiments provide a kind of blast furnace gas dry purification method, the blast furnace coal that this method uses embodiment 1 to provide
Air drying purification system, as shown in figure 5, itself the following steps are included:
(1) blast furnace gas being discharged from 1 furnace roof of blast furnace is made to sequentially enter dry method rough dedusting device 2 and dry method refined dedusting device
3 are dusted processing；The first motor-driven valve 501 and the second motor-driven valve 502 are opened, about 90~200 after making dedusting DEG C (preferably 90
~120 DEG C) coal gas enter the first adsorption tower 401 with by NH therein3, the foreign gases such as HCl are by the first adsorption tower 401
The absorption of first adsorbent 410, wherein the adsorption process of HCl is based on chemisorption, NH3Adsorption process be with physical absorption
It is main；Then enter gaspipe network after so that the gas after adsorption-edulcoration is generated electricity by power generator 7, if power generator 7 is not transported
It is capable then by entering gaspipe network after pressure regulation valve group 6；
(2) when the first 410 adsorption saturation of adsorbent in the first adsorption tower 401, the first motor-driven valve 501 and second is closed
Motor-driven valve 502 opens the 5th motor-driven valve 505 and the 6th motor-driven valve 506, make the blast furnace gas being discharged from 1 furnace roof of blast furnace successively into
Enter dry method rough dedusting device 2 and after dry method refined dedusting device 3 is dusted processing, into parallel with the first adsorption tower 401
Two adsorption towers 402 make the NH in the coal gas of about 90~200 DEG C (preferably 90~120 DEG C) after dedusting3, the foreign gases such as HCl
It is adsorbed by the second adsorbent 420 in the second adsorption tower 402；Send out the gas after adsorption-edulcoration by power generator 7
Enter gaspipe network after electricity, by entering gaspipe network after pressure regulation valve group 6 if power generator 7 is not run；
Meanwhile third motor-driven valve 503, the 4th motor-driven valve 504 and the 11st motor-driven valve 511 are opened, and open first circulation
Blower 11 makes carrier gas be heated to obtain 350~450 DEG C of high temperature carrier gas by storage heater 10, which is to pass through chemistry
Chain combustion reactor 9 adds it as a heat transfer medium and with heating device 8 with inert gas (such as nitrogen) in the 1st operation
Heat to 300~450 DEG C and accumulation of heat, the first adsorption tower 401 which enters adsorption saturation inhales the first adsorbent 410
Attached NH3Desorption comes out, the NH for coming out desorption3Into in burning chemistry chains reactor 9 with oxidation state oxygen carrier 901 therein
Reduction reaction is carried out to generate reduzate gas (mainly including nitrogen, vapor and carbon dioxide) and release heat, chemical chain
The reduzate gas of combustion reactor 9 empties after passing through 10 accumulation of heat of storage heater；
(3) after the first 410 wholly or largely desorption and regeneration of adsorbent in the first adsorption tower 401, stop first and follow
Ring blower 11 closes third motor-driven valve 503 and the 4th motor-driven valve 504, is carried with stopping being passed through high temperature into the first adsorption tower 401
Gas, the cooling of 401 natural cooling of the first adsorption tower；Second circulation blower 12, the 9th motor-driven valve 509 and the tenth motor-driven valve 510 are opened,
Enter air or oxygen-enriched air anti-with reduction-state oxygen carrier 901 therein progress oxidation regeneration in burning chemistry chains reactor 9
Oxidation product gas should be generated and release heat, the oxidation product gas of burning chemistry chains reactor 9 passes through 10 accumulation of heat of storage heater
After empty；
When the reduction-state oxygen carrier 901 in burning chemistry chains reactor 9 is wholly or largely oxidized regeneration, that is, aoxidize
When oxygen volumetric concentration in product gas reaches 2%, stops second circulation blower 12, closes the 9th motor-driven valve 509 and the tenth
Motor-driven valve 510, to stop being passed through air or oxygen-enriched air into burning chemistry chains reactor 9；
(4) when the second 420 adsorption saturation of adsorbent in the second adsorption tower 402, the 5th motor-driven valve 505 and the 6th is closed
Motor-driven valve 506 opens the first motor-driven valve 501 and the second motor-driven valve 502, make the blast furnace gas being discharged from 1 furnace roof of blast furnace successively into
Enter dry method rough dedusting device 2 and after dry method refined dedusting device 3 is dusted processing；The first adsorption tower 401 is again introduced into be inhaled
It is attached, make the gas after adsorption-edulcoration after generating electricity by power generator 7 or by entering gaspipe network after pressure regulation valve group 6；
Desorption and regeneration is carried out to the second adsorbent 420 in the second adsorption tower 402 simultaneously, i.e. the 7th motor-driven valve 507 of opening
With the 8th motor-driven valve 508, and opening first circulation blower 11 makes carrier gas be heated to obtain 350~450 DEG C by storage heater 10
DEG C high temperature carrier gas, which enters the NH that the second adsorption tower 402 of adsorption saturation adsorbs the second adsorbent 4203It is de-
NH that is attached to come out, coming out desorption3It is restored into burning chemistry chains reactor 9 with oxidation state oxygen carrier 901 therein
Reaction generates reduzate gas (mainly including nitrogen, vapor and carbon dioxide) and releases heat, burning chemistry chains reaction
The reduzate gas of device 9 empties after passing through 10 accumulation of heat of storage heater；
(5) after the second 420 wholly or largely desorption and regeneration of adsorbent in the second adsorption tower 402, stop first and follow
Ring blower 11 closes the 7th motor-driven valve 507 and the 8th motor-driven valve 508, is carried with stopping being passed through high temperature into the second adsorption tower 402
Gas, the cooling of 402 natural cooling of the second adsorption tower；Second circulation blower 12, the 9th motor-driven valve 509 and the tenth motor-driven valve 510 are opened,
Enter air or oxygen-enriched air anti-with reduction-state oxygen carrier 901 therein progress oxidation regeneration in burning chemistry chains reactor 9
Oxidation product gas should be generated and release heat, the oxidation product gas of burning chemistry chains reactor 9 passes through 10 accumulation of heat of storage heater
After empty；
When the reduction-state oxygen carrier 901 in burning chemistry chains reactor 9 is wholly or largely oxidized regeneration, that is, aoxidize
When oxygen volumetric concentration in product gas reaches 2%, stops second circulation blower 12, closes the 9th motor-driven valve 509 and the tenth
Motor-driven valve 510, to stop being passed through air or oxygen-enriched air into burning chemistry chains reactor 9；
Make the first adsorption tower 401 and 402 alternating sorbent of the second adsorption tower and regeneration, realizes the dry cleaning of blast furnace gas.
The pH value of blast furnace gas condensate water after test purification finds that its pH value is 6~8, it was demonstrated that purified blast furnace gas
Middle chlorinity < 5mg/Nm3, fundamentally solve the salification and etching problem of TRT device, pipe-line system and equipment etc..
Claims (10)
1. a kind of blast furnace gas dry purification method comprising following steps:
(1) blast furnace gas being discharged from blast furnace roof is made to sequentially enter dry method rough dedusting device and dry method refined dedusting device is removed
After dirt processing；Adsorb the foreign gas in the coal gas after dedusting by the adsorbent in the first adsorption tower；
Then enter gaspipe network after so that the gas after adsorption-edulcoration is generated electricity by power generator, lead to if power generator is not run
Enter gaspipe network after crossing pressure regulator valve group；
(2) when the adsorbent adsorption saturation in the first adsorption tower, sequentially enter the blast furnace gas being discharged from blast furnace roof dry
After method rough dedusting device and dry method refined dedusting device are dusted processing；Make into second adsorption tower in parallel with the first adsorption tower
The foreign gas in coal gas after dedusting is adsorbed by the adsorbent in the second adsorption tower；Then make the gas after adsorption-edulcoration logical
Enter gaspipe network after crossing power generator power generation, by entering gaspipe network after pressure regulation valve group if power generator is not run；
High temperature carrier gas is set to enter the first adsorption tower of adsorption saturation for adsorbent NH simultaneously3Desorption comes out, and comes out desorption
NH3Reduzate gas is generated simultaneously into reduction reaction is carried out with oxidation state oxygen carrier therein in burning chemistry chains reactor
Release heat；
The high temperature carrier gas is obtained from heating carrier gas as storage heater, the temperature of the high temperature carrier gas is 350~
450℃；And the reduzate gas of the burning chemistry chains reactor passes through the storage heater with oxidation product gas and stores
It is emptied after heat, the burning chemistry chains reactor is filled in the 1st operation with inert gas as a heat transfer medium and by heating
Setting makes it be heated to 300~450 DEG C, and the inert gas after heating after the storage heater accumulation of heat by emptying；
(3) after the adsorbent wholly or largely desorption and regeneration in the first adsorption tower, stopping is passed through high temperature carrier gas thereto, the
The cooling of one adsorption tower natural cooling；Make air or oxygen-enriched air enter in burning chemistry chains reactor with reduction-state oxygen carrier therein
Body carries out oxidation regeneration reaction and generates oxidation product gas and release heat；
When the reduction-state oxygen carrier in burning chemistry chains reactor is wholly or largely oxidized regeneration, stopping is passed through thereto
Air or oxygen-enriched air；
(4) when the adsorbent adsorption saturation in the second adsorption tower, sequentially enter the blast furnace gas being discharged from blast furnace roof dry
After method rough dedusting device and dry method refined dedusting device are dusted processing；It is again introduced into the first adsorption tower to be adsorbed, make through inhaling
After gas after attached removal of impurities is generated electricity by power generator or by entering gaspipe network after pressure regulation valve group；
Desorption and regeneration is carried out to the adsorbent in the second adsorption tower simultaneously, the step of the desorption and regeneration and chemistry that the step is related to
Reduction reaction process and oxidation regeneration reaction process in chain combustion reactor are carried out with to the adsorbent in the first adsorption tower
The step of desorption and regeneration, is identical；
Make the first adsorption tower and the second adsorption tower alternating sorbent and regeneration, realizes the dry cleaning of blast furnace gas.
2. blast furnace gas dry purification method according to claim 1, wherein enter the first adsorption tower or the second adsorption tower
Dedusting after coal gas temperature be 90~200 DEG C.
3. blast furnace gas dry purification method according to claim 2, wherein enter the first adsorption tower or the second adsorption tower
Dedusting after coal gas temperature be 90~120 DEG C.
4. blast furnace gas dry purification method according to claim 1, wherein first adsorption tower and described second is inhaled
Adsorbent in attached tower respectively includes basic oxide or basic oxide and active carbon, silica gel, activated alumina and molecular sieve
One or more of mixture.
5. blast furnace gas dry purification method according to claim 1, wherein first adsorption tower and described second is inhaled
Adsorbent desorption and regeneration in attached tower is carried out at 300~400 DEG C.
6. blast furnace gas dry purification method according to claim 1, wherein the load in the burning chemistry chains reactor
Oxysome includes the combination of one or more of Cu base load oxysome, Fe base load oxysome and Ni base load oxysome.
7. blast furnace gas dry purification method according to claim 6, wherein the load in the burning chemistry chains reactor
Oxysome is Cu base load oxysome.
8. blast furnace gas dry purification method according to claim 1, wherein the oxygen in the burning chemistry chains reactor
The reduction reaction for changing state oxygen carrier is carried out at 400~500 DEG C, the reaction of the oxidation regeneration of reduction-state oxygen carrier be 450~
500 DEG C progress.
9. blast furnace gas dry purification method according to claim 1, wherein the dry method rough dedusting device and described dry
Method refined dedusting device is respectively bag filter, electric precipitator, metal dusting device or sinter-plate precipitator.
10. a kind of blast furnace gas dry purification system, the system include at least: dry method rough dedusting device, dry method refined dedusting device,
First adsorption tower, the second adsorption tower and burning chemistry chains reactor, storage heater；
The blast furnace gas of blast furnace roof, which is exported, is sequentially connected to dry method rough dedusting device and dry method refined dedusting device by pipeline, does
Gas exit after the dedusting of method refined dedusting device passes through pipeline respectively and is connected to the first adsorption tower and the second adsorption tower tower bottom
Gas entry；The tower top of first adsorption tower and the second adsorption tower passes through pipeline respectively and is connected to power generator and pressure regulator valve in parallel
Group and then connection gaspipe network；
The tower top of first adsorption tower and the second adsorption tower is also respectively provided with high temperature carrier gas and enters pipeline, the first adsorption tower and second
The tower bottom of adsorption tower is also respectively provided with desorption NH3Outlet conduit；Two desorption NH3Outlet conduit is all connected to burning chemistry chains
The reduction reaction gas access of reactor is additionally provided with reduzate gas vent on burning chemistry chains reactor, this is also originated in
It is connected with air on the pipeline of object gas vent or oxygen-enriched air enters pipeline, i.e. the reduzate gas of burning chemistry chains reactor
Body outlet is also oxidation regeneration reaction gas inlet, and the reduction reaction gas access of burning chemistry chains reactor is also oxidation
Product gas outlet；And heating device is provided on burning chemistry chains reactor；
Adsorbent is filled in first adsorption tower and the second adsorption tower；Oxygen carrier is filled in burning chemistry chains reactor；
It is provided with carrier gas on the storage heater and enters pipeline, and the oxidation product gas outlet of the burning chemistry chains reactor
The storage heater is connected to come the height for its accumulation of heat, after storage heater heating by pipeline with reduzate gas vent
Warm carrier gas enters pipeline by the high temperature carrier gas that high temperature carrier gas outlet is connected to the first adsorption tower and the second absorption column overhead,
And the oxidation product gas and go back that product gas outlet pipeline is used to empty for after its accumulation of heat are additionally provided on the storage heater
Former product gas.
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| CN107385128B (en) * | 2017-09-15 | 2023-04-11 | 中冶赛迪工程技术股份有限公司 | Blast furnace gas spraying deacidification method and device without reducing gas heat value |
| CN111214928B (en) * | 2018-11-26 | 2021-09-14 | 中国科学院大连化学物理研究所 | Factory waste gas treatment system containing ammonia gas |
| CN110252068A (en) * | 2019-07-15 | 2019-09-20 | 湖北申昙环保新材料有限公司 | The desulfurizing and purifying method of blast furnace gas |
| CN110252070A (en) * | 2019-07-15 | 2019-09-20 | 湖北申昙环保新材料有限公司 | The purification method of blast furnace gas |
| CN110252069A (en) * | 2019-07-15 | 2019-09-20 | 湖北申昙环保新材料有限公司 | The sulfur method of blast furnace gas |
| CN110657416A (en) * | 2019-10-28 | 2020-01-07 | 中国能源建设集团陕西省电力设计院有限公司 | Power generation system utilizing blast furnace gas |
| CN115786607B (en) * | 2022-11-15 | 2024-03-26 | 中冶赛迪工程技术股份有限公司 | Blowing method and system |
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