CN1391979A - Flue gas desulfuring method and its device for density current fluidised bed - Google Patents
Flue gas desulfuring method and its device for density current fluidised bed Download PDFInfo
- Publication number
- CN1391979A CN1391979A CN 02121361 CN02121361A CN1391979A CN 1391979 A CN1391979 A CN 1391979A CN 02121361 CN02121361 CN 02121361 CN 02121361 A CN02121361 A CN 02121361A CN 1391979 A CN1391979 A CN 1391979A
- Authority
- CN
- China
- Prior art keywords
- fluidized
- flue gas
- bed reactor
- bed
- desulfurizing
- 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.)
- Granted
Links
Images
Abstract
The present invention relates to the desulfurizing of gas containing sulfur oxide exhausted in industrial process and aims at providing flue gas desulfurizing device with low cost, simple structure and easy maintenance. Sulfur containing flue gas is made to enter to the fluidized reactor from bottom, desulfurizing slurry is made to enter to the reactor from the top, and flue gas is forced to pass through large particle coagulating area comprising large particle bed material and calcium hydroxide and the suspension area comprising calcium hydroxide particle, so that desulfurizing agent and SO2 can contact in sufficient time and space for full chemical reaction. The present invention has high desulfurizing efficiency and high desulfurizing agent utilization.
Description
Technical field:
The present invention relates to contain in the industrial process emission gases desulfuration field of oxygen sulfur compound gas.
Background technology:
Recirculating fluidized bed is the important reaction units of industry such as chemical industry, power, building materials, and being used to carry out flue gas desulfurization is in the eighties in last century.Though the stack gas desulfurization system of circulating fluid bed of exploitation is through multiple improvement both at home and abroad, but do not break away from original technical conceive all the time, it promptly is reactor with the recirculating fluidized bed, system is except that blower fan, also need water pump, air compressor, lime slurry pump, the desulfurizing agent injection equipment, cyclone separator, flying dust feeds back mechanism, not only system is still very complicated, the lime white nozzle performance that is adopted is bigger to the desulfurized effect influence, directly influence mixing of sorbent particle and flue gas, in case nozzle wear, the lime white jeting effect will be had a greatly reduced quality, desulfurized effect also will obviously descend, thereby maintenance workload will be very big also.
" combustion science and technology ", 2001, in the literary composition of 7 (3) pp228～232 " the normal temperature circulating fluid bed flue-gas desulfurizing influences the parameter and the mechanism of desulfuration efficiency ", introduced the circulating fluid bed flue-gas desulfurizing research of carrying out on the recirculating fluidized bed testing stand of diameter 280mm, high 6000mm, the primary structure of testing stand is: the air that comes from air blast mixes SO through after the electrical heating
2, enter from the recirculating fluidized bed bottom; As desulfurizing agent, desulfurizing agent injects the recirculating fluidized bed bottom with the lime white form through atomizing, with SO in the flue gas with white lime
2Reaction; Cyclone separator is arranged on the recirculating fluidized bed outlet, and flying dust that separates and desulfurizing agent are sent recirculating fluidized bed back to through the L valve.This desulfurization method, the quality of desulfurizing agent atomizing is very big to the desulfuration efficiency influence, and the desulfuration efficiency of this test is all less than surpassing 80%.The desulfurizing agent fogging degree has determined desulfurizing agent and SO
2Exposure level, and good mixing is the factor of flue gas desulfurization most critical with contacting." coal-fired sulfur dioxide pollution control handbook (Hao Jiming etc., Chemical Industry Press 2001.4) when touching upon domestic circulating fluid bed flue-gas desulfurizing technology, writes: the experimental study of some units at present, " also have a certain distance apart from industrial implementation, still have many problems not solve ".Open question mainly contains that desulfuration efficiency is low, sorbent utilization is low, system complex, operating cost is higher and maximize or the like, makes these technology industrialization promotion not use.And other kind flue gas desulfur devices or because cost an arm and a leg as rotary spraying technique etc., are equivalent to 0.5～1 boiler price that is complementary, perhaps because the technology shortcoming, as in-furnace calcium spraying etc., desulfuration efficiency is low, generally is not more than 40%, sorbent utilization is low generally is not more than 30%.Mei Xiaoyan etc. (power engineering, 2001.10,21 volume No. 5) point out when introducing the wet desulphurization device of China oneself exploitation, and wet flue gas desulfurization device flue gas with water, temperature drop are serious etc., and shortcoming is very difficult is accepted by the domestic market.
The country that carries out circulating fluid bed flue-gas desulfurizing abroad mainly is Germany and Denmark.Germany Lurgi company and Wulff company all adopts flue gas to enter recirculating fluidized bed by the bottom, and and then atomization water immediately after flue gas enters spray into limestone slurry; And desulfurizing agent is at first made mortar by the FLS.Miljo company of Denmark, and the recirculating fluidized bed bottom is a Venturi tube, and flue gas enters below Venturi tube, and lime white mixes the back and sprays at Venturi tube aditus laryngis place with water, compressed air, and nozzle is a patented technology.Owing to adopt compressed air and water-aspirator pressure to come the atomizing of reinforcing desulfuration agent, contact with the mixing of flue gas though improved desulfurizing agent, also therefore and complicated, operating cost obviously improves in system.
Summary of the invention:
It is high and lacked by Technological Economy such as operating temperature restriction to the present invention is directed to industrial process flue gas desulfurization technique commercial price costliness, system complex, operating cost, adopt different weight fluidized bed flue gas desulfurization method, develop flue gas desulfur device with low cost, simple in structure, easy to maintenance, improve desulfuration efficiency and sorbent utilization.
Method of the present invention is: the sulfur-containing smoke gas of being discharged by burner boosts to 6000～10000pa as fluidizing gas through air blast; Blast fluidized-bed reactor from the bottom bellows of fluidized-bed reactor with the import velocity of flue gas of 1-8 meter per second; The desulfurizing agent feed opening of sending into the fluidized-bed reactor top by slurry pump from the desulfurizing agent slurry of desulfurizing agent mortar pool enters reactor; Bed material in the bulky grain accumulation regions of fluidized-bed reactor bottom is made up of bulky grain quartz sand or limestone particle.Slurry bulk desulfurizing agent falls from reactor head, under the desiccation of the strike of bulky grain bed material and flue gas, is broken down into little slurry group and is ground into individual particle.Flue gas forms sweetening process with bed material and sorbent particle even contact.The main component of lime stone is a calcium carbonate, becomes calcium hydroxide after making pulpous state, and under the effect of fluidizing gas and bulky grain bed material, the thickness particle reaches fully and mixes, and forms the different weight fluidized-bed desulfurizer that bulky grain bed material and fine grained calcium hydroxide are formed.After the calcium hydroxide fine grained occurred, under the effect of flue gas, the parts of fine particle was gone out fluid bed bulky grain accumulation regions by elutriation, becomes suspended particulate in the suspension reaction section.Therefore, the sweetening process of whole fluid bed is made up of two parts, and thick calcium hydroxide particle layer is as the phase I of desulfurization in the bulky grain accumulation regions in the fluid bed, and the suspension calcium hydroxide particle in the suspension reaction section is as the second stage of desulfurization.Because flue gas mixes with desulfurizing agent fully, the time of staying is long, sorbent utilization and desulfuration efficiency all are greatly improved.
Adopt the different weight fluidized bed flue-gas desulfurizing device of this method, form by air blast 1, bellows 2 and air distribution plate 3, bulky grain accumulation regions 4, suspended particulate district 5, wall 6, exhanst gas outlet 7, mortar pool 8, slurry pump 9, feed opening 10, fluidized-bed reactor 11, gas-solid separator 12, material returning device 13 and respective line.Bellows 2 are equipped with in fluidized-bed reactor 11 bottoms, connect with air blast 1 by exhaust gases passes, and fluidized-bed reactor 11 upper ends one side is provided with exhanst gas outlet 7, and the top is by 1～16/m
2Evenly arrange feed opening 10, feed opening 10 connects slurry pump 9, and the other end of slurry pump 9 inserts in the mortar pool 8.The top air distribution plate 3 of bellows 2 is provided with scum pipe 18, and the operating pressure of fluidized-bed reactor 11 is reconciled by scum pipe 18 discharging bed material.When boiler tonnage during greater than 4t/h, in order to strengthen the fragmentation of bulky grain bed material to desulfurizing agent slurry group, the bottom of fluidized-bed reactor 11 is made cone lower joint pin body structure into, and lower joint pin body number arranged side by side is determined according to the flue gas treating capacity.45-70 ° of the cone angle of flare, cylinder vertical height 400～800mm.Air blast extracts flue gas and enters fluidized-bed reactor as fluidizing agent by air distribution plate, and bulky grain bed materials flowization is got up; Desulfurizing agent slurry group is dripped by the fluidized-bed reactor top, slurry group falls after the bulky grain fluid bed, under the desiccation of oarse-grained strike and flue gas, become little slurry group by big slurry group, become calcium hydroxide particle by little slurry group again, when granularity changed, the chemical reaction that sulfur in smoke and calcium hydroxide take place removed the calcium dioxide in the flue gas.
The invention has the advantages that: 1. device is simple.Do not need equipment such as other make-up water pump, air compressor and desulfurizing agent nozzle, therefore reduced operating cost yet.2. cheap.Whole fluidized-bed reactor is made by the common building material, except that fluidized-bed reactor needs the abrasionproof corrosion-proof lining, without any other specific (special) requirements.3. maintenance is simple, operating cost is cheap.Because the desulphurization system working mechanism is simple, does not have special construction and parts, does not need special care and maintenance.Do not have the desulfurizing agent nozzle simultaneously, just do not have mechanical breakdowns such as nozzle wear, obstruction yet.Operating cost mainly is reflected in 4. sulphur efficiencies and sorbent utilization height such as sorbent consumption, power consumption, personal expenditures.Because flue gas must pass the bulky grain accumulation regions of bulky grain bed material and calcium hydroxide composition and the floating zone that calcium hydroxide particle is formed, desulfurizing agent and sulfur dioxide have sufficient time of contact and enough attaching spaces, be enough to guarantee sufficient chemical reaction takes place, improved desulfuration efficiency and sorbent utilization effectively.Desulfuration efficiency can reach between 85～99%.
Description of drawings:
Fig. 1 is the different weight fluidized bed flue-gas desulfurizing device for the configuration of 4t/h boiler.
Fig. 2 is the different weight fluidized bed flue-gas desulfurizing device for the configuration of 10t/h boiler.
Fig. 3 is that different weight fluidized bed flue-gas desulfurizing device and steam generator system link schematic diagram.
The specific embodiment:
Fig. 1 is the different weight fluidized bed flue-gas desulfurizing device for the configuration of 4t/h boiler.After the flue gas that boiler is discharged boosts to 6000Pa through air blast, enter fluidized-bed reactor with the bed materials flowization, pass by quartzy casting bed material and calcium hydroxide particle form different weight fluidized-bed, carry a part of calcium hydroxide fine grained and proceed desulphurization reaction in the suspension space, this moment, calcium to sulphur mole ratio was 1.5, and desulfuration efficiency is 98%.Reactor is made up of machine-processed common brick, steelframe, corrosion protective lining; Air distribution plate is made up of corrosion resistant plate and stainless (steel) wire, and the percent opening of corrosion resistant plate is 5%, loses for preventing a materials flow, installs stainless (steel) wire below air distribution plate additional, and the steel mesh specification is a condition not allow the bed material to pass distribution grid.The fluid bed interface dimensions is 0.96 * 0.96m
2, height for reactor 4m, operation fluidizing velocity 2.5m/s, the lime white nozzle is circular, effective diameter 25mm, totally 16.
Fig. 2 is the flue gas desulfur device of 10t/h boiler configuration, and the fluid bed lower dimension is 1.25 * 0.96m
2, lower vertical section height 0.55m, the reactor angle of flare 60 degree, height for reactor 4m, bottom operating air velocity 5.8m/s, the top interface dimensions is 1.25 * 1.40m
2, top operating air velocity 4m/s.The lime white nozzle is circular, and effective diameter is 33mm.Adapted CLPG-9.4 type cyclone separator, import velocity of flue gas 12m/s, running resistance 500pa, separative efficiency 90%, calcium to sulphur mole ratio is 1.1, desulfuration efficiency is 86%.
Fig. 3 is that different weight fluidized bed flue-gas desulfurizing device and steam generator system link schematic diagram.Under flue valve 14 closed conditions, the flue gas that boiler 19 is discharged is under the effect of air blast 1, enter different weight fluidized bed desulfurization reactor 11, reacted cleaning flue gases enters deduster 15 through cyclone separator 12 and cleaning flue gases passage, under the effect of air-introduced machine 16, enter atmosphere via chimney 17.When desulfurizer need overhaul, open the flue valve 14 on the by-pass flue, flue gas enters atmosphere after entering deduster 15 under the effect of air-introduced machine 16.
Adopt this connection, after flue valve 14 is closed, boiler room original system air-introduced machine is responsible for overcoming deduster 15 and the later running resistance of fluidized-bed reactor 11 suspension sections, air blast is responsible for overcoming the running resistance of bellows in the fluidized-bed reactor 11, air distribution plate and bulky grain accumulation regions, do not need to add air compressor and humidifier, system is greatly simplified, and operation and maintenance cost reduces significantly.In service, whole system all is the gas-solid flow process, and without any mechanical part, also just mechanical breakdowns such as not wearing and tearing, obstruction take place, and can guarantee security of system, continuous, efficient operation.
Claims (6)
1, a kind of different weight fluidized bed flue gas desulfurization method, boost to 6000～10000pa as fluidizing gas by the sulfur-containing smoke gas that burner is discharged through air blast, it is characterized in that, blast fluidized-bed reactor with the import velocity of flue gas of 1-8 meter per second from the bottom bellows of fluidized-bed reactor; The desulfurizing agent feed opening of sending into the fluidized-bed reactor top by slurry pump from the desulfurizing agent slurry of desulfurizing agent mortar pool enters reactor.
2, different weight fluidized bed flue gas desulfurization method as claimed in claim 1 is characterized in that, the bed material in the bulky grain accumulation regions of fluidized-bed reactor bottom is made up of bulky grain quartz sand or limestone particle.
3, a kind of device of implementing the method for claim 1, comprise fluidized-bed reactor (11), it is characterized in that, bellows (2) are equipped with in fluidized-bed reactor (11) bottom, connect with air blast (1) by exhaust gases passes, fluidized-bed reactor (11) upper end one side is provided with exhanst gas outlet (7), and top feed opening (10) connects slurry pump (9), and the other end of slurry pump (9) inserts in the mortar pool (8).
4,, it is characterized in that fluidized-bed reactor (11) top is by 1～16/m as right 3 described devices
2Evenly arrange feed opening (10).
As right 3,4 described devices, it is characterized in that 5, the bottom of fluidized-bed reactor (11) also can be cone lower joint pin body structure, lower joint pin body number arranged side by side is determined according to the flue gas treating capacity, 45-70 ° of the cone angle of flare, cylinder vertical height 400～800mm.
As right 3,4 described devices, it is characterized in that 6, the top air distribution plate (3) of bellows (2) is provided with scum pipe (18).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02121361 CN1199713C (en) | 2002-06-17 | 2002-06-17 | Flue gas desulfuring method and its device for density current fluidised bed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02121361 CN1199713C (en) | 2002-06-17 | 2002-06-17 | Flue gas desulfuring method and its device for density current fluidised bed |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1391979A true CN1391979A (en) | 2003-01-22 |
| CN1199713C CN1199713C (en) | 2005-05-04 |
Family
ID=4744935
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 02121361 Expired - Fee Related CN1199713C (en) | 2002-06-17 | 2002-06-17 | Flue gas desulfuring method and its device for density current fluidised bed |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1199713C (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100372596C (en) * | 2005-01-13 | 2008-03-05 | 清华大学 | Method and device for removing coal fire discharged absorptive particles and precursor thereof |
| CN102297439A (en) * | 2011-07-05 | 2011-12-28 | 哈尔滨工业大学 | Ultra-low temperature smoke-exhausting and energy-saving boiler |
-
2002
- 2002-06-17 CN CN 02121361 patent/CN1199713C/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100372596C (en) * | 2005-01-13 | 2008-03-05 | 清华大学 | Method and device for removing coal fire discharged absorptive particles and precursor thereof |
| CN102297439A (en) * | 2011-07-05 | 2011-12-28 | 哈尔滨工业大学 | Ultra-low temperature smoke-exhausting and energy-saving boiler |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1199713C (en) | 2005-05-04 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100518890C (en) | Efficient desulfurizing and dust collecting process of boiler for circulating fluidized bed | |
| CN101357298A (en) | Circulating fluid bed flue gas desulfurization technique and device | |
| CN101653682A (en) | Boiler-rear flue gas desulphurization and synergism device of circulating fluid bed boiler and desulphurization and synergism method | |
| CN100467100C (en) | Circulating suspension state dried method desulfurizing technology and special purpose desulfurizing tower thereof | |
| CN106422539A (en) | Desulfurization and dust removal combined process and system for biomass power plant | |
| CN100490948C (en) | Twin tower circulating fluidized bed fume desulfurizing method and device | |
| CN101703886B (en) | Desulfuration method by directly utilizing magnesium slags in circulating fluidized bed boiler | |
| CN201427021Y (en) | Flue gas desulfurization device for digestive and circulating fluidized bed | |
| CN201085994Y (en) | Circulation fluidized bed smoke desulphurizing device | |
| CN105327602A (en) | Floating glass melting furnace flue gas waste heat utilization and denitration purification treatment device | |
| CN206295800U (en) | A kind of semi-dry flue gas desulfurization device | |
| CN201389423Y (en) | Flue gas desulphurization dust removing tower for coal burning boiler | |
| CN1199713C (en) | Flue gas desulfuring method and its device for density current fluidised bed | |
| CN202438257U (en) | Gas-solid circulating flue gas absorption desulfuration and dust removal device | |
| CN102350211B (en) | Three-stage desulfurization device for circulating fluidized bed boiler | |
| CN1425491A (en) | Composite Circulation fluidized dry desulfurization process for flue gas and desalfurizing reaction tower | |
| CN201257361Y (en) | Flue gas desulphurization device | |
| CN2277815Y (en) | Composite purifier for self-exciting water-bath fluidized bed | |
| CN1196517C (en) | Compound cycle typed fluidized technique in dry-process of stack gas desulfurization and desulphurisation reaction tower with high performance | |
| CN201421186Y (en) | High-efficiency energy-saving emission-reducing organic heat carrier boiler of circulating fluidize bed | |
| CN113559692A (en) | Double-tower double-circulation semi-dry desulfurization device, process and application | |
| CN102512943B (en) | Smoke desulfurization tower with smashing device | |
| CN2503367Y (en) | Granite wet-type five-grade desulfurization dust control device | |
| CN2524819Y (en) | Semi dry type fume desulfurizing and dust-removing integrated device with solid and gas recirculation | |
| CN2708986Y (en) | High efficient spiral type spraying dust separation desulfur device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |