CN1892106A - Coal-tar powder combustion method and apparatus - Google Patents
Coal-tar powder combustion method and apparatus Download PDFInfo
- Publication number
- CN1892106A CN1892106A CN 200510080800 CN200510080800A CN1892106A CN 1892106 A CN1892106 A CN 1892106A CN 200510080800 CN200510080800 CN 200510080800 CN 200510080800 A CN200510080800 A CN 200510080800A CN 1892106 A CN1892106 A CN 1892106A
- Authority
- CN
- China
- Prior art keywords
- bed
- coke powder
- heat
- gas
- mixer
- 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
Landscapes
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The invention provides a coke powder combusting method, comprising: combusting the coke powder in order through low-speed bed and high-speed bed at 0.3-3m/s and 3-25m/s, respectively; separating the combusted coke powder from gas through gas-solid separator and making the solid powder enter in heat-absorbing fluidized bed to reduce the temperature of the solid powder; making the solid powder enter in mixing segment and mix with fresh coke powder, and entering in circulating combustion again; thus, it can completely combust coke powders of different sizes and its combusting efficiency and sulfur-fixing rate are both largely improved.
Description
Technical field
The invention belongs to coal chemical technology, specifically, relate to and a kind ofly can improve the combustion method of coke powder combustion rate and sulfur-fixing rate and the equipment that this method adopted.
Background technology
The annual coke powder that produces a large amount of high sulfur-bearings of China, this coke powder can't efficiently utilize because of sulfur-bearing is high, present gasification combustion method and used equipment make and to burn that not only efficient is lower, and the flue gas that produces behind the gasification, and combustion becomes the source of atmosphere pollution, formation acid rain again because of the sulfur-bearing height.
The combustion desulfurization experiment of coke powder shows: have amount of sulfur contenting in smoke height, easy slagging scorification, initiation temperature height during (1) coke powder gasification, and combustion, burn the temperature height, burn rate is slow, and the active combustion time is longer, characteristics such as combustibility difference.(2) coke powder burning presents significantly process stage by stage, and the phase I burns easily, and initiation temperature is with to burn temperature lower, and burn rate is very fast, and burning time is shorter; Second stage burning difficulty, initiation temperature is with to burn temperature higher, and burn rate is slower, and burning time is longer; And along with the increase of particle diameter, the initiation temperature of coke powder and burn temperature and increase, increase burning time, and burn rate reduces.(3) coke powder burning and solid sulphur are simultaneous two processes, and burning largely is inconsistent with the optimum target of solid sulphur.High combustion speed is fast more more for temperature for burning, treating capacity is big more, the increase time of staying can make the coke powder burn rate accelerate, treating capacity increases, increase the time of contact of sulfur-containing smoke gas and sulphur-fixing agent, and sulfur-fixing rate increases, but time of staying increase can make the one way quantity combusted increase again simultaneously, amount of sulfur contenting in smoke increases, and sulfur-fixing rate reduces.Therefore, adopt suitable gasification combustion method and equipment, realize that efficient, the clean gasifying burning of coke powder is the difficult problem that present urgent need solves.
In existing field, be called the flow regime (bubbling bed, turbulent bed) of gas speed lower (approximately 1.5m/s is following) low speed bed, higher (about 1.5～16m/s) flow regime is called fast bed, carries bed and the flow regime of gas speed higher (approximately 15m/s more than) is called with gas speed.Carry bed to be usually used in the catalytic cracking of oil.According to the flow regime of coke powder in the combustion chamber, advanced at present coke powder gasification combustion method can be divided into: 1) low speed bed combustion method; 2) fast bed or conveying bed combustion process.There are pluses and minuses separately in two kinds of combustion systems: (1) low speed bed combustion method has that an endoparticle concentration is big, back-mixing is more, the particle time of staying is long, efficiency of carbon con version and the more high factor of gasification efficiency help the coke powder gasification, and combustion, but less because of operating gas velocity in the bed again simultaneously, recycle ratio is less etc., and factor is unfavorable for the coke powder gasification, and combustion; (2) fast bed or carry that bed combustion process has that operating gas velocity is higher, recycle ratio is big, the sulphur-fixing agent consumption is less, gas-solid ratio and all more high factor of gas yield help the coke powder gasification, and combustion, but less because of back-mixing again simultaneously, particle time of staying calorific value short, that the unit mass coal produced is lower etc., and factor is unfavorable for the coke powder gasification, and combustion; (3) when low speed bed burning, granule density is big, back-mixing is big, the gas-solid time of staying is longer, increase the time of contact of sulfur-containing smoke gas and sulphur-fixing agent, sulfur-fixing rate increases, but particle one way amount of burnt is also bigger simultaneously, and amount of sulfur contenting in smoke is bigger, sulfur-fixing rate is lower, and the overstand of more incendive granule in bed occupied the useful space of burner, and treating capacity reduces; When fast bed or the burning of conveying bed, granule density is less, back-mixing is less, the gas-solid time of staying is shorter, particle one way amount of burnt is less, amount of sulfur contenting in smoke is less, and sulfur-fixing rate increases, but also reduce the time of contact of while sulfur-containing smoke gas and sulphur-fixing agent, sulfur-fixing rate reduces, and the time of staying of bulky grain in bed than difficult to burn is too short, does not fully burn, and efficiency of combustion is lower.Therefore, present combustion method is because be independent use, so the characteristics that both existed some to help the coke powder clean combustion all exist some to be unfavorable for the characteristics of coke powder clean combustion again.
Summary of the invention
The present invention is directed to two kinds of deficiencies that coke powder clean combustion method all exists commonly used at present, developed the method and apparatus of the coke powder clean combustion of a kind of suitable coke powder burning and solid sulphur characteristics, that this method both can guarantee was long than the time of staying of coke powder coarse granule in bed of difficult to burn, back-mixing is more, can make again the more incendive time of staying of coke powder fine grained in bed short, back-mixing is less.
The object of the present invention is to provide a kind of combustion method of sulphur coal coke powder,, reached the coke powder efficiency of combustion height of high sulfur-bearing (high-sulfur), the solid good effect of sulphur by with coke powder order process fractional combustion and gas-solid separating device low speed bed and bed at a high speed.
The present invention also aims to provide a kind of equipment that can improve the coke powder efficiency of combustion, by bed at a high speed is set on low speed bed top, and be provided with at least one gas-solid separator, and make the burning of coke powder more complete, combustion rate and sulfur-fixing rate all are improved.
The objective of the invention is to realize by the following method:
The invention provides a kind of combustion method of coke powder, comprising: (1) described coke powder particle burns through low speed bed and high speed bed in proper order, and this low speed bed gas speed is 0.3～3m/s, and the gas speed of bed is 3～25m/s at a high speed; (2) particle after the burning separates through gas-solid separating device with gas, and solid particle enters in the heat-obtaining fluid bed; (3) solid particle that enters in the heat-obtaining fluid bed is lowered the temperature through heat-obtaining, enters mixer, mixes with initiate coke powder fresh granules, reenters the circulating combustion of step (1).
Said method of the present invention, both can make the more incendive time of staying of coke powder fine grained in bed short, back-mixing is less, make again long than the time of staying of coke powder coarse granule in bed of difficult to burn, back-mixing is more, reached all energy completing combustion of coke powder of different-grain diameter, the good effect that its efficiency of combustion and sulfur-fixing rate all are greatly improved.
Wherein coke powder particle described in the step (1) is through burning at mixer before low speed bed in the said method, and the gas speed of this mixer is 0.5～3m/s, and temperature is 600～750 ℃; Be separated into secondary cyclone described in the step (2) and separate, the particle after the described burning separates back (also can increase cyclone separator as required) with gas through secondary cyclone, and the coke powder particle enters the heat-obtaining fluid bed; Described solid particle the process after the heat-obtaining fluid bed of entering also comprises after the temperature (cooling) of reducing to mixer back-mixing again; Wherein low speed bed gas speed is 0.5～3m/s, and temperature is 750～850 ℃; The gas speed of bed is 6～20m/s at a high speed, and temperature is 850～1000 ℃.After particle after the described burning and gas carried out gas solid separation through the two stage cyclone separator respectively, the coke powder particle entered the heat-obtaining fluid bed; Preferably be provided with the heat-obtaining device that is used to lower the temperature on this heat-obtaining fluid bed, reduce to and enter mixer and fresh granules back-mixing circulating combustion again after the temperature of mixer so that be in the coke powder particle of the condition of high temperature after separating.
In order to realize the high performance clean burning of above-mentioned sulphur coal coke powder, the present invention also provides a kind of equipment of coke powder burning, comprise low speed bed, airduct and gas-solid separating device that low speed bed bottom connects, it is characterized in that, this equipment also is provided with mixer, high speed bed and heat-obtaining fluid bed, this mixer is connected in low speed bed bottom, its lower end is provided with airduct, this its cross section of high speed bed is less than low speed bed cross section and be connected in low speed bed top, its exit, upper end is provided with transverse tube and is connected with this heat-obtaining fluid bed by transverse tube, described gas-solid separating device is located at the top of this heat-obtaining fluid bed, the bottom of heat-obtaining fluid bed is provided with inlet valve, communicates with mixer by inlet valve.
Above-mentioned gas-solid separating device is at least one cyclone separator, this cyclone separator is positioned at the top of described heat-obtaining fluid bed, the lower end also is provided with dipleg, one end of this dipleg links to each other with the bottom port of cyclone separator, the other end is located in this heat-obtaining fluid bed, makes the particle after the separation enter this heat-obtaining fluid bed by this dipleg; Described gas-solid separating device is preferably two cyclone separators, and the exhaust outlet of one of them cyclone separator is connected with the import of another cyclone separator.
In order to improve sulphur coal coke powder efficiency of combustion, also be provided with the heat-obtaining device that is used to lower the temperature on the wherein said heat-obtaining fluid bed, can reduce near entering mixer and fresh granules back-mixing circulating combustion again after the mixer temperature so that be in the particle of high temperature after separating; The bottom is provided with discharge duct and airduct, is beneficial to discharging.Similarly, in order to improve the solid sulphur efficiency of sulphur coal coke powder combustion process, preferably in mixer, place sulphur-fixing agent (for example lime stone etc.), because its combustion process gas-solid time of staying of method of the present invention is longer, obviously increase the time of contact of sulfur-containing smoke gas and sulphur-fixing agent, therefore improved sulfur-fixing rate greatly.
In sum, mix the back by coke powder and air and in the combination CFBC device of described strong back-mixing, carry out, can reach the effect of efficient burning, efficiency of sulfur retention.
Coke powder combustion experiment of the present invention (experimental stage also claims hot experiment) is preferably finished in the combination recirculating fluidized bed of a cover steel, idiographic flow is: open fluidized wind and promote wind, screw feeder joins mixer continuously with coke powder particle and sulphur-fixing agent, the heating mixer is by the heat carrier coke powder particle that ignites of circulation, gas and coke powder burning particles and sulphur-fixing agent together move upward, be introduced into lower low speed bed of gas speed, move upward again and enter the higher high speed bed of gas speed, after transverse tube enters the heat-obtaining fluid bed, at the heat-obtaining fluid bed, gas and coke powder burning particles are realized gas solid separation through secondary cyclone, and simultaneously the coke powder burning particles that does not burn in the heat-obtaining fluid bed and heat carrier enter the ignite coke powder fresh granules that added by screw feeder and mixes the back with gas and make progress mobile of mixer again.
In a preferred embodiment, the parameter that records of the present invention is as follows:
The global cycle amount of the coke powder of hot experiment and heat carrier particle is 1159.5～3075kg/h, is entered into the coke powder and the heat carrier particle internal circulating load G of mixer by circulation pipe
S1Be 1148～3000kg/h, join coke powder fresh granules internal circulating load G in the mixer by screw feeder
S2Be 11.5～75kg/h, recycle ratio (G
S1+ G
S2With G
S2Ratio) be 41-101, operating gas velocity is mixer: 1.6m/s, low speed bed: 2.4m/s, high speed bed: 10m/s, heat-obtaining fluid bed: 0.6m/s, bed temperature are mixer: 550-650 ℃, bed outlet at a high speed: 850～860 ℃, the heat-obtaining fluid bed: 790～800 ℃, the burner general reserve is 570kg.
G
S1By inlet valve control, G
S2By screw feeder control, circulating ratio is controlled jointly by inlet valve and screw feeder, and operating gas velocity is controlled by flowmeter, and the heat-obtaining fluidized-bed temperature is controlled by external warmer.Particle mean concentration and pressure distribution adopt pressure transmitter measurement, and bed temperature is by thermocouple measurement, and burning back flue gas is formed employing GDX-104 type chromatographic column, 13-13X molecular sieve chromatography post and thermal conductance detection cell and measured jointly.
In another preferred embodiment of the present invention, operating gas velocity is: mixer 1.6m/s, low speed bed 2.4m/s, high speed bed 10m/s, heat-obtaining fluid bed 0.6m/s; Coke powder particle global cycle amount is 1159.5～3075kg/h, and recycle ratio is 41～101; The particle mean concentration is: mixer 188～372kg/m
3, low speed bed 118～321kg/m
3, high speed bed 20.3～84.6kg/m
3Bed temperature is: mixer 550-650 ℃, at a high speed the bed outlet is 850～860 ℃, 790～800 ℃ of heat-obtaining fluid beds, and coke powder efficiency of combustion and sulfur-fixing rate all can reach 99%, and efficiency of combustion of the prior art and sulfur-fixing rate be it is estimated and the highlyest reached 95% only.
The invention has the advantages that: the bed top is the high speed bed, and the bottom is low speed bed, and the coke powder particle carries out combustion desulfurization at two kinds of different beds of gas speed respectively.In the bed bottom, gas speed lower (0.5～3m/s), the particle entrainment amount is less, the coarse grained back-mixing of coke powder is more, burning time is longer, the fine grain back-mixing of coke powder is less, burning time is shorter, coarse grained one way amount of burnt is bigger, and fine grain one way amount of burnt is less, and amount of sulfur contenting in smoke is unlikely excessive, the time of contact of sulfur-containing smoke gas and sulphur-fixing agent (if sulphur-fixing agent is arranged) is longer, helps increasing burning and the solid sulphur efficiency of coke powder particle in the bed bottom.(the i.e. bed at a high speed at the bed top, because the cross section is less than low speed bed cross section, under the identical situation of tolerance, can improve and reach required gas speed), gas speed higher (6～20m/s), the particle entrainment amount is bigger, recycle ratio is bigger, granule density is less, back-mixing is less, burning time is shorter, mass transfer rate and hot input intensity are higher, and the one way amount of burnt of particle is less, and amount of sulfur contenting in smoke is lower, systemic circulation simultaneously is than (recycle ratio of prior art is about 40, the present invention can reach more than 100) also extended the particle burning time, reduced particle one way amount of burnt, made increase SO the time of contact of sulfur-containing smoke gas and sulphur-fixing agent
2Concentration reduces, and helps increasing mass transfer, rate of heat transfer between gas-solid, improves burning and solid sulphur efficiency.Therefore, the existing relatively coke powder combustion method (burning of prior art, for example low speed bed, gas speed 5～6m/s), the staged-combustion method of coke powder of the present invention and equipment have that coke powder particle size distribution applicatory wide (widely applicable), operating flexibility are big, burning fully, characteristics such as low, the burning of pollutant emission and solid sulphur efficiency height.
Description of drawings
Fig. 1: (hot experiment) device schematic diagram that is used for the coke powder burning for the present invention.
Drawing reference numeral
4-is low speed bed for 1-mixer fluidisation airduct 2-screw feeder 3-mixer
5-is bed 6-transverse tube 7-secondary cyclone 8-primary cyclone at a high speed
9-dipleg II 10-dipleg I 11-external warmer 12-heat-obtaining fluid bed
13-heat-obtaining fluidisation airduct 14-discharge duct 15-inlet valve 16-promotes airduct
The specific embodiment
The density of solid particles that the present invention carries out preliminary experiment (cold test, simulated combustion experiment) employing in advance is 1500kg/m
3, average grain diameter is 100 μ m, and gas is normal temperature, atmospheric air, and gas velocity adopts spinner survey, and particle mean concentration and pressure distribution adopt pressure transmitter measurement, and particle average speed adopts PV-4A type optical fiber measurement instrument to measure.The coke powder grain density that hot test is adopted is 1900kg/m
3, average grain diameter is 100 μ m, the heat carrier grain density is 2500kg/m
3, average grain diameter is 100 μ m, and gas is atmospheric air, and the particle mean concentration adopts pressure transmitter measurement, and bed temperature is by thermocouple measurement, and flue gas is formed common measurements the such as adopting GDX-104 type chromatographic column, 13-13X molecular sieve chromatography post and thermal conductance detection cell.
On the research basis of the result data that preliminary experiment (cold conditions experiment) is obtained, the present invention carries out coke powder combustion experiment (hot experiment), further specifies the solution of the present invention and effect by following embodiment.
The hot experiment of coke powder is finished in a cover steel recirculating fluidized bed, and flow process is seen accompanying drawing 1.Experimentation is: in the screw feeder 2 of at first coke powder particle and sulphur-fixing agent being packed into, heat carrier is packed in the heat-obtaining fluid bed 12, with fuel oil mixer 3 is heated to ignition temperature (for example 600 ℃), starting screw feeder 2 joins the coke powder fresh granules in the mixer 3, treat that the coke powder fresh granules is burnt in mixer 3 after, open mixer fluidisation airduct 1, heat-obtaining fluidisation airduct 13 and lifting airduct 16, in screw feeder, add simultaneously sulphur-fixing agent, coke powder burning particles in the mixer 3 enters low speed bed 4 under the carrying secretly that promotes wind, more incendive coke powder fine grained enters bed 5 at a high speed by low speed bed 4 fast, coke powder coarse granule than difficult to burn is then slower by low speed bed 4 speed, when fine grained that the gas of its burning in low speed bed 4 can be carried secretly, carried secretly by the gases in low speed bed 4 and to move upward fast and enter bed 5 at a high speed, the coke powder burning particles with fast speeds by bed 5 at a high speed and after transverse tube 6 enters heat-obtaining fluid bed 12, most coke powder particles and gas in heat-obtaining fluid bed 12 primary cyclone 8 and realize separating and entering in the heat-obtaining fluid bed 12 through dipleg I10, small part coke powder burning particles is then realized separating and entering into heat-obtaining fluid bed 12 through dipleg II9 through secondary cyclone 7 under the carrying of gas, open the particle cooling after external warmer 11 heat-obtainings make separation, purpose is to make the ignition temperature of the fresh granules that mixer adds lower (promptly reach autoignition temperature and need not outer focus fire), when the coke powder reserve in the heat-obtaining fluid bed 12 reach at least the fluid bed capacity 1/2 after, open inlet valve 15, coke powder burning particles and heat carrier in the heat-obtaining fluid bed enter into mixer 3 through inlet valve 15, to ignite by the coke powder fresh granules that screw feeder 2 joins in the mixer 3, simultaneously under the effect of carrying secretly that promotes wind, it is low speed bed 4 that coke powder burning particles in the mixer 3 enters once more, carries out circulating combustion so again and again.
Simultaneously, coke powder burning particles in mixer 3 entered before low speed bed 4 once more, can adjust the heat-obtaining amount of external warmer as required, promote air quantity, the fluidisation air quantity, the inlet amount of the aperture of inlet valve 15 and screw feeder 2, making the mixer operating gas velocity is 1.6m/s, low speed bed operating gas velocity is 2.4m/s, the bed operating gas velocity is 10m/s at a high speed, heat-obtaining fluidized bed process gas speed is 0.6m/s, the coke powder burning particles amount that is entered mixer 3 by inlet valve 15 is 1148kg/h, the coke powder fresh granules amount that adds mixer 3 by screw feeder 2 is 11.5kg/h, coke powder particle global cycle amount is 1159.5kg/h, recycle ratio is 99.8, and the Ca/S mol ratio is 2 and (can extrapolates and add sulphur-fixing agent CaCO
3Amount), heat-obtaining fluid bed granulate temperature is 800 ℃, treat that operating gas velocity and coke powder particle internal circulating load are stable after, collect flue gas that the coke powder burning produces and also analyze it and form, concentration, temperature and the efficiency of combustion of coke powder particle in the bed are measured.Bed temperature is a mixer: 600 ℃, bed outlet at a high speed: 850 ℃, coke powder particle burning efficient is 99%; Sulfur-fixing rate is 99%.Wherein, when all burnt or break down midway, can open discharge duct 14 material is drawn off.Efficiency of combustion and sulfur-fixing rate are calculated as follows:
Coke powder reserve in the experiment in the heat-obtaining fluid bed, grain density, particle average grain diameter, mixer operating gas velocity, low speed bed and at a high speed the bed operating gas velocity, enter coke powder burning particles amount, Ca/S mol ratio, heat-obtaining fluid bed granulate temperature and the operating gas velocity of mixer with embodiment 1 by inlet valve, the coke powder fresh granules amount that is added mixer by screw feeder is 15kg/h, particle global cycle amount is 1163kg/h, recycle ratio is 77.5 o'clock, measures coke powder particle mean concentration mixer 191kg/m
3, low speed bed 123kg/m
3, high speed bed 20.8kg/m
3, heat-obtaining fluid bed 600kg/m
3, 580 ℃ of bed temperature mixers, the bed outlet is 850 ℃ at a high speed, and coke powder particle burning efficient is: 99%; Sulfur-fixing rate is 98%.
Coke powder reserve in the experimentation in the heat-obtaining fluid bed, grain density, particle average grain diameter, mixer operating gas velocity, low speed bed operating gas velocity, at a high speed the bed operating gas velocity, enter coke powder burning particles amount, Ca/S mol ratio, heat-obtaining fluid bed granulate temperature and the operating gas velocity of mixer with embodiment 1 by inlet valve, when the coke powder fresh granules amount that is added mixer by screw feeder is 19kg/h, coke powder particle global cycle amount is 1167kg/h, recycle ratio is 61.4 o'clock, and the coke powder particle mean concentration of mensuration is mixer 196kg/m
3, low speed bed 126kg/m
3, high speed bed 21.9kg/m
3, heat-obtaining fluid bed 600kg/m
3, bed temperature is 560 ℃ of mixers, and the bed outlet is 850 ℃ at a high speed, and coke powder particle burning efficient is 98%; Sulfur-fixing rate is 97%.
Coke powder reserve in the experimentation in the heat-obtaining fluid bed, grain density, particle average grain diameter, mixer operating gas velocity, low speed bed operating gas velocity, at a high speed the bed operating gas velocity, enter coke powder burning particles amount, Ca/S mol ratio, heat-obtaining fluid bed granulate temperature and the operating gas velocity of mixer with embodiment 1 by inlet valve, when the coke powder fresh granules amount that is added mixer by screw feeder is 28kg/h, coke powder particle global cycle amount is 1176kg/h, recycle ratio is 42 o'clock, and the coke powder particle mean concentration of mensuration is mixer 201kg/m
3, low speed bed 129kg/m
3, high speed bed 23.2kg/m
3, heat-obtaining fluid bed 600kg/m
3, bed temperature is 550 ℃ of mixers, and the bed outlet is 850 ℃ at a high speed, and coke powder particle burning efficient is: 97%; Sulfur-fixing rate is 96%.
Coke powder reserve in the heat-obtaining fluid bed of experimentation, grain density, particle average grain diameter, mixer operating gas velocity, low speed bed and at a high speed bed operating gas velocity, heat-obtaining fluidized bed process gas speed with embodiment 1, the coke powder burning particles amount that is entered mixer by inlet valve is 2060, when the coke powder fresh granules amount that adds mixer is 21kg/h, coke powder particle global cycle amount is 2081kg/h, recycle ratio is 99.1, the Ca/S mol ratio is 1.6, when the heat-obtaining fluidized-bed temperature was 795 ℃, the coke powder particle mean concentration of mensuration was mixer 267kg/m
3, low speed bed 209kg/m
3, high speed bed 47.6kg/m
3, heat-obtaining fluid bed 600kg/m
3, bed temperature is 630 ℃ of mixers, and the bed outlet is 850 ℃ at a high speed, and coke powder particle burning efficient is 98%; Sulfur-fixing rate is 99%.
Coke powder reserve in the experimentation in the heat-obtaining fluid bed, grain density, particle average grain diameter, mixer operating gas velocity, low speed bed operating gas velocity, high speed bed operating gas velocity, heat-obtaining fluidized bed process gas speed are with embodiment 1, the coke powder burning particles amount, Ca/S mole that enters mixer by inlet valve when the heat-obtaining fluidized-bed temperature with embodiment 5, the coke powder fresh granules amount that adds mixer when feeder is 27kg/h, coke powder particle global cycle amount is 2087kg/h, during recycle ratio 77.3, the coke powder particle mean concentration of mensuration is mixer 271kg/m
3, low speed bed 212kg/m
3, high speed bed 48.4kg/m
3, heat-obtaining fluid bed 600kg/m
3, bed temperature is 620 ℃ of mixers, and the bed outlet is 850 ℃ at a high speed, and coke powder particle burning efficient is 97%; Sulfur-fixing rate is 97%.
Coke powder reserve in the experimentation in the heat-obtaining fluid bed, grain density, particle average grain diameter, mixer operating gas velocity, low speed bed operating gas velocity, high speed bed operating gas velocity, heat-obtaining fluidized bed process gas speed are with embodiment 1, the coke powder burning particles amount, Ca/S mole that enters mixer by inlet valve when the heat-obtaining fluidized-bed temperature with embodiment 5, the coke powder fresh granules amount that is added mixer by screw feeder is 35kg/h, coke powder particle global cycle amount is 2095kg/h, recycle ratio is 59.9, the coke powder particle mean concentration mixer 273kg/m of mensuration
3, low speed bed 217kg/m
3, high speed bed 50.1kg/m
3, heat-obtaining fluid bed 600kg/m
3, bed temperature is 610 ℃ of mixers, and the bed outlet is 860 ℃ at a high speed, and coke powder particle burning efficient is 96%; Sulfur-fixing rate is 96%.
Coke powder reserve in the experimentation in the heat-obtaining fluid bed, grain density, particle average grain diameter, mixer operating gas velocity, low speed bed and at a high speed bed operating gas velocity, heat-obtaining fluidized bed process gas speed with embodiment 1, the coke powder burning particles amount, Ca/S mole that enters mixer by inlet valve when the heat-obtaining fluidized-bed temperature with embodiment 5, the coke powder fresh granules amount that is added mixer by screw feeder is 51kg/h, coke powder particle global cycle amount is 2111kg/h, recycle ratio is 41.4 o'clock, and the coke powder particle mean concentration of mensuration is mixer 277kg/m
3, low speed bed 221kg/m
3, high speed bed 51.7kg/m
3, heat-obtaining fluid bed 600kg/m
3, bed temperature is 600 ℃ of mixers, the bed outlet is 860 ℃ at a high speed, coke powder particle burning efficient 95%; Sulfur-fixing rate 95%.
Embodiment 9
Coke powder reserve in the experimentation heat-obtaining fluid bed, grain density, particle average grain diameter, mixer operating gas velocity, low speed bed and at a high speed bed operating gas velocity, heat-obtaining fluidized bed process gas speed with embodiment 1, when the coke powder burning particles amount that is entered mixer by inlet valve is 3000, the coke powder fresh granules amount that is added mixer by screw feeder is 30kg/h, coke powder particle global cycle amount is 3030kg/h, recycle ratio is 101, the Ca/S mol ratio is 1.2, when the heat-obtaining fluidized-bed temperature was 790 ℃, the coke powder particle mean concentration of mensuration was mixer 359kg/m
3, low speed bed 306kg/m
3, high speed bed 45kg/m
3, heat-obtaining fluid bed 600kg/m
3, bed temperature is 650 ℃ of mixers, and the bed outlet is 850 ℃ at a high speed, and coke powder particle burning efficient is 98%; Sulfur-fixing rate is 98%.
Coke powder reserve in the experimentation in the heat-obtaining fluid bed, grain density, particle average grain diameter, mixer operating gas velocity, low speed bed and at a high speed bed operating gas velocity, heat-obtaining fluid bed granulate temperature and operating gas velocity with embodiment 1, the coke powder burning particles amount, Ca/S mole that enters mixer by inlet valve when the heat-obtaining fluidized-bed temperature with embodiment 9, as the coke powder fresh granules amount 40kg/h that adds mixer by screw feeder, coke powder particle global cycle amount 3040kg/h, during recycle ratio 76, measuring coke powder particle mean concentration is mixer 363kg/m
3, low speed bed 314kg/m
3, high speed bed 81.3kg/m
3, heat-obtaining fluid bed 600kg/m
3, bed temperature is 640 ℃ of mixers, and the bed outlet is 850 ℃ at a high speed, and coke powder particle burning efficient is 96%; Sulfur-fixing rate is 96%.
Coke powder reserve in the experimentation in the heat-obtaining fluid bed, grain density, particle average grain diameter, mixer gas speed, low speed bed and bed operating gas velocity at a high speed, heat-obtaining fluid bed gas speed is with embodiment 1, the coke powder burning particles amount, Ca/S mole that enters mixer by inlet valve when the heat-obtaining fluidized-bed temperature with embodiment 9, when the coke powder fresh granules amount that is added mixer by screw feeder is 52kg/h, coke powder particle global cycle amount is 3052kg/h, recycle ratio is 58.7 o'clock, and the coke powder particle mean concentration of mensuration is mixer 368kg/m
3, low speed bed 316kg/m
3, high speed bed 82.2kg/m
3, heat-obtaining fluid bed 600kg/m
3, bed temperature is 630 ℃ of mixers, and the bed outlet is 860 ℃ at a high speed, and coke powder particle burning efficient is 95%; Sulfur-fixing rate is 94%.
Coke powder reserve in the experimentation in the heat-obtaining fluid bed, grain density, particle average grain diameter, mixer operating gas velocity, low speed bed and bed operating gas velocity at a high speed, heat-obtaining fluidized bed process gas speed is with embodiment 1, the coke powder burning particles amount, Ca/S mole that enters mixer by inlet valve when the heat-obtaining fluidized-bed temperature with embodiment 9, when the coke powder fresh granules amount that is added mixer by screw feeder is 75kg/h, coke powder particle global cycle amount 3075kg/h, recycle ratio is 41 o'clock, and the coke powder particle mean concentration of mensuration is mixer 372kg/m
3, low speed bed 321kg/m
3, high speed bed 84.6kg/m
3, heat-obtaining fluid bed 600kg/m
3, 620 ℃ of bed temperature mixers, the bed outlet is 860 ℃ at a high speed, and coke powder particle burning efficient is 93%; Sulfur-fixing rate is 93%.
Claims (10)
1. the combustion method of a coke powder, comprising:
(1) described coke powder particle burns through low speed bed and high speed bed in proper order, and this low speed bed gas speed is 0.3～3m/s, and the gas speed of bed is 3～25m/s at a high speed;
(2) particle after the burning separates through gas-solid separating device with gas, and solid particle enters in the heat-obtaining fluid bed;
(3) solid particle that enters in the heat-obtaining fluid bed is lowered the temperature through heat-obtaining, enters mixer, mixes with initiate coke powder fresh granules, reenters the circulating combustion of step (1).
2. the combustion method of coke powder as claimed in claim 1, wherein coke powder particle described in the step (1) through before low speed bed in the mixer burning, the gas speed of this mixer is 0.5～3m/s, temperature is 600～750 ℃.
3. the combustion method of coke powder as claimed in claim 2 wherein is separated into secondary cyclone and separates described in the step (2), the coke powder particle after the described burning is with after gas separates through secondary cyclone, and the coke powder particle enters the heat-obtaining fluid bed.
4. the combustion method of coke powder as claimed in claim 3 comprises also that wherein described coke powder particle enters the heat-obtaining fluid bed and reduces to after the temperature of mixer back-mixing again.
5. the combustion method of coke powder as claimed in claim 1, wherein low speed bed gas speed is 0.5～3m/s, temperature is 750～850 ℃.
6. the combustion method of coke powder as claimed in claim 1, the gas speed of its high speed bed is 6～20m/s, temperature is 850～1000 ℃.
7. the equipment of coke powder burning, comprise low speed bed, airduct and gas-solid separating device that low speed bed bottom connects, it is characterized in that, this equipment also is provided with mixer, high speed bed and heat-obtaining fluid bed, this mixer is connected in low speed bed bottom, its lower end is provided with airduct, this its cross section of high speed bed is less than low speed bed cross section and be connected in low speed bed top, its exit, upper end is provided with transverse tube and is connected with this heat-obtaining fluid bed by transverse tube, described gas-solid separating device is located at the top of this heat-obtaining fluid bed, the bottom of heat-obtaining fluid bed is provided with inlet valve, communicates with mixer by inlet valve.
8. the equipment of coke powder burning as claimed in claim 7, wherein said gas-solid separating device is at least one cyclone separator, this cyclone separator is positioned at the top of described heat-obtaining fluid bed, the lower end also is provided with dipleg, one end of this dipleg links to each other with the bottom port of cyclone separator, the other end is located in this heat-obtaining fluid bed, makes the coke powder particle after the separation enter this heat-obtaining fluid bed by this dipleg.
9. the equipment of coke powder burning as claimed in claim 8, wherein said gas-solid separating device is two cyclone separators, the exhaust outlet of one of them cyclone separator is connected with the import of another cyclone separator.
10. the equipment of coke powder burning as claimed in claim 9, the bottom of wherein said heat-obtaining fluid bed is provided with discharge duct and airduct.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200510080800XA CN100436941C (en) | 2005-07-05 | 2005-07-05 | Coal-tar powder combustion method and apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB200510080800XA CN100436941C (en) | 2005-07-05 | 2005-07-05 | Coal-tar powder combustion method and apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1892106A true CN1892106A (en) | 2007-01-10 |
| CN100436941C CN100436941C (en) | 2008-11-26 |
Family
ID=37597218
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB200510080800XA Active CN100436941C (en) | 2005-07-05 | 2005-07-05 | Coal-tar powder combustion method and apparatus |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100436941C (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101417800B (en) * | 2008-07-16 | 2010-08-11 | 孔庆然 | Process for preparing carbon disulphide by using circulating fluid bed |
| CN105279895A (en) * | 2014-07-23 | 2016-01-27 | 国家电网公司 | Anti-touch device of overhead power line |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1523500A (en) * | 1975-10-21 | 1978-09-06 | Battelle Development Corp | Method of operating a fluidized bed system |
| DE3582385D1 (en) * | 1984-09-24 | 1991-05-08 | Combustion Power | CIRCULATING FLUIDIZED BURNING PROCESS AND DEVICE. |
| US5526775A (en) * | 1994-10-12 | 1996-06-18 | Foster Wheeler Energia Oy | Circulating fluidized bed reactor and method of operating the same |
| JP3508036B2 (en) * | 1995-07-17 | 2004-03-22 | 中部電力株式会社 | Boiler for circulating fluidized bed power generation |
| CN2259552Y (en) * | 1996-04-09 | 1997-08-13 | 北京通用能源动力公司 | Circulation fluidized-bed boiler improved from pulverized-fuel boiler |
| CN1172738C (en) * | 2002-09-17 | 2004-10-27 | 山东大学 | Compound desulfurizing process of circulating fluidized bed boiler |
| CN1224446C (en) * | 2003-08-15 | 2005-10-26 | 武汉凯迪电力股份有限公司 | large-sized dry-process flue gas desulfurizing method with single-tower muiti-bed circulating fluidization |
-
2005
- 2005-07-05 CN CNB200510080800XA patent/CN100436941C/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101417800B (en) * | 2008-07-16 | 2010-08-11 | 孔庆然 | Process for preparing carbon disulphide by using circulating fluid bed |
| CN105279895A (en) * | 2014-07-23 | 2016-01-27 | 国家电网公司 | Anti-touch device of overhead power line |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100436941C (en) | 2008-11-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Fan et al. | Impact of air staging along furnace height on NOx emissions from pulverized coal combustion | |
| CN102585913B (en) | Coal gas, tar, semi-coke and steam poly-generation method based on fluidized bed pyrolysis technology | |
| CN1784483A (en) | Compositon for preventing scaling,excluding of soot,clinker and sludge,and controlling flame in combustion apparatus | |
| CN102942943B (en) | Oil shale gas-solid heat carrier dry distillation and semicoke combustion electricity generation integral process | |
| CN2501564Y (en) | Apparatus by bio-matter pyrolytic gas refiring denitration | |
| WO2016078177A1 (en) | Biomass micron fuel high-temperature industrial boiler | |
| CN101368724A (en) | Coal thermal decomposition grate firing apparatus and its combustion method | |
| WO2017161633A1 (en) | Cyclone combustion apparatus, combustion device, and combustion method | |
| CN1148528C (en) | Layered decoupling coal-burning technology and mechanical layered decoupling furnace | |
| CN1892106A (en) | Coal-tar powder combustion method and apparatus | |
| CN1916124A (en) | Catalytic coal gasifaction furnace of differential speed bed, and method of catalytic gasification | |
| CN1959207A (en) | Method for burning petroleum coke or gasified remained coke, and inner mixed type combustion equipment | |
| CN102443445B (en) | Process and device for continuously gasifying biomass and simultaneously removing tar in moving bed | |
| CN204490820U (en) | Gasifying biomass kiln gas self-purifying device | |
| CN109054873A (en) | A kind of biomass boiler system of included biomass upgrading function | |
| CN1279310C (en) | Jetting-fluidized vortex coal powder burners | |
| CN104152184A (en) | Biomass cyclone pyrolysis-suspension combustion composite gasification device and gasification method thereof | |
| CN113551222A (en) | Biomass fuel low-nitrogen combustion device and low-nitrogen combustion method thereof | |
| CN1594971A (en) | Dust cloud combustion furnace | |
| CN2816613Y (en) | Device for feeding coal upwards from coal-burning boiler bottom and boiler mounted with same | |
| KR100387732B1 (en) | Circulation Fluidized Bed Boiler System Mounted with Pelletizer for Anthracite | |
| CN205878145U (en) | Pulverized coal boiler | |
| CN2714965Y (en) | Dust cloud combustion furnace | |
| CN2494927Y (en) | Mechanical layered decoupling combustion stove | |
| CN117511581B (en) | Internal and external dual-mode heating coal rapid cracking reaction device and method |
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 |