Liquid heaters and vaporizers – Miscellaneous
Patent
1991-09-17
1992-08-18
Favors, Edward G.
Liquid heaters and vaporizers
Miscellaneous
110245, 16510416, B09B 300, F22B 100
Patent
active
051389827
DESCRIPTION:
BRIEF SUMMARY
TECHNICAL FIELD
The present invention relates to an apparatus for incinerating coal, anthracite, coal dressing sludge, petro coke, bark, bagasse, industrial waste, municipal waste and other combustibles by using a so-called circulating type fluidized bed as well as for recovering thermal energy from the fluidized bed, and a method of controlling the amount of diffusion gas to be blown into a thermal energy recovery chamber and the amount of fuel to be supplied in order to regulate the amount of thermal energy recovered and to maintain a constant temperature in the primary incinerating chamber of the fluidized bed.
PRIOR ART
Heretofore, as a circulating fluidized bed type incinerator, such ones as those disclosed in Japanese Patent Publication Nos. 46988/76 and 5242/68 have been known.
One example of the above-mentioned circulating type fluidized bed incinerator will be explained by referring to FIG. 1.
A diffusion plate 2 is provided at a furnace bottom of an incinerator 1 for the purpose of causing fluidization of a fluidizing medium. The diffusion plate 2 is inclined so that the wall side provided with a waste feeding device 3 is higher than the opposite side, the lower portion of the opposite side being coupled with an incombustible discharge opening 4.
Fluidizing air fed from a blower 8 is blown upwardly from the diffusion plate 2 through air chambers 5, 6 and 7 to fluidize the fluidizing medium.
The mass flow of the fluidizing air blown up from each of the air chambers is arranged to be sufficient to produce a fluidized bed, the flow blown up from the chamber 7 being the largest and that from the chamber 5 being the smallest.
For example, the mass flow is selected from the following ranges, namely, that blown up from the air chamber 7 being in the range of 4-20 Gmf, or preferably 6-12 Gmf, that from the air chamber 6 being in the range of 3-10 Gmf, or preferably 4-6 Gmf, and that from the chamber 5 being in the range of 1-4 Gmf, preferably 1-2.5 Gmf.
1 Gmf is a value of the mass flow at which the fluidization is commenced.
The state of the fluidizing medium is changed from a static state, which is referred to as a static bed, to a dynamic state, which is referred to as a fluidized bed, with the above value as a threshold between the two states.
While the example shown in FIG. 1 shows three air chambers, the number is optional and may, for example, be two or more than three chambers, and the mass flow of the fluidizing air is arranged to be large for the chamber near the discharge opening 4 and small for the chamber remote from the discharge opening.
Just above the air chambers 7 and 6, an inclined wall 9 is provided to serve as a deflecting wall for interrupting passage of the upward flowing fluidizing air so as to deflect the air towards the combustible feeding device 3.
At the upper side of the inclined wall 9, an inclined surface 10 whose inclination is opposite to that of the wall 9 is provided to prevent the fluidizing medium from becoming piled up thereon.
The inclination of the diffusion plate 2 is, in the case where the incombustibles are contained in the combustibles to be charged, preferably in the range of 5.degree.-15.degree.; however, in the case where the amount of incombustibles is small, the inclination may be nil and the plate may be horizontal since the fluidizing medium can be put into circulation by adjusting the flow rate of the air blown from the respective air chambers.
The surface of the wall 9 may be either flat, convex or concave. At a ceiling 11 of the incinerator, a combustion gas exhaust 12, a feed conduit 13 for feeding liquid waste generated upon operating the incinerator, and a cooling water feeding conduit 14 etc. are provided.
As to the operation of the incinerator 1, the fluidizing air is fed thereinto by the blower 8 and the fluidizing air is injected in regulated amounts of mass flow decreasing in the order of the chambers 7, 6 and 5.
In the conventional fluidized bed, the fluidizing medium moves violently up-and-down, just like boiling water, to produce a flui
REFERENCES:
patent: 3702595 (1972-11-01), Muirhead et al.
patent: 3881857 (1975-05-01), Hoy et al.
patent: 3921590 (1975-11-01), Mitchell et al.
patent: 3970011 (1976-07-01), Virr et al.
patent: 4279222 (1981-07-01), Pearce
patent: 4301771 (1981-11-01), Jukkola et al.
patent: 4338887 (1982-07-01), Leon
patent: 4363292 (1982-12-01), Engstrom
patent: 4419330 (1983-12-01), Ishihara et al.
patent: 4452155 (1984-06-01), Ishihara et al.
patent: 4457289 (1984-07-01), Korenberg
patent: 4528945 (1985-07-01), Virr et al.
patent: 4619314 (1986-10-01), Shimoda
patent: 4938170 (1990-07-01), Ohshita et al.
7th International Conference on Fluidized Bed Combustion-vol. 1, Jan. 83, "The Control of Industrial Fluidized Bed Boiler Plant", Michael J. Virr, pp. 350-359.
"A Novel In-Bed Heat Transfer Tube Capable of Decreasing h.sub.w Linearly With Load Turndown", Horio et al., pp. 655-663.
"Fluidization Engineering", Kunii et al., pp. 272-277.
Power Technology, 19 (Jun. 1978), pp. 197-203, "Bed to Surface Heat Transfer In A Fluidized Bed of Large Particles", Deloye et al.
Higo Tsutomu
Inumaru Naoki
Kawaguchi Hajime
Kosugi Shigeru
Ohshita Takahiro
Ebara Corporation
Favors Edward G.
LandOfFree
Internal circulating fluidized bed type boiler and method of con does not yet have a rating. At this time, there are no reviews or comments for this patent.
If you have personal experience with Internal circulating fluidized bed type boiler and method of con, we encourage you to share that experience with our LandOfFree.com community. Your opinion is very important and Internal circulating fluidized bed type boiler and method of con will most certainly appreciate the feedback.
Profile ID: LFUS-PAI-O-1241175