METHOD AND APPARATUS FOR RECOVERING CALCIUM CHLORIDE FROM SPENT ABSORBENT LIQUID IN EXHAUST GAS DESULFURIZATION PROCESS

Abstract: Method and apparatus for recovering CaCl₂ in solid form from a spent liquor containing CaSO₄ and CaCl₂ and occurring in an exhaust gas desulfurization process which remove sulfur oxides by the use of an absorbent liquid from exhaust gases resulting from combustion of coal and having a high Cl content, removing impurities including CaSO₄ from the spent liquor in a thickener, spraying the spent liquor into a drying chamber while blowing thereinto hot air to dry the sprayed particles of said spent liquor to obtain powder of CaCl₂, and collecting the powder of CaCl₂ after separation by use of a solid separator.

Description: BACKGROUND OF THE INVENTION 1. Field of the Invention This invention relates to a method and appara tus for recovering Cacti2 in solid form from a spent 2 liquor occurring in an exhaust gas desulfurization processes, and more particularly to a method and apparatus for recovering in a valuable form Cacti2 which builds up in the treating absorbent liquid in a wet lime-gypsum desulfurization process 2. Description of the Prior Art In the wet lime-gypsum desulfurization process, CaS03 which is produced by absorption of 502 into a treating liquid containing lime components such as CaC03 and/or Ca(OH)2 is further oxidized into CaSO4 for reuse. The inventors have been engaged in a comprehensive research in this respect, and have already developed and actually applied on an-industrial scale the technology of increasing the solubility of the absorbent Ca(OH)2 by adding a suitable amount of Caul2 to the treating liquid thereby to improve the rate of removal of sulfur oxides. On the other hand, due to a sudden change in the energy situation, there has been an increasing trend toward relying again on coal. The exhaust gas which results from combustion of coal contains C1 ions in a high concentration of up to 400 ppm in addition to sulfur components like SO, the C1 ions forming CaC12 by bonding with Ca ions of the lime components, consequently increasing the Cacti2 concentration in the treating liquid. The CaC12 concentration which has complicate influences on the 502 absorption reaction, oxidation reaction, quality of gypsum of the by-product and corrosion of component parts of the desulfurization system should be maintained at a predetermined appropriate level even in the above-mentioned improved method of our prior proposal. In order to attain this, it becomes necessary to discharge a large quantity of waste water from the system. However, the discard of waste water is currently under control of strict regulations and needs a treatment which can be economically and technically a great burden. In view of these situations, the present inventors have been engaged in research work to develop a method for recovering in solid form the concentrated CaC12 content of the treating liquid without necessitating the discard of waste water. In the CaCl2-added lime-gypsum process, the Caul2 concentration in the absorbent liquid is at most at the level of 40%, and, in consideration of the saturated concentration of the aqueous CaC12 solution, it is extremely difficult to recover it efficiently in solid form and in an economical manner. Besides, it was expected that the recovery in solid form might be difficult in the actual operations of the ordinary wet lime-gypsum process in which the absorbent liquid would contain accumulated Caul2 in much lower concentration and require an additional condensing operation for that purpose. There is an industrially established technology as long as the recovery of the dehydrate from aqueous solution of Caul2 is concerned. However, in the case of the afore-mentioned exhaust gas desulfurization process, the operation involves more complicate various conditions as compared with the recovery from the aqueous solution of CaC12 alone. More particularly, experiments of CaC12 recovery were conducted by the use of: (1) a method of condensing the treating liquid by indirect heating (under the atmospheric pressure) in an oil bath; (2) a method of condensing similarly by indirect heating but under a reduced pressure; and (3) a method of condensing the liquid by blowing thereinto a hot gas under the atmospheric pressure. As a result, it has been found that the methods (1) and (2) has a limitation in the degree of condensation due to vigorous foaming and inability of raising the heating temperature, coupled with the problem that CaSO4 which coexists in the liquid causes scale deposition on the inner surfaces of the condensing vessel, dropping its heat transfer efficiency. The method (3) is advantageous not only in that it can condense the liquid to a desired concentration without the foaming trouble, but also in that its heating mechanism is free of the adverse effect of the scale deposition. Therefore, we repeated experiments for the recovery of CaC12 in solid form by the method (3), and succeeded in arriving at some attainment as disclosed in our co-pending patent application (Japanese Patent Application No. 55-73457). SUMMARY OF THE INVENTION We continued our research for the industrialization of the above-mentioned method, taking various approaches by employing different means, in an attempt to establish a method which can recover CaCl2 in solid form under more stablized operating conditions. Thus, it is an object of the present invention to provide a method of recovering CaC12 from the spent absorbent liquid in the exhaust gas desulfurization by the wet lime-gypsum process, collecting CaC12 in solid form of high utility without causing troubles to the desulfurization process. According to one aspect of the present invention, there is provided a method for recovering Caul2 in solid form from spent liquor containing CaSO4 and CaC12 occurring in an exhaust gas desulfurization process for removing sulfur oxides by the use of an absorbent liquid from an exhaust gas resulting from combustion of coal and having a high C1 content, the method comprising: removing impurities including CaSO4 from the spent liquor; spraying the spent liquor into a drying chamber while blowing thereinto hot air to dry the sprayed particles of the spent liquor to obtain solid powder of CaC12; and collecting the powder =of CaC12 after separation by the use of a solid separator. According to another aspect of the present invention there is also provided an apparatus for recovering Caul2 in solid form from a spent liquor containing CaSO4 and CaC12 occurring in an exhaust gas desulfurization process which removes sulfur oxides by the use of an absorbent liquid from exhaust gas resulting from combustion of coal and having a C1 content, the apparatus comprising: a thickener for removing impurities including CaSO4 from the spent liquor; a drier for drying the spent liquor; a nozzle mounted in an upper portion of the drier for spraying the spent liquor thereinto; a blow hole provided in an upper portion of the drier for blowing hot air thereinto to obtain solid powder of CaC12 by drying the sprayed particles of the spent liquor; and a solid separator connected to the bottom of the drier for collecting dried powder of Caul2. The above and other objects, features and advantages of the invention will become apparent from the following description and appended claims, taken in conjunction with the accompanying drawings. BRIEF DESCRIPTION OF THE DRAWING In the accompanying drawing:: The sole figure is a flowsheet of a recovery system according to the present invention. PARTICULAR DESCRIPTION OF THE INVENTION Hereafter, the invention and its effects are described in connection with the developments of various experiments conducted under the following conditions with regard to: (A) a method of condensation by hot air blowing; (B) a spray-dry method according to the invention; and (C) a drying method using a drum drier. Method (A): Spent treating liquid from the exhaust desulfurization process was received in a vessel for flocculating and sedimenting a small amount of suspended solids, and the supernatant liquid was transferred into a condensing vessel after adding thereto a defoaming agent for the sake of safety. The liquid was thickened by blowing hot air thereinto until a slurry was obtained by precipitation of crystals of CaC12¯2H20, which was put into a centrifugal separator to separate the dihydrate in solid form. Method (B): The supernatant liquid which was obtained in the same manner as in the foregoing method was sprayed from above into a vertical drying chamber by means of a high pressure pump, while at the same time blowing hot air into the drying chamber from above, bringing them instantaneously into parallel flow contact to produce powder by evaporation. The powder of the dihydrate which was entrained in the air flows was led into a cyclone for separation. Method (C): The supernatant liquid which was obtained in the same manner as in the foregoing methods was applied thinly around the circumferential surface of a drum which was heated by a heating medium like steam for drying the applied liquid. The dihydrate which was formed by drying was scraped off after each revolution of the drum to separate the solid in the form of flakes. There was obtained the dihydrate in any one of the Methods (A) to (C), which showed differences in the aspect of operationability as discussed and evaluated in greater detail hereinbelow. In the following description, Methods (A) to (C) are referred to as "a hot air blowing method", "a spray-drier method" and "a drum-drier method", respectively. Scaling The hot air blowing method gives rise to a medium degree of scaling on the inner wall surfaces of the container although it has no influences on the heat transfer efficiency. However, in the case of a continuous operation, it will necessitate a periodical scale removing operation which is disadvantageous from the standpoint of the maintenance and service of the apparatus.. and its service life. In contrast, the operation proceeds extremely favorably in this regard in the spray drier method and the drum drier method with substantially no scaling. Corrosion of Component Parts It is necessary to take some measures against corrosion of component parts in the case of the hot air blowing method in which the apparatus has relatively large liquid contacting surface areas and the liquid temperature sometimes goes up to 110 - 1200C. In the drum drier method, the drum is used in a heavily corrosive environment since its entire circumferential surface is applied with the treating liquid of a high temperature which reaches as high as 1500C in some cases according to our experiments, also requiring to provide some measures against corrosion. On the other hand, there is no need for providing special corrosion preventing means for the apparatus as a whole in the spray drier method, except the spray nozzle which is the only one component that contacts the treating liquid, and the temperature of the liquid is at most at the level of 50 C. Foamina The hot air blowing method involves less foaming but there will occur a slight degree of foaming inan operation on a larger scale unless a defoaming agent is added. In contrast, the other two methods are completely free of the foaming problem. Pipe blocking The hot air blowing method suffers from clogging of the air blowing pipe due to scaling or blocking of the slurry line by precipitated crystals, in contrast to the other two methods which have no problems of this sort. Stability of operation In the case of the hot air blowing method, the operation loses stability due to larger changes in operating condition which are caused depending upon the slurry concentration, the degree of supersaturation, the liquid level in the condensing vessel and the extent of foaming, causing variations in the load of the centrifugal separator. On the other hand, the drying rate is varied slightly by the moisture content in the other two methods, but there occurs no trouble which disturbs the stability of operation in any distinctive degree. Quality of recovered product (dihydrate) It is impossible to control the particle size of the product in the hot air blowing method in which a slurry of high viscosity is subjected to the centrifugal separation, as well as in the drum drier method in which the product scraped off from the drum surface is in the form of flakes of irregular shapes and sizes. In the spray drier method, however, it is possible to obtain a product which is essentially in the form of fine powder, and to control the particle size by varying the spraying nozzle diameter. Besides, the spray drier method can produce calcium chloride of spherical form which has a wider range of application. As a result of the comparative evaluations of the methods (A) to (C) in various aspects of the operation as discussed above, it has been concluded that the spray drier method is regarded as the best by overall judgement since it is simplified in process itself, less susceptible to the problems bf scaling and corrosion, and capable of controlling the particle size of the product. The drawing shows a flowsheet of a process incorporating the spray drier method according to the present invention, wherein the spent treating liquid from an exhaust gas desulfurization system is fed to a thickener 1 as indicated by arrow A, returning flocculated or sedimentary impurities 2 like CaSO4 to a solid collecting section of the exhaust gas desulfurization system as indicated by arrow B. The supernatant liquid of the thickener 1 is transferred into a feed liquid storage tank 4 and fed to a nozzle 6 by a feed pump 5 for spraying same into a drying chamber 7. The reference numeral 8 denotes a feedback pipe for returning excess liquid to the tank 4. On the other hand, fuel and combustion air are blown into a burner 10 of a hot blast generating furnace 9 as indicated by arrows C and D, respectively, while blowing a large quantity of air into the furnace by an air blower 11 as indicated by arrow E. The generated hot blasts which are blown into the drying chamber 7 from its top through pipe 12 envelop the sprayed feed liquid from the nozzle to heat and dry the liquid. Although the feed liquid and hot blast are contacted in parallel flow for maintaining an optimum particle density and for making the drying chamber 7 compact, of course there may be employed a counter-flow or cross-flow system depending upon the desired properties of the final Caul2 product. The dried powder 13 which drops into a hopper at the bottom of the drying chamber 7 is fed to a plural number of cyclones 16 (two in the particular example shown) through a transfer pipe 15 by the action of the pressure in the drying chamber 7 and the pressurized air from a pneumatic fan 14, thereby separating the fine and coarse particles from air. The powder thus obtained is dropped into a storage chamber 17, the separated air which still contains very fine particles is passed through a bag filter 24 or the like to remove the fine powder particles and then fed into the transfer gas by the pneumatic fan 14 to serve as a carrier air again. The recovered CaC12 in the storage chamber 17 is dropped into a product container 23 through a double damper 19. In this manner, the recovery of Caul2 in solid form is attained by a closed system. However, it is to be noted that various alterations or modifications can be added to the particular example shown, and¯that the invention includes such alterations or modifications as long as encompassed by the scope of the invention as defined in the appended claims. Example A spent treating liquid of an exhaust gas desulfurization process, with a CaC12 concentration of 16%, and a condensed liquid having a concentration of 38% were sprayed under pressure into a drying chamber at a rate of 25 - 37 Q/m, while hot air having a temperature of 305 - 3200C at the inlet was blown into the chamber to dry the sprayed liquid. The temperature in the middle portion of the drying chamber was 120 l500C and its internal pressure was -25 mmAg. The product separated by the cyclones was white powder of CaC12 2H2O having a particle size of 100 - 150 ijm and a residual moisture content less than 5.

Claims: WHAT IS CLAIMED IS: 1. A method for recovering Caul2 in solid form from spent liquor containing CaSO4 and C aCl2 and occurring in an exhaust gas desulfurization process which remove sulfur oxides by the use of an absorbent liquid from exhaust gases resulting from combustion of coal and having a high C1 content, said method comprising: removing impurities including CaSO4 from said spent liquor; spraying said spent liquor into a drying chamber while blowing thereinto hot air to dry the sprayed particles of said spent liquor to obtain powder of CaC12; and collecting the resulting powder of Caul2 after separation by the use of a solid separator. 2. A method as set forth in claim 1, wherein said hot air is blown into said drying chamber in parallel flow with said sprayed spent liquor. 3. An apparatus for recovering Caul2 in solid form from a spent liquor containing CaSO4 and CaC12 occurring in an exhaust gas desulfurization process which removes sulfur oxides by the use of an absorbent liquid from exhaust gases resulting from combustion of coal and having a high Ci content, said apparatus comprising: a thickener for removing impurities including CaSO4 from said spent liquor; a drier for drying said spent liquor; a nozzle mounted in an upper portion of said drier for spraying said spent liquor thereinto; a blowing hole provided in an upper portion of said drier for blowing hot air thereinto to obtain powder of CaC12 by drying sprayed particles of said spent liquor; and a solid separator connected to the bottom of said drier for collecting dried powder of Caul2. 4. An apparatus as set forth in claim 3, wherein said spraying nozzle and blow hole are oriented such that the sprayed spent liquor and hot air are contacted in parallel flow.

Inventors: MASUDA, TOYOHIKO, NADA, JUNICHIRO, NISHIDA, HIDEO, SUGIYAMA, KIMIO, YAMAGATA, MASAHIRO
Applicants: KABUSHIKI KAISHA KOBE SEIKO SHO
Application year: 1982
Main classification: C01F11
IPC codes: B01D53, C02F1, C01F11