CN1221645A - Liquid bleeding device and method for controlling concentration of slurry in wet flue gas desulfurization system - Google Patents
Liquid bleeding device and method for controlling concentration of slurry in wet flue gas desulfurization system Download PDFInfo
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- CN1221645A CN1221645A CN98118664A CN98118664A CN1221645A CN 1221645 A CN1221645 A CN 1221645A CN 98118664 A CN98118664 A CN 98118664A CN 98118664 A CN98118664 A CN 98118664A CN 1221645 A CN1221645 A CN 1221645A
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- 239000007788 liquid Substances 0.000 title claims abstract description 283
- 239000002002 slurry Substances 0.000 title claims abstract description 213
- 239000003546 flue gas Substances 0.000 title claims abstract description 37
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 36
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 28
- 230000023556 desulfurization Effects 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title claims abstract description 20
- 230000000740 bleeding effect Effects 0.000 title abstract 3
- 239000007787 solid Substances 0.000 claims abstract description 42
- 239000006096 absorbing agent Substances 0.000 claims description 38
- 238000010521 absorption reaction Methods 0.000 claims description 33
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 24
- 239000002250 absorbent Substances 0.000 claims description 18
- 230000002745 absorbent Effects 0.000 claims description 18
- 238000005192 partition Methods 0.000 claims description 12
- 238000007599 discharging Methods 0.000 claims description 10
- 229940043430 calcium compound Drugs 0.000 claims description 4
- 150000001674 calcium compounds Chemical class 0.000 claims description 4
- 238000005259 measurement Methods 0.000 claims description 3
- 230000004044 response Effects 0.000 claims description 3
- 230000009471 action Effects 0.000 abstract description 6
- 230000006698 induction Effects 0.000 abstract 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 29
- 239000010440 gypsum Substances 0.000 description 20
- 229910052602 gypsum Inorganic materials 0.000 description 20
- 230000001276 controlling effect Effects 0.000 description 16
- 235000019738 Limestone Nutrition 0.000 description 11
- 239000006028 limestone Substances 0.000 description 11
- 238000013019 agitation Methods 0.000 description 7
- 238000002360 preparation method Methods 0.000 description 7
- 238000005406 washing Methods 0.000 description 7
- 230000008859 change Effects 0.000 description 6
- 230000008021 deposition Effects 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- 230000000630 rising effect Effects 0.000 description 5
- 230000015572 biosynthetic process Effects 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000000706 filtrate Substances 0.000 description 4
- 238000011282 treatment Methods 0.000 description 4
- 238000007664 blowing Methods 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 230000001590 oxidative effect Effects 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- 239000003463 adsorbent Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000011065 in-situ storage Methods 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- -1 limestone Chemical class 0.000 description 1
- 238000010297 mechanical methods and process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
- 229910052815 sulfur oxide Inorganic materials 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 238000012795 verification Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
- B01D47/06—Spray cleaning
- B01D47/063—Spray cleaning with two or more jets impinging against each other
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/346—Controlling the process
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/606—Carbonates
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- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
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- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
An object of this invention is to provide a simple liquid bleeding device making it possible to bleed out only a liquid component from a slurry within a tank, and a method for controlling the concentration of a slurry in a wet flue gas desulfurization system by using such a device. Specifically, this invention provides 1 a liquid bleeding device which comprises a slurry outlet member formed in a sidewall of the tank at a position lower than the level of the slurry and which enables the slurry within the tank to flow out under the action of a pressure head difference. matter, and a liquid component induction path whose upper end is connected to the inner side of the outlet member of the liquid bleeder and whose lower end extends toward the bottom of the tank and is left open, the cross-sectional dimension and length of the liquid component induction path being determined so that, when the slurry flows out from the liquid bleeder by way of the liquid component induction path under the action of a pressure head difference, the flow velocity of the liquid component therein is lower than the settling velocity of the solid matter.
Description
The present invention relates to a liquid discharge apparatus suitable for use in, for example, an absorption tank of a wet flue gas desulfurization system, and a method for controlling the slurry concentration in a wet flue gas desulfurization system using such an apparatus.
In recent years, an in-situ oxidation type warm lime-gypsum method has been popular as a flue gas desulfurization technique for removing sulfur oxides (typified by sulfur dioxide) from flue gas produced from thermal power plants and the like. According to the method, an absorbent slurry containing suspended calcium compounds, such as limestone, is fed from an absorber tank located at the bottom of the absorber tower and circulated through a gas-liquid contact zone located at the upper portion of the absorber tower. At the same time, the flue gas is passed into an absorption column and brought into gas-liquid contact with an absorbent slurry. On the other hand, oxidizing air is forcibly blown into the absorption tower tank so that the slurry subjected to gas-liquid contact is oxidized in the absorption tower tank to produce gypsum as a by-product.
In order to achieve stable operation of the flue gas desulfurization system, it is necessary to keep the amount of slurry (i.e., the liquid level) present in the absorber tank within a certain limit by controlling, for example, the amount of slurry discharged to recover gypsum. On the other hand, the slurry concentration (i.e., the solid matter concentration mainly composed of gypsum) in the absorber tank must be kept within a predetermined range (usually 20 to 30 wt%).
If the slurryconcentration is too high, troubles such as clogging of pipes and pumps in the circulation system for supplying the slurry to the upper part of the absorption tower or in the piping for discharging the slurry from the tank of the absorption tower are easily caused, thus making the operation difficult. On the other hand, if the slurry concentration is too low, so-called seed crystals of gypsum present in the slurry are reduced, and as a result, a large portion of gypsum successively formed in the absorption tower tank by absorption of sulfur dioxide and subsequent reaction precipitates and adheres to the surfaces of the equipment parts such as the inner wall surfaces of the absorption tower tank to form scales, and can also cause troubles in clogging the pipes. Further, the low-concentration slurry is disadvantageous in view of the operation cost because of the increase in load in the solid-liquid separation treatment of the recovered gypsum.
Meanwhile, the sulfur dioxide content in the flue gas often fluctuates with power generation load and the like, and therefore, the feed rate of the absorbent (e.g., limestone) fed into the absorption tower drum must be controlled at all times so as to reach a minimum required level corresponding to the fluctuating inlet sulfur dioxide content. Further, the air distributor wash water for blowing the oxidizing air or the like is always introduced into the absorption tower tank at a fixed flow rate.
For these reasons, solids added to or formed in the tank are reduced at lower sulfur dioxide levels in, for example, flue gases (i.e., low load conditions). On the other hand, the above-mentioned washing water is always introduced at a fixed flow rate, so that the slurry concentration in the tank becomes low. Especially when a chiller for cooling and separating particulate matter is installed upstream of the absorber tower (i.e., the system is of the dual loop type), the flue gas entering the absorber tower is nearly saturated with water vapor so that only a small amount of water is vaporized in the absorber tower and carried away by the flue gas. As a result, in operation, the slurry concentration in the tank is likely to fall outside the above specified range.
Moreover, even when the system is shut down (i.e., desulfurization is suspended), the washing water is often continuously supplied. Therefore, even if the system is not of the two-circuit type, the slurry concentration in the tank may be reduced outside the above-specified range.
However, in the prior art, no simple method of discharging only the slurry liquid component in the absorber tank has been found. Therefore, when the slurry concentration is lowered due to the change in the water balance, only passive measures such as reducing the amount of makeup water supplied to the absorber tank (or the amount of filtrate returned to the absorber tank from the separated gypsum) or stopping such supply can be taken.
Therefore, if operation or shutdown is continued for a longer period of time under such low load conditions, the slurry concentration will drop to too low a level. If the system is operated with such slurry conditions, said fouling formation is unavoidable and very cumbersome operations like internal cleaning are required in a short time interval. In addition, it causes an increase in the load of the solid-liquid separation treatment of the recovered gypsum, resulting in an increase in the operation cost.
As disclosed in Japanese Patent provisional publication (Japanese Patent provisional publication) No.230620/184, the present applicant has previously proposed a method of controlling the concentration of a slurry in which the slurry is divided into two portions of high concentration and low concentration, and the two portions are discharged at independently controlled flow rates. But no simple method has beenproposed to discharge only the liquid component without using a pump or special power.
It is therefore an object of the present invention to provide a simple liquid discharge apparatus which can discharge only the liquid component of the slurry in the tank, and a method for controlling the slurry concentration in a wet flue gas desulfurization system using such an apparatus.
To achieve the above object, the present invention provides a liquid discharge apparatus for discharging a liquid component of a low-solid content slurry from a tank containing the slurry, the slurry in the tank consisting of a liquid containing suspended matter, the liquid discharge apparatus comprising: (1) a liquid discharger comprising a slurry outlet means formed in a side wall of the tank below a liquid level of the slurry and allowing the slurry in the tank to flow out by a head difference, (2) a liquid component suction passage having an upper end connected to an inner side of the outlet means of the liquid discharger and a lower end extending to a bottom of the tank and opened, the liquid component suction passage having a cross-sectional size and a length determined so that a flow velocity of the liquid component therein is lower than a settling velocity of the solid matter when the slurry flows out of the liquid discharger through the passage by the head difference.
Although the liquid discharge apparatus of the present invention comprises a liquid discharge means connected to the liquid component suction passage and thus has a very simple and inexpensive structure, only the liquid component can be discharged from the tank, as will be described later.
First, since the liquid discharger includes a slurry outlet means formed at a position of the side wall of the tank lower than the liquid level of the slurry and allows the slurry in the tank to flow out by the head difference, the liquid can be discharged from the liquid discharger through the liquid component suction passage without any power. Moreover, since the sectional size and length of the liquid component suction passage are determined so that the flow velocity of the liquid component therein is lower than the settling velocity of the solid matter, the solid matter is separated in the liquid component suction passage, and as a result, the liquid discharged from the liquid discharger is a low-solid-content liquid component.
Further, for use in a wet flue gas desulfurization system in which a slurry containing a calcium compound as an adsorbent is supplied from an absorption tower formed at the bottom of the absorption tower and circulated through a gas-liquid contact region at the upper part of the absorption tower so that untreated flue gas is brought into contact with the slurry to remove at least sulfur dioxide present in the untreated flue gas by absorption into the circulating slurry, the invention also provides a method of controlling the concentration of the slurry in the system, which comprises installing the liquid discharge device of the invention on the absorption tower, and controlling the concentration of the slurry in the absorption tower by adjusting the amount of the liquid component discharged from the absorption tower and the amount of the liquid component supplied to the absorption tower with the liquid discharge device.
In the method for controlling the slurry concentration in a wet desulfurization system according to the present invention, the liquid discharge apparatus of the present invention is installed in the absorber tank, and the slurry concentration in the absorber tank is controlled by adjusting the amount of the liquid component discharged from the absorber tank and the amount of the liquid component supplied to the absorber tank by the liquid discharge apparatus.
Thus, the present invention makes it possible to achieve positive concentration control by a method of discharging a liquid component from a tank with a simple device, which has not been possible in the prior art. Therefore, the problem of concentration reduction under low load or shutdown conditions is solved, and appropriate concentration control of the slurry in the absorber tank can be reliably and inexpensively achieved.
Brief description of the drawings
FIG. 1 is a schematic diagram illustrating one example (first embodiment) of a wet flue gas desulfurization system employing the present invention;
FIG. 2 is an enlarged view illustrating a liquid drain for the system of FIG. 1;
FIG. 3 is an enlarged view illustrating another example (second embodiment) of the liquid discharge apparatus of the present invention;
FIG. 4 is a perspective view illustrating an example (second embodiment) of the liquid discharge apparatus of the present invention shown in FIG. 3;
FIG. 5 is an enlarged view illustrating still another example (third embodiment) of the liquid discharge apparatus of the present invention;
FIG. 6 is a simplified flow diagram illustrating experimental equipment demonstrating the action of the present invention;
fig. 7 is a graph showing the results of an experiment performed to demonstrate the effect of the present invention.
Detailed description of the preferred embodiments
To achieve the above object, the present invention provides a liquid discharge apparatus for discharging aliquid component of a slurry of low solids content from a tank of the slurry consisting of a liquid containing suspended solids, the liquid discharge apparatus comprising: (1) a liquid discharger comprising a slurry outlet means formed in a side wall of the tank below a liquid level of the slurry and allowing the slurry in said tank to flow out by a head difference, (2) a liquid component suction passage having an upper end connected to an inner side of the outlet means of the liquid discharger and a lower end extending to a bottom of the tank and opened, the sectional dimension and length of the liquid component suction passage being determined so that a flow velocity of the liquid component therein is lower than a settling velocity of the solid matter when the slurry flows out of said liquid discharger through the passage by the head difference.
In a preferred embodiment of the invention, the liquid discharge device is provided with a vertically mounted partition having an opening for passage of the slurry therethrough so as to define a liquid component suction passage.
When the tank is provided with a partition plate having an opening for the passage of the slurry and vertically installed to define a suction passage for the liquid component, the flow of the slurry into the suction passage caused by the agitation of the slurry with air bubbles entrained in the optional tank is prevented. Thus, the turbulent flow of the air-entrained bubble slurry formed by the inward flow caused by the agitation is surely prevented from reaching the liquid component suction passage. Further, when discharging the liquid, the slurry in the tank flows into the inside of the partition through the opening and then flows into the liquid component suction passage through the lower end thereof. The discharge of said low-solids liquid component can thus be accomplished with particularly high reliability.
In another preferred embodimentof the invention, the liquid discharger has an on/off member (e.g. a valve) connected to its external member.
When the liquid discharger has an on/off member connected to its external member, the discharge of the liquid component of the slurry can be controlled (i.e., started and stopped) or regulated (so as to regulate the flow rate of the discharge).
In a further preferred embodiment of the invention, the opening/closing member of the liquid discharger comprises a flow passage forming member (e.g. a pipe or a hose) having an inlet and an outlet for the slurry, the inlet being connected to the outlet member of the liquid discharger, and the vertical position of the outlet with respect to the level of the slurry being variable.
When the opening/closing member is said to comprise a flow path forming member having an inlet and an outlet for the slurry, wherein the inlet is connected to the outlet member of the liquid discharger and the vertical position of the outlet with respect to the level of the slurry can be changed, the deposition of the scales in the flow path of the opening/closing member is greatly suppressed and the maintenance of the opening/closing member is facilitated even in the case where the scales are deposited. Moreover, the elimination of the valve mechanism results in a corresponding cost savings.
In this case, the discharge of the slurry liquid component can be stopped by raising the vertical position of the outlet of the flow passage forming member above the level of the slurry liquid, and the discharge of the slurry liquid component can be started by lowering the vertical position of the outlet of the flow passage forming member below the level of the slurry liquid. Further, the discharge flow rate can be adjusted by controlling the head difference between the slurry level and the outlet of said flow passage forming member.
In still another preferred embodiment of the present invention, the slurry flow path is inclined upward by 5 degrees or more with respect to a horizontal plane in at least the outlet member of the liquid discharger while extending in the slurry flow direction.
When the slurry flow path in at least the outlet member of the liquid discharger is inclined 5 degrees or more upward with respect to the horizontal plane during its extension in the slurry flow direction, fouling and clogging of the liquid discharger flow path due to deposition of gypsum particles can be avoided. From this point of view again, the discharge of components having a low solids content can be carried out particularly easily and with high reliability.
In a still further preferred embodiment of the present invention, the liquid discharge means is provided with a blow pipe extending from the upper end of the liquid component suction passage and having a top end opening located above the surface of the slurry.
When the liquid discharge means is provided with a blow pipe extending from the upper end of the liquid component suction passage and having a top end opening located above the surface of the slurry, the slurry liquid component can be discharged more smoothly because if air bubbles enter the liquid component suction passage, they can be discharged from the upper end of the blow pipe.
In a further preferred embodiment of the invention, the liquid discharge apparatus is provided with an agitator for agitating the slurry present in the tank in the region below the suction passage of the liquid component.
When the liquid discharge apparatus is provided with an agitator for agitating the slurry existing in the region below the liquid component suction passage of the tank, the retention or sedimentation of the substances separated in the solid component suction passage and settled through the passage is prevented due to the agitation action of the agitator, particularly in the region below the liquid component suction passage. As a result, troubles (e.g., change in concentration of discharged liquid and formation of fouling at the bottom of the can) due to such stagnation and deposition can be surely avoided.
Further, for use in a wet flue gas desulfurization system in which the concentration of the slurry in the system is controlled by installing the liquid discharge apparatus of the present invention on the absorber tank and controlling the concentration of the slurry in the absorber tank by adjusting the amount of the liquid component discharged from the absorber tank and the amount of the liquid component supplied to the absorber tank with the liquid component discharge apparatus, the slurry containing a calcium compound as an adsorbent is supplied from the absorber tank formed at the bottom of the absorber and circulated through a gas-liquid contact zone in the upper part of the absorber to bring untreated flue gas into contact with the slurry to remove at least sulfur dioxide present in the untreated flue gas by absorption into the slurry.
In a method for controlling the slurry concentration in a wet flue gas desulfurization system according to a preferred embodiment of the present invention, the slurry concentration in the absorber tank is automatically controlled so as to be equal to a desired concentration by measuring the slurry concentration in the absorber tank with a concentration detector and automatically adjusting the amount of the discharged liquid component or the amount of the supplied liquid component in response to the result of measurement with the concentration detector using a controller.
When the concentration of the slurry in the absorption tower tank is automatically controlled so as to be equal to a desired concentration by automatically adjusting the amount of the discharged liquid component or the amount of the supplied liquid component by measuring the concentration of the slurry in the absorption tower tank with a concentration detector and using a controller in response to the result of the measurement by the concentration detector, unmanned control of the concentration is possible, whereby labor and the like can be saved.
Several embodiments of the present invention will be described below with reference to the accompanying drawings. (first embodiment)
FIG. 1 is a schematic diagram illustrating one example (first embodiment) of an in situ oxidation-type wet flue gas desulfurization system using the present invention.
As shown in fig. 1, the system comprises an absorption tower 1 and a tank 2 installed at the bottom of the absorption tower 1. The tank 2 is provided with a so-called air rotating distributor 3 for blowing oxidizing air K in the form of fine air bubbles into the slurry S while stirring the slurry S, thereby allowing the absorbent slurry containing the absorbed sulfur dioxide to be efficiently brought into contact with the air in the tank 2 to be sufficiently oxidized to form gypsum.
More specifically, in this system, the untreated flue gas a is introduced into the flue gas inlet section 1a of the absorption tower 1 and is brought into contact with the absorbent slurry sprayed from the header 5 by the circulation pump 4, so that at least the sulfur dioxide present in the untreated flue gas a is removed by absorption into the absorbent slurry. The resulting flue gas is discharged as treated flue gas B through the flue gas outlet section 1B. The absorbent charged liquid ejected from the header 5 flows downward while absorbing sulfur dioxide, and enters the tank 2, where it is oxidized by being brought into contact with a large number of air bubbles blown into the absorbent slurry stirred by the air distributor 3, and then gypsum is produced by a neutralization reaction.
The main reactions occurring during these treatments can be represented by the following reaction equations (1) to (3). It should be understood that a so-called stationary air distributor consisting of a set of stationary air distribution pipes may also be used as the air distributor 3 instead of a so-called rotating air distributor. (flue gas inlet section of absorption column)
Thus, gypsum and a small amount of limestone (acting as absorbent) are mainly suspended in the slurry S in the tank 2. In the embodiment, the slurry S is discharged through a line 6 extending from the side wall of the tank 2 and supplied to a solid-liquid separator 7. The result of the filtration is that gypsum C with a low temperature content (typically about 10%) is recovered. On the other hand, the filtrate from the solid-liquid separator 7 is sent to a slurry preparation tank 8 as water W constituting the absorbent slurry1. Typically, a portion of the filtrate from the solid-liquid separator 7 is removed from the system as desulfurization waste water in order to avoid accumulation of impurities in the circulating slurry.
A slurry preparation tank 8 equipped with a stirrer 9 is used for preparing an absorbent slurry by stirring finely powdered limestone D from a limestone hopper (not shown) with the filtrate W1Or water W supplied separately2And (4) mixing. The absorbent slurry in the slurry preparation tank 8 is supplied to the tank 2 of the absorptiontower 1 with a slurry pump 10, if necessary.
During operation, the amount of water supplied to the slurry preparation tank 8 may be adjusted by, for example, a controller (not shown) and a flow control valve (not shown). An appropriate amount of limestone corresponding to the amount of supplied water is supplied from a limestone hopper by controlling the operation of a rotary valve (not shown). Thus, the slurry preparation tank 8 is maintained in a state in which the absorbent slurry having a predetermined concentration (for example, about 20 to 30% by weight) is always stored, the concentration thereof being within a certain range.
In addition, in order to maintain a high desulfurization degree and a high purity of gypsum during operation, the concentration of sulfur dioxide in the untreated flue gas a and the pH value of the absorbent slurry and the concentration of limestone in the tank 2 were measured with sensors. So that the feed rate of the limestone D, the feed rate of the absorbent slurry, and other parameters are appropriately controlled by a controller (not shown).
In addition, the amount of slurry discharged through line 6 is controlled by means of, for example, a flow control valve (not shown) to keep the amount of slurry in tank 2 constant.
In addition, in order to replenish the water that is gradually lost by evaporation in the absorption tower 1 or the like, replenishment water (for example, industrial water) is supplied to, for example, the tank 2 as necessary.
Furthermore, washing water W3The air distributor 3 is fed with air K to avoid solid matter sticking to the nozzles or the like blowing the air outwards. The washing water W3Flows into the slurry together with air K.
For scale of, for example, about 1,000,000Nm3Desulfurization system for flue gas,/h washing water W3Is usually set at about 4m3/h。
As shown in enlarged fig. 2, the tank 2 is also equipped with a liquid discharge device 20 which is very simple and inexpensive to install.
The liquid discharge apparatus 20 is an apparatus for discharging a liquid component of a slurry having a low solid content from the tank 2, and comprises a liquid discharger part 20a which allows the slurry in the tank 2 to flow out by a head difference h, a liquid component suction pipe (or liquid component suction passage) 22 which separates a solid matter from the slurry introduced into the liquid discharger part 20a, and an agitator 25 which agitates the slurry existing in a region of the tank 2 lower than the liquid component suction pipe 22.
In this embodiment, the liquid discharger part 20a comprises an outlet pipe (or outlet member) 21 connected to an opening formed in the side wall of the tank 2 below the surface of the slurry and having an end surface extending outwardly from the side wall of the tank 2, and a valve (or opening/closing member) 23 connected to the outer end surface of the outlet pipe 21.
Also, in this embodiment, the entire flow path composed of the outlet pipe 21, the valve 23, and the pipe connected to the valve 23 is inclined upward at an angle θ with respect to the horizontal plane while extending outward (i.e., in the flow direction of the slurry).
The angle theta is determined so that it is greater than the angle of repose (5 degrees) of the gypsum particles in the liquid. Thus, since the entire flow path has no horizontal portion and is inclined at least at the angle of repose described above, the liquid discharge device 20 advantageously avoids the formation of or clogging of fouling at the outlet pipe 21, valve 23, etc. due to gypsum particle deposition.
In this embodiment, the head difference h is defined as the difference in height between the discharge end of the pipe opening connected to the outside of the valve 23 and the level of the slurry, at a value such that the discharge flow rate reaches the desired value Q. This value can be determined according to the Bernoull theorem and by flow resistance calculations. For example, calculations made by the inventors have shown that if the head difference h is set to about 1m, the discharge flow rate can reach about 4m3H is substantially equal to said washing water W3The flow rate of (c).
The liquid component suction pipe 22 has an upper end connected to an inner end of said outlet pipe 21 constituting the liquid discharger part 20a, and a lower end extending toward the bottom of the tank 2 and remaining open. At the upper end of the liquid component suction pipe is provided a blow pipe 24 which extends vertically and whose upper end is located above the liquid level of the slurry. The blow-down pipe 24 functions to allow air bubbles to escape from the upper end if they flow into the liquid component suction pipe 22, thereby making the discharge of the slurry liquid component smoother.
The length of the liquid component suction pipe 22 is determined at least to be a value (for example, about 1m) which prevents the turbulent motion of the slurry S flowing in the tank 2 due to agitation from reaching the upper end of the inner space thereof. Further, the inner diameter D of the liquid component suction pipe 22 is determined so that the flow rate of the liquid component in the upper non-turbulent flow region of the inner space thereof is lower than the settling velocity of the solid matter when the slurry is discharged from the valve 23 through the liquid component suction pipe 22 and the liquid discharger portion 20a by the head difference h.
Specifically, the average particle diameter of the solid matter in the slurry S is about 40. mu.m. Therefore, if the average flow velocity V of the liquid component in the liquid component suction pipe 22 is set to, for example, about 10m/h, this value is lower than the settling velocity of the solid matter. The inner sectional area of the liquid component suction pipe 22 is determined by Q/V. Thus, when Q is equal to, for example, 4m as described above3At/h, the inner cross-sectional area is 4/10=0.4m2. Therefore, in this case, the inner diameter D may be set so that the inner sectional area is 0.4m2The value of (c).
If the inner diameter D is increased, the flow rate of the slurry ascending in the liquid component suction pipe (or the liquid component suction passage) 22 becomes low, and the liquid having a lower solid content can be discharged. Thus, the appropriate said internal diameter D (i.e. flow rate V) may be determined in accordance with the desired solids content of the discharged liquid. For example, if the flow rate V is set to 4m/h or less, the solids content of the discharged liquid can be reduced to about 10g/l or less, as can be seen in the exemplary data set forth below.
In this embodiment, the agitator 25 comprises an axial flow type impeller, a motor disposed outside the tank 2 for driving the impeller, and a rotating shaft sealing means for connecting the motor and the impeller, in an area lower than the liquid component suction pipe 22 and placed in or toward the tank 2. The agitator 25 agitates the slurry existing in the area below the liquid component suction pipe 22 to avoid stagnation or sedimentation of the separated solids in this area.
The function of the above-described liquid discharge apparatus 20 and the method of using it to control the slurry concentration in the tank 2 will now be described.
When using the above-mentioned liquid discharge device 20, if the valve 23 is opened, a flow of liquid having a fixed flow rate is generated, the magnitude of the flow rate depending on the flow resistance of the liquid discharge device 20 (including the resistance of the valve 23) and the head difference h. As a result, the liquid is discharged at this fixed flow rate through the liquid component suction pipe 22 and the liquid discharger portion 20 a.
Since the liquid component suction pipe 22 is sized in the manner described above, the turbulent flow of the slurry S in the tank 2 does not reach the upper end of the liquid component suction pipe 22, and the flow rate of the liquid component in the liquid component suction pipe 22 is lower than the settling velocity of the solid matter at least in the non-turbulent flow region. As a result, the solid matter in the slurry does not rise to the upper end of the liquid component suction pipe 22, and is thus separated from the liquid component therein. Thus, the liquid discharged from the valve 23 is substantially free of solid matter, and as a result, only the liquid component in the slurry is discharged at a predetermined flow rate.
The liquid discharge device of the invention can thus be positively controlled in concentration in the following manner: when the operation is carried out under low load conditions or in a shutdown state, and the concentration of the slurry S in the tank 2 has fallen below its optimum range or is likely to fall below it, the flow rate of the slurry S discharged through the line 6 is reduced or the discharge is stopped, and the valve 23 of the liquid discharge device 20 is opened by an amount determined according to the degree of concentration reduction. These operations may be performed automatically by the controller 15, which measures this state by means of the concentration sensor 14, or manually by an operator after judging that this state has occurred.
As described above, the maximum discharge capacity of the liquid discharge device 20 is determined to be equal to or less than the washing water W3And the feed rate of make-up water, which is introduced into tank 2 to increase the liquid content of slurry S. Thus, even when operating under low load or shutdown conditions, by opening the valve 23, it is possible to ensure that the concentration of the slurry S is within said optimum range.
On the other hand, when the concentration of the slurry S in the tank 2 has exceeded its optimum range or is likely to exceed it, the valve 23 of the liquid discharge device 20 is partially or completely closed, the feed rate of the water to the tank 2 is increased according to the degree of increase in the concentration, and the flow rate of the slurry S discharged through the line 6 is increased. These operations may be performed automatically by the controller 15, which measures the state by means of the concentration sensor 14, or manually by an operator after judging that the state has occurred. To increase the feed rate of water to tank 2, the feed rate of make-up water to the tank may be increased or the feed rate of water supplied in the form of an absorbent slurry may be increased.
Excess liquid discharged by the liquid discharge 20 may be discharged from the system after reaching the standard through the necessary waste water treatment. However, if water balance is maintained, the excess liquid may be directed, for example, to the slurry preparation tank 8 shown in FIG. 1 for reuse as part of the liquid component making up the absorbent slurry. Therefore, the need for the treatment of the waste water can be eliminated, and the water W introduced into the slurry preparation tank 8 can be saved2。
The excess liquid may also be used, for example, as wash water for various parts of a desulfurization system, such as the air distributor of an absorption tower, or the demister (not shown) installed at the flue gas outlet of an absorption tower.
Although the solid matter separated in the liquid component suction pipe 22 is settled down through the liquid component suction pipe 22, the stirring action of the stirrer 25 used in the present embodiment can prevent it from being stagnated or settled, particularly in the area lower than the liquid component suction pipe 22. Therefore, in this embodiment, troubles (e.g., change in concentration of discharged liquid and formation of bottom foulings) due to such retention and deposition can be surely avoided. (second embodiment)
Fig. 3 and 4 illustrate a liquid drain 30 according to a second embodiment of the present invention. The desulfurization system to which the liquid discharge apparatus 30 is applied and the method for controlling the slurry concentration using the same are the same as those described for the first embodiment, and therefore, explanation thereof is omitted. In addition, the same members as those mentioned above for the first embodiment are denoted by the same reference numerals, and the explanation thereof is not repeated.
The liquid discharge apparatus 30 is an apparatus for discharging a liquid component of a slurry having a low solid content from the tank 2, and comprises a liquid discharge portion 30a which enables the slurry in the tank 2 to flow out by a head difference h, a liquid component suction passage 32 whose upper end is connected to an inner end of an outlet pipe (or outlet member) 31 constituting the liquid discharge portion 30a and whose lower end extends toward the bottom of the tank 2 and is kept open, and a partition 33 (shown in fig. 4) which encloses the liquid component suction passage 32.
In fig. 3 and 4, reference numeral 35 denotes a vent similar to the vent 24 described for the first embodiment.
In this embodiment, the liquid discharge portion 30a includes an outlet pipe 31 connected to an opening formed in the side wall of the tank 2 and having an end face extending outward from the side wall of the tank 2, and a valve 23 connected to an outer end face of the outlet pipe 31. Also, the entire flow path composed of the outlet pipe 31, the valve 23, and the pipe connected to the valve 23 extends outward (i.e., in the slurry flow direction), inclined upward by an angle θ with respect to the horizontal plane.
Similar to the first embodiment, the angle θ should be determined to be greater than the angle of repose (5 degrees) of the gypsum particles in the liquid.
In this embodiment, the liquid component suction passage 32 is an inner space formed by a box-shaped member 34 mounted on the inner wall of the tank 2, as shown in fig. 4, to which the outlet pipe 31 is connected. The box-shaped member 34 described above remains open and forms the open lower end face of the liquid component suction passage 32.
The partition 33 has an opening 33a serving as a slurry passage, and in this embodiment, is vertically installed at the side of the tank 2 so as to enclose the box-shaped member 34. In fig. 4, the upper end of the partition 33 extends to a level significantly higher than the level of the slurry S in the tank 2. However, the liquid level of the slurry S may be located beyond the upper end of the partition plate.
The baffle 33 serves to close off the flow caused by the agitation of the air bubbles entrained in the tank 2. Therefore, the partition 33 has a function of surely preventing the turbulent flow of the slurry entrained with the air bubbles, which is caused by the inward flow generated by the agitation, from reaching the inner space of the box-shaped member 34 (i.e., the liquid component suction passage 32).
During the liquid discharge, the slurry in the tank 2 flows into the inside of the partition 33 through the opening 33a, and then enters the liquid component suction passage 32 through the open lower end of the box-shaped member 34.
Similar to the first embodiment, the length L of the liquid component suction passage 32 is determined to have a value (e.g., about 1m) that at least does not allow the turbulence of the slurry S flowing in the tank 2 due to agitation to reach the top end of the internal space thereof. Further, the inner width W of the liquid component suction passage 32 is determined so that the liquid component rises in the inner space thereof at a lower flow velocity than the settling velocity of the solid matter when the slurry flows out through the liquid component suction passage 32 and the liquid discharge portion 30a by the head difference h.
The liquid drain 30 functions in the same manner as described in relation to the first embodiment. Specifically, by opening the valve 23, a flow of liquid is generated having a fixed flow rate, the magnitude of which depends on the flow resistance of the liquid discharge device 30 (including the resistance of the valve 23) and the head difference h. As a result, the liquid is discharged at the fixed flow rate through the liquid component suction passage 32 and the liquid discharge portion 30 a.
Due to the above-mentioned action of the partition 33 and the previously determined size of the liquid component suction passage 32, the turbulent flow of the slurry S in the tank 2 must not reach the inside of the liquid component suction passage 32, and the flow rate of the liquid component in the liquid component suction passage 32 is lower than the settling velocity of the solid matter at least in the non-turbulent flow region. As a result, the solid matter in the slurry does not rise to the upper end of the liquid component suction passage 32, and is separated from the liquid component in the passage. Thus, the liquid discharged by the valve 32 is substantially free of solid matter, with the result that only the liquid component of the slurry is discharged at a fixed flow rate. (third embodiment)
Fig. 5 is a schematic diagram illustrating a liquid drain 50 according to a third embodiment of the present invention. The desulfurization system to which the liquid discharge apparatus 50 is applied and the method of controlling the slurry concentration therewith are the same as those described for the first embodiment, and therefore, the explanation thereof is omitted, and further, the same components as those mentioned previously for the first embodiment are denoted by the same reference numerals, and the explanation thereof will not be repeated.
The liquid discharge apparatus 50 is an apparatus for discharging a liquid component of a slurry having a low solid content from the tank 2, and includes a liquid discharge portion 50a for allowing the slurry in the tank 2 to flow out by a head difference h, and a liquid component suction pipe 22 for separating solid matters from the slurry entering the liquid discharge portion 50 a.
In this embodiment, the liquid discharge portion 50a is composed of the outlet tube 21 and a hose (or flow passage forming member) 51 connected to the outer end of the outlet tube 21.
The hose 51 corresponds to the flow passage forming member of the present invention, and functions as the opening/closing member of the present invention. One end (or slurry inlet) of which is connected to an outlet pipe 21. In this case, the hose 51 has flexibility to allow its other end (or slurry outlet) to move vertically with respect to the slurry level.
As a result of this structure, the discharge of the slurry liquid component can be terminated by keeping the vertical position of the other end of the hose 51 above the slurry liquid level, and also can be started by keeping the vertical position of the other end of the hose 51 below the slurry liquid level, as shown in fig. 5 by reference numeral 51 a. Further, when the slurry liquid component is discharged, the discharge flow rate thereof can be adjusted by changing the vertical position of the other end of the hose 51 to thereby control the head difference h.
Thus, in this embodiment, the hose 51 functions as an on/off device that stops or starts the slurry liquid component and adjusts its flow rate. Therefore, the cost can be reduced as compared with the case of using a valve. Moreover, this embodiment has the great advantage that the trouble of the valve mechanism being clogged with dirt is never caused, and that even if dirt adheres to the inside of the hose 51, the maintenance (i.e., cleaning) work is easy to perform.
The change and adjustment of the vertical position of the other end (or outlet) of the hose 51 can be done manually, for example, using a suitable tool that can hold the hose 51 in various positions, or mechanically, by moving the hose 51 vertically by means of a motor and drive, such as an air cylinder. It goes without saying that when such a mechanical method is used, the vertical position of the other end of the hose 51 can be automatically controlled by the controller 15 in accordance with a signal from the slurry concentration sensor 14. (verification data)
Experimental data demonstrating the operation and effectiveness of the liquid discharge apparatus of the present invention will now be described. An experimental apparatus having the structure shown in fig. 6 was used for this purpose.
Specifically, the slurry tank 41 of the absorption tower tank of the simulated desulfurization system is filled with the initial slurry, and a liquid discharge pipe 42 serving as a liquid component suction passage of the present invention is installed in the slurry tank 41 so as to stand upright and protrude above the upper end of the slurry tank 41. The slurry liquid component in the slurry tank 41 is discharged through the liquid discharge pipe 42 and returned to the slurry tank 41 by using the suction pump 43, thereby circulating.
The actual absorber slurry obtained from the absorber tank (actual equipment) of the desulfurization system was used as the initial slurry. The test slurry had a solids content of 240.7g/l and a gypsum concentration of 1,309.0mmol/l unreacted limestone concentration of 126.0 mmol/l.
The slurry tank 41 and the liquid drain pipe 42 are provided with water-passing jackets 41a and 42a, respectively. The warm water in the thermostatic tank 44 is circulated successively through the jackets 41a and 42a using the hot water feed pump 45. The temperature of the slurry in the slurry tank 41 and the temperature of the slurry circulated through the liquid drain 42 are maintained at the normal operating temperature (50 ℃) of the absorber tank (actual equipment) of the desulfurization system by controlling the output power of the heater 46 for heating warm water in the thermostatic tank 44.
The slurry in the slurry tank 41 is stirred by the stirrer 47 in the same manner as in the absorber tank (actual equipment) of the desulfurization system.
The liquid discharge tube 42 has an inner diameter (D) of 35mm, a length (L) of 1,000mm, and a height (H) above the slurry surface of 800 mm.
Experiments were carried out by controlling the flow rate of the suction pump 43 so as to adjust the rising speed (V) of the slurry in the liquid discharge pipe 42 to 1,2,4,7 or 10 m/h. Then, the solid content of the overflow slurry (or the drain liquid) drained from the liquid drain 42 at each rising speed is measured.
The results of these experiments are shown in figure 7. Specifically, the solids content of the overflow slurry at each of the rise rates was 1.4,5.4,10.4,83.5 and 144.0 g/l. Thus, it was confirmed that if the rising speed (V) was set to 10m/h or less, a liquid component having a significantly reduced solid content as compared with the initial slurry could be discharged. In particular, when the velocity (V) is set to 4m/h or less, the solid content of the discharged liquid can be further significantly reduced.
In connection with this, the concentration of gypsum in the discharged liquid was 7.2,10.0,8.7,454.7 and 784.9mmol/l at the respective rising speeds. Furthermore, the concentrations of unreacted limestone in the let-down liquid were 0.8,31.4,78.3,49.3 and 85.1mmol/l at the respective rising speeds.
It is to be understood that the present invention is not limited to the above-described embodiments, but may be embodied in various other forms. For example, the liquid discharge apparatus of the present invention can be applied not only to the absorption tower tank of a desulfurization system as described above, but also to any equipment and plant that require a liquid component to be discharged from a slurry liquid in a simple manner. In these cases, the liquid discharge device of the present invention can produce the same effect.
Moreover, the liquid discharge apparatus of the present invention does not necessarily require the installation of an opening/closing member such as the valve 23 shown in fig. 2. It is of course possible to use it to allow the liquid component to be continuously discharged from the tank at a fixed flow rate.
Further, the flow passage forming member constituting the opening/closing member of the liquid discharger of the present invention is not limited to the flexible hose, but may be, for example,a rigid pipe. For example, one open end (or inlet) of such a tube may be connected to the pipe 21 of fig. 5 by a rotary change joint, so that the pipe can be rotated by means of the rotary change joint along, for example, the wall of the tank. This rotation then causes the other open end (or outlet) of the pipe to move vertically with respect to the slurry level.
Claims (9)
1. A liquid discharge apparatus for discharging a low solids content liquid component from a slurry containing tank containing liquid in which solid matter is suspended, said liquid discharge apparatus comprising (1) a liquid discharge vessel including a slurry outlet means formed in a side wall of said vessel below the level of the slurry liquid and adapted to permit the slurry liquid in said vessel to flow out under the influence of head differential, (2) a liquid component suction passage connected at an upper end thereof to an inner side of said liquid discharge vessel outlet means and extending at a lower end thereof to the bottom of the vessel and open, said liquid component suction passage having a cross-sectional dimension and length determined so that the flow rate of the liquid component therein is lower than the settling rate of the solid matter when the slurry liquid flows out of said liquid discharge vessel through the passage under the influence of head differential.
2. A liquid discharge apparatus as claimed in claim 1, provided with a partition having an opening for passing the slurry therethrough, the partition being vertically installed so as to enclose said liquid component suction passage.
3. A liquid discharge apparatus as claimed in claim 1 or 2, wherein said liquid discharge means has an on/off member connected to its outlet member.
4. A liquid discharge apparatus as claimed in claim 3, wherein said opening/closing member of said liquid discharge apparatus comprises a flow passage forming member having a slurry inlet and an outlet, the inlet being connected to said outlet member of said liquid discharge apparatus, and the vertical position of the outlet being variable with respect to the level of the slurry.
5. A liquid discharge apparatus as claimed in any one of claims 1 to 4, wherein the slurry flow path is inclined upwardly at an angle of 5 degrees or more to the horizontal at least in said liquid discharge outlet member when the slurry flow path extends in the slurry flow direction.
6. A liquid discharge apparatus as claimed in any one of claims 1 to 5, which is provided with a blow pipe extending upwardly from an upper end of said liquid component suction passage and having an open upper end located above a liquid surface of the slurry.
7. A liquid discharge apparatus as claimed in any one of claims 1 to 6, which is provided with an agitator for agitating a slurry existing in said tank in a region lower than the suction passage of said liquid component.
8. A method for controlling the concentration of a slurry in a wet flue gas desulfurization system, which comprises equipping said absorber tank with a liquid discharge device as defined in any one of claims 1 to 7, and controlling the concentration of the slurry in said absorber tank by adjusting the amount of a liquid component discharged from said absorber tank and the amount of a liquid component supplied to said absorber tank with said liquid discharge device, wherein a slurry containing a calcium compound as an absorbent is supplied from the absorber tank formed at the bottom of the absorber tank and circulated through a gas-liquid contact zone located at the upper part of the absorber to bring untreated flue gas into gas-liquid contact with the slurry to remove at least sulfur dioxide present in the untreated flue gas by absorption into the slurry.
9. A method for controlling the slurry concentration in a wet flue gas desulfurization system as recited in claim 8, wherein the slurry concentration in said absorber tank is automatically controlled so as to be equal to a desired concentration by measuring the slurry concentration in said absorber tank with a concentration detector, and automatically adjusting the amount of the discharged liquid component or the amount of the supplied liquid component with a controller in response to the result of measurement with the concentration detector.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP24344697 | 1997-08-25 | ||
| JP243446/97 | 1997-08-25 | ||
| JP243446/1997 | 1997-08-25 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1221645A true CN1221645A (en) | 1999-07-07 |
| CN1101245C CN1101245C (en) | 2003-02-12 |
Family
ID=17104008
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN98118664A Expired - Fee Related CN1101245C (en) | 1997-08-25 | 1998-08-24 | liquid bleeding device and method for controlling concentration of slurry in wet flue gas desulfurization system |
Country Status (5)
| Country | Link |
|---|---|
| KR (1) | KR100294625B1 (en) |
| CN (1) | CN1101245C (en) |
| CZ (1) | CZ289292B6 (en) |
| TR (1) | TR199801656A3 (en) |
| TW (1) | TW380056B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106891963A (en) * | 2017-03-19 | 2017-06-27 | 张新 | For the equipment and device of double suspensions of transporting children |
| CN113578015A (en) * | 2020-04-30 | 2021-11-02 | 中国石油天然气股份有限公司 | Desulfurizing device |
| CN114867544A (en) * | 2020-07-15 | 2022-08-05 | 富士电机株式会社 | Exhaust gas treatment device |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115201149B (en) * | 2022-07-22 | 2025-06-10 | 山西北方兴安化学工业有限公司 | Nitrocotton water suspension concentration detection system based on near infrared spectrum |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4362628A (en) * | 1980-07-23 | 1982-12-07 | Methods Engineering, Inc. | Method and apparatus for cleaning basins |
| CN2030106U (en) * | 1988-04-02 | 1989-01-04 | 于忠民 | Gravity separator for solid oil and water |
| CA2104648C (en) * | 1992-08-24 | 2000-06-20 | Richard Guy Batson | Process for treating a suspension of solid particles in a carrier liquid |
| FR2725143B1 (en) * | 1994-10-04 | 1999-08-06 | Degremont | LONGITUDINAL DECANTER WITH FLOW SEPARATION |
-
1998
- 1998-06-15 TW TW087109499A patent/TW380056B/en not_active IP Right Cessation
- 1998-08-24 CZ CZ19982690A patent/CZ289292B6/en not_active IP Right Cessation
- 1998-08-24 CN CN98118664A patent/CN1101245C/en not_active Expired - Fee Related
- 1998-08-24 KR KR1019980034273A patent/KR100294625B1/en not_active Expired - Fee Related
- 1998-08-25 TR TR1998/01656A patent/TR199801656A3/en unknown
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106891963A (en) * | 2017-03-19 | 2017-06-27 | 张新 | For the equipment and device of double suspensions of transporting children |
| CN113578015A (en) * | 2020-04-30 | 2021-11-02 | 中国石油天然气股份有限公司 | Desulfurizing device |
| CN113578015B (en) * | 2020-04-30 | 2024-04-30 | 中国石油天然气股份有限公司 | Desulfurization device |
| CN114867544A (en) * | 2020-07-15 | 2022-08-05 | 富士电机株式会社 | Exhaust gas treatment device |
Also Published As
| Publication number | Publication date |
|---|---|
| CZ289292B6 (en) | 2001-12-12 |
| HK1020897A1 (en) | 2000-05-26 |
| KR100294625B1 (en) | 2001-09-17 |
| KR19990023823A (en) | 1999-03-25 |
| TW380056B (en) | 2000-01-21 |
| CZ269098A3 (en) | 1999-07-14 |
| TR199801656A2 (en) | 1999-10-21 |
| TR199801656A3 (en) | 1999-10-21 |
| CN1101245C (en) | 2003-02-12 |
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