CN104085944B - One-level de-aerator plant is reclaimed in the mixing of water of condensation de-mineralized water - Google Patents
One-level de-aerator plant is reclaimed in the mixing of water of condensation de-mineralized water Download PDFInfo
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- CN104085944B CN104085944B CN201410261535.4A CN201410261535A CN104085944B CN 104085944 B CN104085944 B CN 104085944B CN 201410261535 A CN201410261535 A CN 201410261535A CN 104085944 B CN104085944 B CN 104085944B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 321
- 238000009833 condensation Methods 0.000 title claims abstract description 65
- 230000005494 condensation Effects 0.000 title claims abstract description 65
- 238000002156 mixing Methods 0.000 title claims abstract description 46
- 238000005276 aerator Methods 0.000 title claims abstract description 18
- 239000010865 sewage Substances 0.000 claims abstract description 50
- 238000001816 cooling Methods 0.000 claims abstract description 34
- 238000011033 desalting Methods 0.000 claims abstract description 34
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 29
- 238000001354 calcination Methods 0.000 claims abstract description 19
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 14
- 238000006243 chemical reaction Methods 0.000 claims abstract description 14
- 230000000630 rising effect Effects 0.000 claims abstract description 10
- 238000005070 sampling Methods 0.000 claims description 13
- 239000007788 liquid Substances 0.000 claims description 6
- 238000007789 sealing Methods 0.000 claims description 6
- 230000002093 peripheral effect Effects 0.000 claims description 3
- 239000002585 base Substances 0.000 description 20
- 238000006392 deoxygenation reaction Methods 0.000 description 19
- 239000007789 gas Substances 0.000 description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 9
- 239000012535 impurity Substances 0.000 description 9
- 239000001301 oxygen Substances 0.000 description 9
- 229910052760 oxygen Inorganic materials 0.000 description 9
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical compound O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000004134 energy conservation Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000004880 explosion Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 230000003020 moisturizing effect Effects 0.000 description 3
- 239000003513 alkali Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000007664 blowing Methods 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910003460 diamond Inorganic materials 0.000 description 1
- 239000010432 diamond Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
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- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
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Abstract
The present invention relates to the mixing of a kind of water of condensation de-mineralized water and reclaim one-level de-aerator plant, comprise calcining furnace water of condensation, fluidized-bed water of condensation, synthetic ammonia cooling and desalting water and conversion cooling and desalting water, pressure-bearing surge tank is circumferentially connected with the first, the 3rd water inlet pipe being positioned at upper strata, and is positioned at the second, the 4th water inlet pipe of lower floor; Synthetic ammonia cooling and desalting water and conversion cooling and desalting water access first and the 3rd water inlet pipe respectively, and calcining furnace water of condensation and fluidized-bed water of condensation access second and the 4th water inlet pipe respectively; Be connected with surge tank steam discharge pipe in the middle part of the roof of pressure-bearing surge tank and reverse checkvalve and the first control valve are installed from lower to upper successively; The lower end of surge tank rising pipe is connected with the entrance of the first water pump through the base plate of pressure-bearing surge tank, and the first water pump outlet accesses boiler replenishing water pipe; The base plate of pressure-bearing surge tank is provided with sewage draining exit, and sewage draining exit is connected with blow-off pipe, blow-off pipe is provided with the second control valve.This device condensation water residual heat utilization ratio is high and reliable.
Description
Technical field
The present invention relates to the mixing of a kind of water of condensation de-mineralized water and reclaim one-level de-aerator plant, can be used for the recovery of the high-temperature condensation water of alkali factory production line generation and the de-mineralized water through heating.
Background technology
For preventing heat power equipment and corrosive pipeline thereof, and prevent non-condensable gases to be mixed into steam and reduce steam quality, must remove and be dissolved in dissolved oxygen in boiler replenishing water and other non-condensable gases, realize often through deoxygenator.According to Henry's law and Dalton's law, for the various gases be dissolved in the water, under pressure, the temperature of water is higher, and solubleness is lower; Or under pressure, the pressure component of gas is lower, and the solubleness of this gas is lower.Thermal de-aeration is exactly when boiler replenishing water is heated to the temperature of saturation under corresponding pressure, vapor partial pressure power will close to total pressure on the water surface, the pressure component of various gas soluble in water is close to zero, therefore, water does not just have the ability of gas dissolved, gas soluble in water is just precipitated, thus the oxygen removed in water and other gases.Thermal deaerator comprises deoxygenation head and deoxygenation case, deoxygenation head is positioned at deoxygenation upper box part, the side wall upper part of deoxygenation head is connected with deoxygenation head water inlet pipe, the lower sidewall of deoxygenation head is connected with deoxygenation vapour pipe, the top of deoxygenation head is connected with deoxygenation head steam discharge pipe, and the bottom of deoxygenation case is connected with deoxygenation case water shoot.
In alkali factory production line, because a large amount of steam that uses can produce a lot of water of condensation, as calcining furnace water of condensation, fluidized-bed water of condensation and dry ammonium water of condensation etc., the temperature of water of condensation after flash distillation utilizes still has 135 DEG C ~ 155 DEG C.In addition, synthetic ammonia and shift conversion step can use a large amount of de-mineralized waters as indirect cooling water, the temperature about 60 DEG C ~ 80 DEG C of the synthetic ammonia cooling and desalting water after heating, through the temperature about 60 DEG C ~ 95 DEG C of the conversion cooling and desalting water of heating.Because of the water of condensation that produces and the temperature of cooling and desalting water higher, water quality meets again the requirement of boiler replenishing water, Ge Jian factory often by above steam condensate and cooling and desalting Water Sproading in the deoxygenation case of atmospheric type deaerator, then deliver to boiler as boiler replenishing water by deoxygenation case by water pump.
There is following weak point in above way of recycling: 1. deoxygenator is air suspended type, working temperature about 104 DEG C, and water of condensation and the mixed actual temperature of de-mineralized water are considerably beyond 104 DEG C, therefore excess portion by deoxygenation head and a large amount of kiting of flash tank be communicated with deoxygenator, can only waste a large amount of residual heat resources and water resources.2. greatly, by direct contact heat transfer, heat is difficult to reaching balance instantaneously, therefore easily produces thermal explosion in deoxygenation case, affects equipment safety operation for water of condensation and the de-mineralized water temperature difference.3. there is contradiction in the continuity that the intermittence of boiler replenishing water and water of condensation produce: when boiler not moisturizing or rate of water make-up little time, the valve opening that calcining furnace water of condensation enters deoxygenator is less, and system builds the pressure, and calcining fire grate water of condensation is not smooth; When a large amount of moisturizing of boiler, the valve opening that calcining furnace water of condensation enters deoxygenator is large, and system back pressure reduces, and calcining furnace steam string, to deoxygenator, aggravates the discharge of waste heat.4. deoxygenation case limited volume, can not form effectively buffering between boiler unit and productive unit.
Summary of the invention
The object of the invention is to, overcome problems of the prior art, provide a kind of water of condensation de-mineralized water to mix and reclaim one-level de-aerator plant, condensation water residual heat utilization ratio is high and can guarantee that the fluctuation of boiler replenishing water does not affect the normal operation with vapour unit.
For solving above technical problem, one-level de-aerator plant is reclaimed in a kind of water of condensation de-mineralized water mixing of the present invention, comprise the calcining furnace water of condensation of 135 DEG C ~ 155 DEG C, the fluidized-bed water of condensation of 135 DEG C ~ 155 DEG C, the conversion cooling and desalting water of the synthetic ammonia cooling and desalting water of 60 DEG C ~ 80 DEG C and 60 DEG C ~ 95 DEG C, also comprise closed pressure-bearing surge tank, described pressure-bearing surge tank be circumferentially vertically connected with the first water inlet pipe, second water inlet pipe, 3rd water inlet pipe and the 4th water inlet pipe, described first water inlet pipe is relative with the mouth of pipe of the 3rd water inlet pipe and short transverse staggers mutually, described second water inlet pipe is relative with the mouth of pipe of the 4th water inlet pipe and short transverse staggers mutually, the height of described first water inlet pipe and the 3rd water inlet pipe is higher than described second water inlet pipe and the 4th water inlet pipe, described synthetic ammonia cooling and desalting water and conversion cooling and desalting water access described first water inlet pipe and the 3rd water inlet pipe respectively, and described calcining furnace water of condensation and fluidized-bed water of condensation access described second water inlet pipe and the 4th water inlet pipe respectively, be connected with surge tank steam discharge pipe in the middle part of the roof of described pressure-bearing surge tank, described surge tank steam discharge pipe is provided with reverse checkvalve and the first control valve from lower to upper successively, be provided with the surge tank rising pipe of opening upwards in described pressure-bearing surge tank, the lower end of described surge tank rising pipe is connected with the entrance of the first water pump through the base plate of pressure-bearing surge tank, and described first water pump outlet accesses boiler replenishing water pipe, the base plate of described pressure-bearing surge tank is provided with sewage draining exit, and described sewage draining exit is connected with blow-off pipe, described blow-off pipe is provided with the second control valve.
Relative to prior art, the present invention achieves following beneficial effect: (1) calcining furnace water of condensation, fluidized-bed water of condensation, synthetic ammonia cooling and desalting water and conversion cooling and desalting water enter in pressure-bearing surge tank respectively, discharge from surge tank rising pipe after mixing, send into boiler replenishing water pipe by the first water pump; The non-condensable gasess such as the flash-off steam produced above the water surface and the oxygen of spilling are discharged from the surge tank steam discharge pipe at pressure-bearing surge tank top.(2) pressure-bearing surge tank can bear certain pressure and water level can adjust in a big way, the contradiction between continuity that the intermittence of boiler replenishing water and water of condensation produce can be made up, isolating with being formed between vapour unit and boiler replenishing water system and cushioning, guarantee that the fluctuation of boiler replenishing water does not affect the normal operation with vapour unit, avoid when boiler replenishing water amount hour, water of condensation pipe network back pressure is high, and calcining furnace and fluidised bed system occur that the row's of building the pressure water of condensation is not smooth; It also avoid when a large amount of moisturizing of boiler, water of condensation pipe network back pressure is low, and the steam string of calcining furnace and fluidised bed system, to deoxygenator, aggravates the discharge of waste heat.(3) the temperature of synthetic ammonia cooling and desalting water and conversion cooling and desalting water is slightly low and containing non-condensable gasess such as oxygen, calcining furnace water of condensation and the high and non-condensable gasess such as oxygen-free gas of fluidized-bed condensate temperature, after cooling and desalting water mixes with steam condensate, temperature rises, and the pressure-bearing surge tank operating pressure saturation pressure that to be pressure-bearing surge tank mixing water temperature corresponding, the pressure component of oxygen and other non-condensable gases is close to zero, solubleness is close to zero, discharge from surge tank steam discharge pipe with exhaust steam after overflowing the water surface, thus reach the object of deoxygenation.(4) the reverse checkvalve on surge tank steam discharge pipe can guarantee that air can not pour in down a chimney in pressure-bearing surge tank, prevents from introducing extraneous oxygen.(5) the first control valve is by controlling the quantity discharged of exhaust steam, makes to maintain certain pressure in pressure-bearing surge tank, fully to receive the heat of water of condensation and de-mineralized water, reduces the loss of exhaust steam discharge and heat, not only energy-conservation but also environmental protection.(6) improve boiler replenishing water temperature, reduce unit steam coal consumption.(7) the first water inlet pipe that the cooling and desalting water that temperature is relatively low, density is higher is higher from position and the 3rd water inlet pipe enter, the second water inlet pipe that the water of condensation that temperature is relatively high, density is lower is lower from position and the 4th water inlet pipe enter pressure-bearing surge tank, natural convection can be formed in pressure-bearing surge tank, promote abundant heat exchange.(8) along with the increase of working hour, can gather certain impurity bottom pressure-bearing surge tank, water quality can decline, and now can open the second control valve, discharges the water of water degradation, guarantee boiler replenishing water water quality from blow-off pipe.
As preferred version of the present invention, the annular water distributor that the mouth of pipe that described first water inlet pipe, the second water inlet pipe, the 3rd water inlet pipe and the 4th water inlet pipe are positioned at pressure-bearing surge tank is connected to along the horizontal plane and the inner peripheral wall of pressure-bearing surge tank extends, the middle and lower part of each described annular water distributor is evenly distributed with the jet hole of the axis jet to pressure-bearing surge tank respectively, the axis of each described jet hole become 30 ° ~ 45 ° angles with horizontal plane and respectively with the axes intersect of pressure-bearing surge tank.The water inlet of every road is all by ring pipe water outlet in the tank that arranges jet hole, and current blowing perforation oliquely downward sprays, and contacts with water body in tank with parabolical, extends the duration of contact with water body in tank, realizes abundant heat exchange, avoid thermal explosion.
As preferred version of the present invention, the inner chamber middle and lower part of described pressure-bearing surge tank is provided with Forced Mixing impeller, described Forced Mixing impeller is fixedly connected on Forced Mixing impeller shaft, described Forced Mixing impeller shaft vertically downward through pressure-bearing surge tank base plate and and realize sealing pressure-bearing surge tank base plate, the lower end of described Forced Mixing impeller shaft is connected with Forced Mixing impeller drive motor.When the temperature difference of water of condensation and cooling and desalting water is larger, only by natural heat-exchange, in tank, temperature is still difficult to be evenly distributed, and easily in pressure-bearing surge tank, formation temperature is poor, now open Forced Mixing impeller and Forced Mixing is carried out to tank inner storing water, promote the homogeneity of temperature distribution in tank.
As preferred version of the present invention, the intracavity bottom of described pressure-bearing surge tank is provided with disturbance impeller, described disturbance impeller is fixedly connected on disturbance impeller shaft, described disturbance impeller shaft vertically downward through pressure-bearing surge tank base plate and and realize sealing pressure-bearing surge tank base plate, the lower end of described disturbance impeller shaft is connected with disturbance impeller drive motor; Described disturbance impeller shaft departs from the axis of described pressure-bearing surge tank, and the plate inner wall of described pressure-bearing surge tank is provided with eddy current baffle plate, and described eddy current baffle plate is perpendicular to base plate and extend along base plate diametric(al).When needs blowdown, impurity often accumulates in the bottom of pressure-bearing surge tank, is difficult to discharge with current, now opens disturbance impeller and impurity can be flashed by bottom water flow rotation; If current are stable circulation state, then good not to the disturbance effect of impurity, disturbance impeller shaft of the present invention departs from the axis of pressure-bearing surge tank, can avoid making current present stable circulation state; The eddy current baffle plate that plate inner wall is installed thoroughly can destroy circulation more, makes current occur turbulence state, is more conducive to disturbance and the discharge of impurity.
As preferred version of the present invention, described sewage draining exit is provided with multiple, be divided into inner ring sewage draining exit and outer ring sewage draining exit two groups, each inner ring sewage draining exit to be evenly distributed on close to pressure-bearing surge tank axis circumferentially, each outer ring sewage draining exit to be evenly distributed on away from pressure-bearing surge tank axis circumferentially, and each inner ring sewage draining exit and each outer ring sewage draining exit are distributed on the different diameter of base plate.Multiple orientation of base plate distribute more sewage draining exit, can improve contaminant removal effectiveness, reduce water displacement.
As preferred version of the present invention, described inner ring sewage draining exit and outer ring sewage draining exit are respectively provided with four, and the angle between each inner ring sewage draining exit place diameter and adjacent sewage draining exit place, outer ring diameter is 45 °.Inner ring sewage draining exit and outer ring sewage draining exit staggered in a circumferential direction, centered by pressure-bearing surge tank axis, be equipped with sewage draining exit to extraradial eight directions, blowdown can be made more evenly rationally, better effects if, within the shortest time, get rid of as far as possible many dirts, reduce water displacement.
As preferred version of the present invention, the intracavity bottom of described pressure-bearing surge tank is provided with sampling tube, it is outer and be connected with sampling water cooler that described sampling tube stretches out pressure-bearing surge tank, the export pipeline of described sampling water cooler is provided with online electric conductivity detector and online Ph value detector.In-tank mixing electrical conductivity of water and Ph value can be detected in real time.
As preferred version of the present invention, the signal wire of described online electric conductivity detector and online Ph value detector accesses the corresponding signal input terminus of PLC respectively, and the corresponding signal output terminal of described PLC is connected with the control line of described second control valve; When PLC detects that the Ph value that specific conductivity that online electric conductivity detector provides is greater than set(ting)value or online Ph value detector and provides controls the second control valve when exceeding setting range and opens, control the second control valve closedown when PLC detects that specific conductivity that online electric conductivity detector provides is less than set(ting)value and the Ph value that provides of Ph value detector is in setting range online.The specific conductivity that PLC can provide according to online electric conductivity detector and the Ph value that online Ph value detector provides, the keying of automatic control disturbance impeller and the second control valve, improves the automatization level of system.
As preferred version of the present invention, described first water inlet pipe, the second water inlet pipe, the 3rd water inlet pipe and the 4th water inlet pipe are separately installed with temperature sensor and under meter, different azimuth and the different heights of the liquid Space of described pressure-bearing surge tank are provided with multiple temperature sensor altogether, and the gas-phase space of described pressure-bearing surge tank is provided with pressure transmitter.Temperature sensor can detect the water temperature of each water inlet pipe and pressure-bearing surge tank, and under meter can measure the actual flow of each water inlet pipe.
As preferred version of the present invention, the signal wire of described pressure transmitter, each described temperature sensor and each described under meter accesses the corresponding signal input terminus of PLC respectively, and the corresponding signal output terminal of described PLC is connected with the control line of described first control valve; The aperture controlling the first control valve when PLC detects t>t0 or p>p0 strengthens, and the aperture controlling the first control valve when PLC detects t<t0 or p<p0 reduces; Wherein t each temperature sensor that is described pressure-bearing surge tank liquid Space survey the mean value of water temperature, the force value that p surveys for described pressure transmitter; T0 is the set temperature value of PLC, and t0=(t1 × m1+t2 × m2+t3 × m3+t4 × m4) ÷ (m1+m2+m3+m4) × safety coefficient, t1, t2, t3 and t4 are respectively the water temperature that the temperature sensor on first, second, third and fourth water inlet pipe detects, and m1, m2, m3 and m4 are respectively the flow measured by the under meter on first, second, third and fourth water inlet pipe; P0 is the setup pressure value of PLC, and p0 is the saturation pressure force value of water vapor corresponding at t0 temperature, and safety coefficient gets 0.8 ~ 0.95.The set temperature value of PLC gets the weighted mean water temperature t0 of each water inlet pipe, there is one-to-one relationship in the saturation pressure p0 of water vapor and water temperature t0, when temperature in tank is greater than design temperature or tank internal pressure is greater than setting pressure, the aperture that PLC controls the first control valve strengthens, to strengthen the discharge of exhaust steam; When temperature in tank lower than design temperature or tank internal pressure lower than setting pressure time, the aperture that PLC controls the first control valve reduces, and prevents that steam discharge is excessive even occurs that tank outer air is poured in down a chimney; Adopt PLC automatically to regulate the aperture of the first control valve according to water temperature and pressure, improve the automatization level of system, avoid the excess emitters of exhaust steam, under guaranteeing that pressure-bearing surge tank is operated in the peak pressure/temperature of permission, not only energy-conservation but also environmental protection.
Accompanying drawing explanation
Below in conjunction with the drawings and specific embodiments, the present invention is further detailed explanation, and accompanying drawing only provides reference and explanation use, is not used to limit the present invention.
Fig. 1 is the schematic diagram that one-level de-aerator plant is reclaimed in water of condensation de-mineralized water of the present invention mixing.
Fig. 2 is the part sectioned view at pressure-bearing surge tank the 3rd water inlet pipe position in the present invention.
Fig. 3 is the base plate vertical view of pressure-bearing surge tank in the present invention.
In figure: PLC.PLC controller; E1. pressure-bearing surge tank; E1a. sewage draining exit; E1b. eddy current baffle plate; E1c. Forced Mixing impeller; E1d. disturbance impeller; E1e. sampling tube; G1. the first water inlet pipe; G2. the second water inlet pipe; G3. the 3rd water inlet pipe; G4. the 4th water inlet pipe; G5. surge tank steam discharge pipe; G6. surge tank rising pipe; G7. blow-off pipe; Vd. reverse checkvalve; V1. the first control valve; B1. the first water pump; T1. the first temperature sensor; T2. the second temperature sensor; T3. three-temperature sensor; T4. the 4th temperature sensor; T5. the 5th temperature sensor; T6. the 6th temperature sensor; T7. the 7th temperature sensor; T8. the 8th temperature sensor; P. pressure transmitter; V2. the second control valve; M1. first-class gauge; M2. second gauge; M3. the 3rd under meter; M4. the 4th under meter; Q. to sample water cooler; Q1. online electric conductivity detector; Q2. online Ph value detector.
Embodiment
As shown in Figure 1, one-level de-aerator plant is reclaimed in water of condensation de-mineralized water mixing of the present invention, comprise the conversion cooling and desalting water of the calcining furnace water of condensation of 135 DEG C ~ 155 DEG C, the fluidized-bed water of condensation of 135 DEG C ~ 155 DEG C, the synthetic ammonia cooling and desalting water of 60 DEG C ~ 80 DEG C and 60 DEG C ~ 95 DEG C, also comprise closed pressure-bearing surge tank E1.Pressure-bearing surge tank E1 is circumferentially vertically connected with the first water inlet pipe G1, the second water inlet pipe G2, the 3rd water inlet pipe G3 and the 4th water inlet pipe G4, first water inlet pipe G1 is relative with the mouth of pipe of the 3rd water inlet pipe G3 and short transverse staggers mutually, second water inlet pipe G2 is relative with the mouth of pipe of the 4th water inlet pipe G4 and short transverse staggers mutually, and the height of the first water inlet pipe G1 and the 3rd water inlet pipe G3 is higher than the second water inlet pipe G2 and the 4th water inlet pipe G4.Synthetic ammonia cooling and desalting water and conversion cooling and desalting water access the first water inlet pipe G1 and the 3rd water inlet pipe G3 respectively, and calcining furnace water of condensation and fluidized-bed water of condensation access the second water inlet pipe G2 and the 4th water inlet pipe G4 respectively; Be connected with surge tank steam discharge pipe G5 in the middle part of the roof of pressure-bearing surge tank E1, surge tank steam discharge pipe G5 be provided with from lower to upper successively reverse checkvalve Vd and the first control valve V1; Be provided with the surge tank rising pipe G6 of opening upwards in pressure-bearing surge tank E1, the lower end of surge tank rising pipe G6 is connected with the entrance of the first water pump B1 through the base plate of pressure-bearing surge tank E1, and the outlet of the first water pump B1 accesses boiler replenishing water pipe; The base plate of pressure-bearing surge tank E1 is provided with sewage draining exit E1a, and sewage draining exit E1a is connected with blow-off pipe G7, blow-off pipe G7 is provided with the second control valve V2.
The synthetic ammonia cooling and desalting water that during work, temperature is relatively low, density is higher and higher from position respectively the first water inlet pipe G1 of conversion cooling and desalting water and the 3rd water inlet pipe G3 enter; The second water inlet pipe G2 that the calcining furnace water of condensation that temperature is relatively high, density is lower and fluidized-bed water of condensation are lower from position and the 4th water inlet pipe G4 enters pressure-bearing surge tank E1, can form natural convection, promote abundant heat exchange in pressure-bearing surge tank.Discharge from surge tank rising pipe G6 after cooling and desalting water mixes with water of condensation, send into boiler replenishing water pipe by the first water pump B1.The temperature of synthetic ammonia cooling and desalting water and conversion cooling and desalting water is slightly low and containing non-condensable gasess such as oxygen, calcining furnace water of condensation and the high and non-condensable gasess such as oxygen-free gas of fluidized-bed condensate temperature, after cooling and desalting water mixes with steam condensate, temperature rises, and the pressure-bearing surge tank E1 operating pressure saturation pressure that to be pressure-bearing surge tank mixing water temperature corresponding, the pressure component of oxygen and other non-condensable gases is close to zero, solubleness is close to zero, discharge from surge tank steam discharge pipe G5 with exhaust steam after overflowing the water surface, thus reach the object of deoxygenation.Reverse checkvalve Vd on surge tank steam discharge pipe G5 can guarantee that air can not pour in down a chimney in pressure-bearing surge tank E1, prevents from introducing extraneous oxygen.First control valve V1 can control the quantity discharged of exhaust steam, make to maintain certain pressure in pressure-bearing surge tank E1, fully to receive the heat of water of condensation and de-mineralized water, reduce the loss of exhaust steam discharge and heat, improve boiler replenishing water temperature, reduce unit steam coal consumption.Along with the increase of working hour, can gather certain impurity bottom pressure-bearing surge tank E1, water quality can decline, and now can open the second control valve V2, from the water that blow-off pipe G7 discharges water degradation, guarantees boiler replenishing water water quality.
As improvement, first water inlet pipe G1 is provided with the first temperature sensor T1 and first-class gauge M1, second water inlet pipe G2 is provided with the second temperature sensor T2 and second gauge M2,3rd water inlet pipe G3 is provided with three-temperature sensor T3 and the 3rd under meter M3, the 4th water inlet pipe G4 is provided with the 4th temperature sensor T4 and the 4th under meter M4.Different azimuth and the different heights of the liquid Space of pressure-bearing surge tank E1 are provided with multiple temperature sensor altogether, such as, be separately installed with the 5th temperature sensor T5, the 6th temperature sensor T6, the 7th temperature sensor T7 and the 8th temperature sensor T8 at height different sites.The gas-phase space of pressure-bearing surge tank E1 is also provided with pressure transmitter P.
For improving the automatization level of system, the signal wire of the first temperature sensor T1, the second temperature sensor T2, three-temperature sensor T3, the 4th temperature sensor T4, the 5th temperature sensor T5, the 6th temperature sensor T6, the 7th temperature sensor T7, the 8th temperature sensor T8, first-class gauge M1, second gauge M2, the 3rd under meter M3, the 4th under meter M4 and pressure transmitter P accesses the corresponding signal input terminus of PLC respectively, and the corresponding signal output terminal of PLC is connected with the control line of the first control valve V1.
The aperture controlling the first control valve V1 when PLC detects t>t0 or p>p0 strengthens, and the aperture controlling the first control valve V1 when PLC detects t<t0 or p<p0 reduces; Wherein t each temperature sensor that is pressure-bearing surge tank liquid Space survey the mean value of water temperature, such as the 5th temperature sensor T5, the 6th temperature sensor T6, the 7th temperature sensor T7 and the 8th temperature sensor T8 survey the mean value of water temperature; The force value that p surveys for pressure transmitter P; T0 is the set temperature value of PLC, and t0=(t1 × m1+t2 × m2+t3 × m3+t4 × m4) ÷ (m1+m2+m3+m4) × safety coefficient, t1, t2, t3 and t4 are respectively the water temperature that the first temperature sensor T1, the second temperature sensor T2, three-temperature sensor T3 and the 4th temperature sensor T4 detect, and m1, m2, m3 and m4 are respectively first-class gauge M1, second gauge M2, the 3rd under meter M3 and the flow measured by the 4th under meter M4.P0 is the setup pressure value of PLC, and p0 is the saturation pressure force value of water vapor corresponding at t0 temperature, and safety coefficient gets 0.8 ~ 0.95.
The set temperature value of PLC gets the weighted mean water temperature t0 of each water inlet pipe, there is one-to-one relationship in the saturation pressure p0 of water vapor and water temperature t0, when temperature in tank is greater than design temperature or tank internal pressure is greater than setting pressure, the aperture that PLC controls the first control valve V1 strengthens, to strengthen the discharge of exhaust steam; When temperature in tank lower than design temperature or tank internal pressure lower than setting pressure time, the aperture that PLC controls the first control valve V1 reduces, and prevents that steam discharge is excessive even occurs that tank outer air is poured in down a chimney.Adopt PLC automatically to regulate the aperture of the first control valve V1 according to water temperature and pressure, improve the automatization level of system, avoid the excess emitters of exhaust steam, under guaranteeing that pressure-bearing surge tank is operated in the peak pressure/temperature of permission, not only energy-conservation but also environmental protection.
The intracavity bottom of pressure-bearing surge tank E1 can be provided with sampling tube E1e, it is outer and be connected with sampling water cooler Q that sampling tube E1e stretches out pressure-bearing surge tank E1, the export pipeline of sampling water cooler Q is provided with online electric conductivity detector Q1 and online Ph value detector Q2, to detect in-tank mixing electrical conductivity of water and Ph value in real time.
For improving the automatization level of system, the signal wire of online electric conductivity detector Q1 and online Ph value detector Q2 accesses the corresponding signal input terminus of PLC respectively, and the corresponding signal output terminal of PLC is connected with the control line of the second control valve V2; When PLC detects that the Ph value that specific conductivity that online electric conductivity detector Q1 provides is greater than set(ting)value or online Ph value detector Q2 and provides controls the second control valve V2 when exceeding setting range and opens, when PLC detect specific conductivity that online electric conductivity detector Q1 provides be less than set(ting)value and the Ph value that provides of online Ph value detector Q2 in setting range time control the second control valve V2 and close, realize the Ph value that the specific conductivity that provides according to online electric conductivity detector Q1 and online Ph value detector Q2 provide, the keying of automatic control the second control valve V2.
As shown in Figure 2, as improvement, the annular water distributor that the mouth of pipe that first water inlet pipe G1, the second water inlet pipe G2, the 3rd water inlet pipe G3 and the 4th water inlet pipe G4 are positioned at pressure-bearing surge tank is connected to along the horizontal plane and the inner peripheral wall of pressure-bearing surge tank extends, for the 3rd water inlet pipe G3 in Fig. 2, the middle and lower part of each annular water distributor is evenly distributed with the jet hole of the axis jet to pressure-bearing surge tank respectively, the axis of each jet hole become 30 ° ~ 45 ° angles with horizontal plane and respectively with the axes intersect of pressure-bearing surge tank.The water inlet of every road is all by ring pipe water outlet in the tank that arranges jet hole, and current blowing perforation oliquely downward sprays, and contacts with water body in tank with parabolical, extends the duration of contact with water body in tank, realizes abundant heat exchange, avoid thermal explosion.
As shown in Figure 1, when the temperature difference of water of condensation and cooling and desalting water is larger, only by natural heat-exchange, in tank, temperature is still difficult to be evenly distributed, and easily in pressure-bearing surge tank E1, formation temperature is poor.Forced Mixing impeller E1c can be installed in the inner chamber middle and lower part of pressure-bearing surge tank, Forced Mixing impeller E1c is fixedly connected on Forced Mixing impeller shaft, Forced Mixing impeller shaft vertically downward through pressure-bearing surge tank base plate and and realize sealing pressure-bearing surge tank base plate, the lower end of Forced Mixing impeller shaft is connected with Forced Mixing impeller drive motor, and Forced Mixing impeller shaft is preferably placed on the axis of pressure-bearing surge tank.Open Forced Mixing impeller E1c and Forced Mixing is carried out to tank inner storing water, promote the homogeneity of temperature distribution in tank.
Because accumulation of impurities is in the bottom of pressure-bearing surge tank, be difficult to during blowdown discharge with current, at the intracavity bottom of pressure-bearing surge tank, disturbance impeller E1d can be installed, disturbance impeller E1d is fixedly connected on disturbance impeller shaft, disturbance impeller shaft vertically downward through pressure-bearing surge tank base plate and and realize sealing pressure-bearing surge tank base plate, the lower end of disturbance impeller shaft is connected with disturbance impeller drive motor, opens disturbance impeller E1d and impurity can be flashed by bottom water flow rotation, be beneficial to discharge.
Disturbance impeller shaft preferably departs from the axis of pressure-bearing surge tank, to avoid making current present stable circulation state.
As shown in Figure 3, as improvement, the plate inner wall of pressure-bearing surge tank can be provided with eddy current baffle plate E1b, eddy current baffle plate E1b is perpendicular to base plate and extend along base plate diametric(al), eddy current baffle plate E1b thoroughly can destroy circulation, makes current occur turbulence state, is more conducive to disturbance and the discharge of impurity.
Sewage draining exit E1a can be provided with multiple, such as be divided into inner ring sewage draining exit and outer ring sewage draining exit two groups, each inner ring sewage draining exit to be evenly distributed on close to pressure-bearing surge tank axis circumferentially, each outer ring sewage draining exit to be evenly distributed on away from pressure-bearing surge tank axis circumferentially, and each inner ring sewage draining exit and each outer ring sewage draining exit are distributed on the different diameter of pressure-bearing surge tank base plate.
Inner ring sewage draining exit and outer ring sewage draining exit are preferably respectively provided with four, inner ring sewage draining exit and outer ring sewage draining exit staggered in a circumferential direction, phase place staggers successively 45 ° and arrange, four inner ring sewage draining exits assume diamond in shape layout, four outer ring sewage draining exits are arranged in squares, and the angle between each inner ring sewage draining exit place diameter and adjacent sewage draining exit place, outer ring diameter is 45 °.
The foregoing is only the better possible embodiments of the present invention, non-ly therefore limit to scope of patent protection of the present invention.In addition to the implementation, the present invention can also have other embodiments.All employings are equal to the technical scheme of replacement or equivalent transformation formation, all drop in the protection domain of application claims.
Claims (10)
1. one-level de-aerator plant is reclaimed in a water of condensation de-mineralized water mixing, comprise the calcining furnace water of condensation of 135 DEG C ~ 155 DEG C, the fluidized-bed water of condensation of 135 DEG C ~ 155 DEG C, the conversion cooling and desalting water of the synthetic ammonia cooling and desalting water of 60 DEG C ~ 80 DEG C and 60 DEG C ~ 95 DEG C, it is characterized in that: also comprise closed pressure-bearing surge tank, described pressure-bearing surge tank be circumferentially vertically connected with the first water inlet pipe, second water inlet pipe, 3rd water inlet pipe and the 4th water inlet pipe, described first water inlet pipe is relative with the mouth of pipe of the 3rd water inlet pipe and short transverse staggers mutually, described second water inlet pipe is relative with the mouth of pipe of the 4th water inlet pipe and short transverse staggers mutually, the height of described first water inlet pipe and the 3rd water inlet pipe is higher than described second water inlet pipe and the 4th water inlet pipe, described synthetic ammonia cooling and desalting water and conversion cooling and desalting water access described first water inlet pipe and the 3rd water inlet pipe respectively, and described calcining furnace water of condensation and fluidized-bed water of condensation access described second water inlet pipe and the 4th water inlet pipe respectively, be connected with surge tank steam discharge pipe in the middle part of the roof of described pressure-bearing surge tank, described surge tank steam discharge pipe is provided with reverse checkvalve and the first control valve from lower to upper successively, be provided with the surge tank rising pipe of opening upwards in described pressure-bearing surge tank, the lower end of described surge tank rising pipe is connected with the entrance of the first water pump through the base plate of pressure-bearing surge tank, and described first water pump outlet accesses boiler replenishing water pipe, the base plate of described pressure-bearing surge tank is provided with sewage draining exit, and described sewage draining exit is connected with blow-off pipe, described blow-off pipe is provided with the second control valve.
2. one-level de-aerator plant is reclaimed in water of condensation de-mineralized water mixing according to claim 1, it is characterized in that: the annular water distributor that the mouth of pipe that described first water inlet pipe, the second water inlet pipe, the 3rd water inlet pipe and the 4th water inlet pipe are positioned at pressure-bearing surge tank is connected to along the horizontal plane and the inner peripheral wall of pressure-bearing surge tank extends, the middle and lower part of each described annular water distributor is evenly distributed with the jet hole of the axis jet to pressure-bearing surge tank respectively, the axis of each described jet hole become 30 ° ~ 45 ° angles with horizontal plane and respectively with the axes intersect of pressure-bearing surge tank.
3. one-level de-aerator plant is reclaimed in water of condensation de-mineralized water mixing according to claim 1, it is characterized in that: the inner chamber middle and lower part of described pressure-bearing surge tank is provided with Forced Mixing impeller, described Forced Mixing impeller is fixedly connected on Forced Mixing impeller shaft, described Forced Mixing impeller shaft vertically downward through pressure-bearing surge tank base plate and and realize sealing pressure-bearing surge tank base plate, the lower end of described Forced Mixing impeller shaft is connected with Forced Mixing impeller drive motor.
4. one-level de-aerator plant is reclaimed in water of condensation de-mineralized water mixing according to claim 1, it is characterized in that: the intracavity bottom of described pressure-bearing surge tank is provided with disturbance impeller, described disturbance impeller is fixedly connected on disturbance impeller shaft, described disturbance impeller shaft vertically downward through pressure-bearing surge tank base plate and and realize sealing pressure-bearing surge tank base plate, the lower end of described disturbance impeller shaft is connected with disturbance impeller drive motor; Described disturbance impeller shaft departs from the axis of described pressure-bearing surge tank, and the plate inner wall of described pressure-bearing surge tank is provided with eddy current baffle plate, and described eddy current baffle plate is perpendicular to base plate and extend along base plate diametric(al).
5. one-level de-aerator plant is reclaimed in water of condensation de-mineralized water mixing according to claim 1, it is characterized in that: described sewage draining exit is provided with multiple, be divided into inner ring sewage draining exit and outer ring sewage draining exit two groups, each inner ring sewage draining exit to be evenly distributed on close to pressure-bearing surge tank axis circumferentially, each outer ring sewage draining exit to be evenly distributed on away from pressure-bearing surge tank axis circumferentially, and each inner ring sewage draining exit and each outer ring sewage draining exit are distributed on the different diameter of base plate.
6. one-level de-aerator plant is reclaimed in water of condensation de-mineralized water mixing according to claim 5, it is characterized in that: described inner ring sewage draining exit and outer ring sewage draining exit are respectively provided with four, the angle between each inner ring sewage draining exit place diameter and adjacent sewage draining exit place, outer ring diameter is 45 °.
7. one-level de-aerator plant is reclaimed in water of condensation de-mineralized water mixing according to claim 1, it is characterized in that: the intracavity bottom of described pressure-bearing surge tank is provided with sampling tube, it is outer and be connected with sampling water cooler that described sampling tube stretches out pressure-bearing surge tank, the export pipeline of described sampling water cooler is provided with online electric conductivity detector and on-line pH value detector.
8. one-level de-aerator plant is reclaimed in water of condensation de-mineralized water mixing according to claim 7, it is characterized in that: the signal wire of described online electric conductivity detector and on-line pH value detector accesses the corresponding signal input terminus of PLC respectively, the corresponding signal output terminal of described PLC is connected with the control line of described second control valve; When PLC detects that the pH value that specific conductivity that online electric conductivity detector provides is greater than set(ting)value or on-line pH value detector and provides controls the second control valve when exceeding setting range and opens, when PLC detect specific conductivity that online electric conductivity detector provides be less than set(ting)value and the pH value that provides of on-line pH value detector in setting range time control the second control valve and close.
9. one-level de-aerator plant is reclaimed in water of condensation de-mineralized water mixing according to claim 1, it is characterized in that: described first water inlet pipe, the second water inlet pipe, the 3rd water inlet pipe and the 4th water inlet pipe are separately installed with temperature sensor and under meter, different azimuth and the different heights of the liquid Space of described pressure-bearing surge tank are provided with multiple temperature sensor altogether, and the gas-phase space of described pressure-bearing surge tank is provided with pressure transmitter.
10. one-level de-aerator plant is reclaimed in water of condensation de-mineralized water mixing according to claim 9, it is characterized in that: the signal wire of described pressure transmitter, each described temperature sensor and each described under meter accesses the corresponding signal input terminus of PLC respectively, and the corresponding signal output terminal of described PLC is connected with the control line of described first control valve; The aperture controlling the first control valve when PLC detects t>t0 or p>p0 strengthens, and the aperture controlling the first control valve when PLC detects t<t0 or p<p0 reduces; Wherein t each temperature sensor that is described pressure-bearing surge tank liquid Space survey the mean value of water temperature, the force value that p surveys for described pressure transmitter; T0 is the set temperature value of PLC, and t0=(t1 × m1+t2 × m2+t3 × m3+t4 × m4) ÷ (m1+m2+m3+m4) × safety coefficient, t1, t2, t3 and t4 are respectively the water temperature that the temperature sensor on first, second, third and fourth water inlet pipe detects, and m1, m2, m3 and m4 are respectively the flow measured by the under meter on first, second, third and fourth water inlet pipe; P0 is the setup pressure value of PLC, and p0 is the saturation pressure force value of water vapor corresponding at t0 temperature, and safety coefficient gets 0.8 ~ 0.95.
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| CN201410261535.4A CN104085944B (en) | 2014-06-13 | 2014-06-13 | One-level de-aerator plant is reclaimed in the mixing of water of condensation de-mineralized water |
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| CN201410261535.4A CN104085944B (en) | 2014-06-13 | 2014-06-13 | One-level de-aerator plant is reclaimed in the mixing of water of condensation de-mineralized water |
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| CN104085944B true CN104085944B (en) | 2016-01-27 |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH01203906A (en) * | 1988-02-10 | 1989-08-16 | Brother Ind Ltd | Optical fiber sensor device |
| JPH0727304A (en) * | 1993-07-08 | 1995-01-27 | Takuma Co Ltd | Boiler water feeding system |
| CN201059546Y (en) * | 2007-07-05 | 2008-05-14 | 王嘉贤 | Device for recycling and transmitting device in enclosed type high-temperature condensate water and water collection pot |
| CN204039093U (en) * | 2014-06-13 | 2014-12-24 | 江苏巴威节能服务有限公司 | One-level deaerating type of cycles is reclaimed in the mixing of water of condensation de-mineralized water |
-
2014
- 2014-06-13 CN CN201410261535.4A patent/CN104085944B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH01203906A (en) * | 1988-02-10 | 1989-08-16 | Brother Ind Ltd | Optical fiber sensor device |
| JPH0727304A (en) * | 1993-07-08 | 1995-01-27 | Takuma Co Ltd | Boiler water feeding system |
| CN201059546Y (en) * | 2007-07-05 | 2008-05-14 | 王嘉贤 | Device for recycling and transmitting device in enclosed type high-temperature condensate water and water collection pot |
| CN204039093U (en) * | 2014-06-13 | 2014-12-24 | 江苏巴威节能服务有限公司 | One-level deaerating type of cycles is reclaimed in the mixing of water of condensation de-mineralized water |
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