CN104085943B - Secondary de-aerator plant is reclaimed in the exhaust steam of water of condensation de-mineralized water indirect heat exchange - Google Patents
Secondary de-aerator plant is reclaimed in the exhaust steam of water of condensation de-mineralized water indirect heat exchange Download PDFInfo
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- CN104085943B CN104085943B CN201410261533.5A CN201410261533A CN104085943B CN 104085943 B CN104085943 B CN 104085943B CN 201410261533 A CN201410261533 A CN 201410261533A CN 104085943 B CN104085943 B CN 104085943B
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Abstract
The present invention relates to a kind of water of condensation de-mineralized water indirect heat exchange exhaust steam and reclaim secondary de-aerator plant, pressure-bearing surge tank is provided with first and third water inlet pipe being positioned at upper strata and second, four water inlet pipes being positioned at lower floor; Mixing condensation water respectively by third and fourth interchanger and synthetic ammonia de-mineralized water, convert de-mineralized water indirect heat exchange after access second, four water inlet pipes respectively, synthetic ammonia de-mineralized water and conversion de-mineralized water by accessing first and third water inlet pipe respectively after third and fourth interchanger heat exchange; Surge tank exhaust steam enters First Heat Exchanger and is cooled to surge tank exhaust steam water of condensation and fills into pressure-bearing surge tank through condensation water collection tank and the second water pump, non-condensable gases discharge simultaneously; Surge tank water outlet sends into higher-pressure deaerator by the first water pump, and deoxygenation case water shoot is through the 3rd water pump access boiler replenishing water pipe, and pressure-bearing surge tank base plate is connected with blow-off pipe.This device condensation water residual heat utilization ratio is high and reliable.
Description
Technical field
The present invention relates to a kind of water of condensation de-mineralized water indirect heat exchange exhaust steam and reclaim secondary 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 indirect heat exchange exhaust steam to reclaim secondary 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, secondary de-aerator plant is reclaimed in a kind of water of condensation de-mineralized water indirect heat exchange exhaust steam of the present invention, the calcining furnace water of condensation of 135 DEG C ~ 155 DEG C, fluidized-bed water of condensation and dry ammonium water of condensation enter calcining furnace condensate pipe, fluidized-bed condensate pipe and dry ammonium condensate pipe respectively, the synthetic ammonia cooling and desalting water of 60 DEG C ~ 80 DEG C enters synthetic ammonia desalination water pipe, and the conversion cooling and desalting water of 60 DEG C ~ 95 DEG C enters conversion desalination water pipe, described calcining furnace condensate pipe, fluidized-bed condensate pipe and dry ammonium condensate pipe access water of condensation header respectively, also comprise the 3rd interchanger, 4th interchanger and the pressure-bearing surge tank closed, 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, the outlet of described water of condensation header is connected with the 3rd interchanger mixing condensation water inlet of described 3rd interchanger and the 4th interchanger mixing condensation water inlet of the 4th interchanger respectively, 3rd interchanger mixing condensation water out of described 3rd interchanger is connected with described second water inlet pipe, and the 4th interchanger mixing condensation water out of described 4th interchanger is connected with described 4th water inlet pipe, described synthetic ammonia desalination water pipe is connected with the 3rd interchanger synthetic ammonia de-mineralized water import of described 3rd interchanger, 3rd interchanger synthetic ammonia de-mineralized water outlet of described 3rd interchanger is connected with described first water inlet pipe, described conversion desalination water pipe converts de-mineralized water import with the 4th interchanger and is connected, and the 4th interchanger conversion de-mineralized water outlet of described 4th interchanger is connected with described 3rd water inlet pipe, 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, the outlet of described first control valve is connected with the First Heat Exchanger surge tank exhaust steam import of First Heat Exchanger, the First Heat Exchanger surge tank exhaust steam condensation-water drain of described First Heat Exchanger is connected with the surge tank exhaust steam water of condensation water inlet pipe of condensation water collection tank, the condensation water collection tank rising pipe of described condensation water collection tank is connected with the entrance of the second water pump, and the outlet pipe of described second water pump accesses in described pressure-bearing surge tank, First Heat Exchanger circulating cooling water inlet and the First Heat Exchanger circulating cooling water out of described First Heat Exchanger connect and compose circulation with the circulating cooling water pipe of outside respectively, the inlet duct of First Heat Exchanger circulating cooling water inlet is provided with the 3rd control valve, the outlet pipe of First Heat Exchanger surge tank exhaust steam condensation-water drain is provided with the first non-condensable gases delivery pipe stretched out straight up, the surge tank rising pipe of opening upwards is provided with 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, described first water pump outlet is through the deoxygenation head water inlet pipe of the 5th control valve access higher-pressure deaerator, the entrance of deoxygenation case water shoot access the 3rd water pump of described higher-pressure deaerator, described 3rd water pump outlet access boiler replenishing water pipe, external steam is by the 4th control valve access deoxygenation vapour pipe, the deoxygenation crown portion of described higher-pressure deaerator is connected with the deoxygenation head steam discharge pipe of discharge deoxygenation exhaust steam and non-condensable gases, 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) first calcining furnace water of condensation, fluidized-bed water of condensation and dry ammonium water of condensation enter water of condensation header becomes mixing condensation water, mixing condensation water, 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 higher-pressure deaerator by the first water pump and carry out deep deoxygenization, to meet the requirement of high-duty boiler to oxygen level; Deoxygenation head steam mixes the non-condensable gasess such as the oxygen overflowed in the deoxygenation exhaust steam and water produced and discharges from the deoxygenation head steam discharge pipe in deoxygenation crown portion.(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, fluidized-bed and dry ammonium 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, high and the non-condensable gasess such as oxygen-free gas of mixing condensation water temp, after synthetic ammonia cooling and desalting water, conversion cooling and desalting water and mixing condensation water are mixed, 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 surge tank exhaust steam after overflowing the pressure-bearing surge tank water surface, realize one-level deoxygenation; Water through one-level deoxygenation is discharged the deoxygenation head water inlet pipe sending into higher-pressure deaerator through the first water pump and the 5th control valve by surge tank rising pipe, external steam enters deoxygenation head from deoxygenation vapour pipe and the 4th control valve and carries out secondary deoxygenation to water inlet, the non-condensable gasess such as the deoxygenation exhaust steam that the mixing of deoxygenation head steam produces and oxygen are discharged from deoxygenation head steam discharge pipe, and the water through secondary deoxygenation sends into boiler as boiler replenishing water by the 3rd water pump.(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 surge tank 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 surge tank 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 synthetic ammonia cooling and desalting water that temperature is relatively low, density is higher and conversion cooling and desalting water first water inlet pipe higher from position and the 3rd water inlet pipe enter, the second water inlet pipe that the mixing condensation water 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.(9) the calcining furnace water of condensation of 135 DEG C ~ 155 DEG C, the dry ammonium water of condensation of the fluidized-bed water of condensation of 135 DEG C ~ 155 DEG C and 135 DEG C ~ 155 DEG C enters water of condensation header first respectively and mixes, mixing condensation water enters the 3rd interchanger and the 4th interchanger and the synthetic ammonia de-mineralized water of 60 DEG C ~ 80 DEG C and the conversion de-mineralized water of 60 DEG C ~ 95 DEG C more respectively and carries out indirect heat exchange, the temperature of mixing condensation water reduces, the temperature of synthetic ammonia de-mineralized water and conversion de-mineralized water raises, reduce the temperature difference of mixing condensation water and de-mineralized water, make the temperature field in pressure-bearing surge tank more even, avoid the generation of thermal explosion, (10) the surge tank exhaust steam of pressure-bearing surge tank discharge enters First Heat Exchanger and is recycled and is condensed into surge tank exhaust steam water of condensation after water coolant cools indirectly and enters in condensation water collection tank, fill into pressure-bearing surge tank by the second water pump, reclaim the most of water entrained by surge tank exhaust steam and partial heat.(11) after surge tank exhaust steam condensation, the non-condensable gasess such as the oxygen of discharging with surge tank exhaust steam are still gaseous state, discharge from the first non-condensable gases delivery pipe; Non-condensable gases density is little, and the first non-condensable gases delivery pipe stretches out the discharge being beneficial to non-condensable gases straight up.
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 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 surge tank 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 surge tank 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.
As preferred version of the present invention, the inlet duct of described 3rd interchanger mixing condensation water inlet is provided with the 7th control valve, the inlet duct of described 4th interchanger mixing condensation water inlet is provided with the 8th control valve, the corresponding signal output terminal of described PLC is connected with the control line of the 8th control valve with described 7th control valve, and described PLC controls the aperture of described 7th control valve according to the water temperature that the temperature sensor on described first water inlet pipe and the second water inlet pipe detects; Described PLC controls the aperture of described 8th control valve according to the water temperature that the temperature sensor on described 3rd water inlet pipe and the 4th water inlet pipe detects; The outlet pipe of described First Heat Exchanger surge tank exhaust steam condensation-water drain is provided with the 9th temperature sensor of detection surge tank exhaust steam condensate temperature, the corresponding signal input terminus of the signal wire access PLC of described 9th temperature sensor, the corresponding signal output terminal of described PLC is connected with the control line of described 3rd control valve, and described PLC controls the aperture size of the 3rd control valve according to the temperature height that the 9th temperature sensor detects.
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 secondary de-aerator plant is reclaimed in water of condensation de-mineralized water indirect heat exchange exhaust steam of the present invention.
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; 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;
S1. calcining furnace condensate pipe; S2. fluidized-bed condensate pipe; S3. dry ammonium condensate pipe; S4. other condensate pipe; S0. water of condensation header; Y1. synthetic ammonia desalination water pipe; Y2. desalination water pipe is converted;
H1. First Heat Exchanger; H1a. First Heat Exchanger circulating cooling water inlet; H1b. First Heat Exchanger circulating cooling water out; H1c. First Heat Exchanger surge tank exhaust steam import; H1d. First Heat Exchanger surge tank exhaust steam condensation-water drain; H1e. the first non-condensable gases delivery pipe; T9. the 9th temperature sensor; V3. the 3rd control valve;
E2. condensation water collection tank; E2a. condensation water collection tank rising pipe; E2b. surge tank exhaust steam water of condensation water inlet pipe; B2. the second water pump;
E3. higher-pressure deaerator; E3a. deoxygenation vapour pipe; E3b. deoxygenation head water inlet pipe; E3c. deoxygenation head steam discharge pipe; E3d. deoxygenation case water shoot; B3. the 3rd water pump; V4. the 4th control valve; V5. the 5th control valve;
H3. the 3rd interchanger; H3a. the 3rd interchanger synthetic ammonia de-mineralized water import; H3b. the 3rd interchanger synthetic ammonia de-mineralized water outlet; H3c. the 3rd interchanger mixing condensation water inlet; H3d. the 3rd interchanger mixing condensation water out; V7. the 7th control valve;
H4. the 4th interchanger; H4a. the 4th interchanger conversion de-mineralized water import; H4b. the 4th interchanger conversion de-mineralized water outlet; H4c. the 4th interchanger mixing condensation water inlet; H4d. the 4th interchanger mixing condensation water out; V8. the 8th control valve.
Embodiment
As shown in Figure 1, secondary de-aerator plant is reclaimed in water of condensation de-mineralized water indirect heat exchange exhaust steam of the present invention, comprises closed pressure-bearing surge tank E1, the 3rd interchanger H3 and the 4th interchanger H4.The calcining furnace water of condensation of 135 DEG C ~ 155 DEG C enters calcining furnace condensate pipe S1, the fluidized-bed water of condensation of 135 DEG C ~ 155 DEG C enters fluidized-bed condensate pipe S2, the dry ammonium water of condensation of 135 DEG C ~ 155 DEG C enters dry ammonium condensate pipe, the synthetic ammonia cooling and desalting water of 60 DEG C ~ 80 DEG C enters synthetic ammonia desalination water pipe Y1, the conversion cooling and desalting water of 60 DEG C ~ 95 DEG C enters conversion desalination water pipe Y2, calcining furnace condensate pipe S1, fluidized-bed condensate pipe S2 and dry ammonium condensate pipe S3 access water of condensation header S0 respectively, also other condensate pipe S4 can be accessed water of condensation header S0.
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.Access the first water inlet pipe G1 and the 3rd water inlet pipe G3 respectively after synthetic ammonia cooling and desalting water and conversion cooling and desalting water heat up, after mixing condensation water for cooling, 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.
The outlet of the first control valve V1 is connected with the First Heat Exchanger surge tank exhaust steam import H1c of First Heat Exchanger H1, the First Heat Exchanger surge tank exhaust steam condensation-water drain H1d of First Heat Exchanger H1 is connected with the surge tank exhaust steam water of condensation water inlet pipe E2b of condensation water collection tank E2, the condensation water collection tank rising pipe E2a of condensation water collection tank E2 is connected with the entrance of the second water pump B2, in the outlet pipe access pressure-bearing surge tank E1 of the second water pump B2, First Heat Exchanger circulating cooling water inlet H1a and the First Heat Exchanger circulating cooling water out H1b of First Heat Exchanger H1 connect and compose circulation with the circulating cooling water pipe of outside respectively, namely First Heat Exchanger circulating cooling water inlet H1a is connected with the circulating cooling water pipe of low temperature, First Heat Exchanger circulating cooling water out H1b is connected with the circulating cooling water pipe of high temperature, the inlet duct of First Heat Exchanger circulating cooling water inlet H1a is provided with the 3rd control valve V3, the outlet pipe of First Heat Exchanger surge tank exhaust steam condensation-water drain H1d is provided with the first non-condensable gases delivery pipe H1e stretched out straight up, first non-condensable gases delivery pipe H1e is provided with stopping valve.First non-condensable gases delivery pipe H1e is preferably installed on the highest point of First Heat Exchanger surge tank exhaust steam condensating water outlet tube, and the best is installed on the descending opposite direction of turning round of First Heat Exchanger surge tank exhaust steam condensating water outlet tube.
The surge tank rising pipe G6 of opening upwards is provided with 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, the outlet of the first water pump B1 accesses the deoxygenation head water inlet pipe E3b of higher-pressure deaerator E3 through the 5th control valve V5, the deoxygenation case water shoot E3d of higher-pressure deaerator E3 accesses the entrance of the 3rd water pump B3, the outlet access boiler replenishing water pipe of the 3rd water pump B3, external steam accesses deoxygenation vapour pipe E3a by the 4th control valve V4, the deoxygenation crown portion of higher-pressure deaerator E3 is connected with the deoxygenation head steam discharge pipe E3c of discharge deoxygenation exhaust steam and non-condensable gases.
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 outlet of water of condensation header S0 is connected with the 3rd interchanger mixing condensation water inlet H3c of the 3rd interchanger H3 and the 4th interchanger mixing condensation water inlet H4c of the 4th interchanger H4 respectively, the 3rd interchanger mixing condensation water out H3d of the 3rd interchanger H3 is connected with the second water inlet pipe G2, and the 4th interchanger mixing condensation water out H4d of the 4th interchanger H4 is connected with the 4th water inlet pipe G4; Synthetic ammonia desalination water pipe Y1 is connected with the 3rd interchanger synthetic ammonia de-mineralized water import H3a of the 3rd interchanger H3, the 3rd interchanger synthetic ammonia de-mineralized water outlet H3b of the 3rd interchanger H3 is connected with the first water inlet pipe G1, conversion desalination water pipe Y2 converts de-mineralized water import H4a with the 4th interchanger and is connected, and the 4th interchanger conversion de-mineralized water outlet H4b of the 4th interchanger H4 is connected with the 3rd water inlet pipe G3.
During work, the calcining furnace water of condensation of 135 DEG C ~ 155 DEG C, the dry ammonium water of condensation of the fluidized-bed water of condensation of 135 DEG C ~ 155 DEG C and 135 DEG C ~ 155 DEG C enters water of condensation header S0 first respectively and mixes, other water of condensation also can enter water of condensation header S0 and mix, mixing condensation water enters the 3rd interchanger H3 and the 4th interchanger H4 and the 60 DEG C ~ synthetic ammonia de-mineralized water of 80 DEG C more respectively and the conversion de-mineralized water of 60 DEG C ~ 95 DEG C carries out indirect heat exchange, the temperature of mixing condensation water reduces, the temperature of synthetic ammonia de-mineralized water and conversion de-mineralized water raises, reduce the temperature difference of mixing condensation water and de-mineralized water, make the temperature field in pressure-bearing surge tank more even.The synthetic ammonia cooling and desalting water that 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 mixing condensation water that temperature is relatively high, density is lower is 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 synthetic ammonia cooling and desalting water, conversion cooling and desalting water and mixing condensation water are mixed, send into higher-pressure deaerator E3 by the first water pump B1 and carry out secondary deoxygenation.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, high and the non-condensable gasess such as oxygen-free gas of mixing condensation water temp, synthetic ammonia cooling and desalting water, conversion cooling and desalting water and the mixed rear temperature of mixing condensation water rise, and the saturation pressure of the operating pressure of pressure-bearing surge tank E1 corresponding to pressure-bearing surge tank mixing water temperature, 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 surge tank exhaust steam after overflowing the pressure-bearing surge tank water surface, realize one-level deoxygenation, water through one-level deoxygenation is discharged the deoxygenation head water inlet pipe E3b sending into higher-pressure deaerator E3 through the first water pump B1 and the 5th control valve V5 by surge tank rising pipe G6, external steam enters deoxygenation head from deoxygenation vapour pipe E3a and the 4th control valve V4 and carries out secondary deoxygenation to water inlet, the non-condensable gasess such as deoxygenation exhaust steam and oxygen are discharged from deoxygenation head steam discharge pipe E3c, water through secondary deoxygenation is discharged from deoxygenation case water shoot E3d, sends into boiler as boiler replenishing water by the 3rd water pump B3.
Surge tank exhaust steam enters First Heat Exchanger H1 from First Heat Exchanger surge tank exhaust steam import H1c, being recycled becomes surge tank exhaust steam water of condensation after water coolant cools indirectly and discharges from First Heat Exchanger surge tank exhaust steam condensation-water drain H1d, this surge tank water of condensation enters condensation water collection tank E2 from surge tank exhaust steam water of condensation water inlet pipe E2b, the second water pump B2 is entered again from condensation water collection tank rising pipe E2a, the non-condensable gasess such as the second water pump B2 is pumped in pressure-bearing surge tank E1, the oxygen of discharging with surge tank exhaust steam are discharged from the first non-condensable gases delivery pipe H1e.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 surge tank 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 surge tank 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 surge tank 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 surge tank 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.
For improving automatization level, the inlet duct of the 3rd interchanger mixing condensation water inlet H3c is provided with the 7th control valve V7, the inlet duct of the 4th interchanger mixing condensation water inlet H4c is provided with the 8th control valve V8, the corresponding signal output terminal of PLC is connected with the control line of the 8th control valve V8 with the 7th control valve V7, and PLC controls the aperture of the 7th control valve V7 according to the water temperature that the first temperature sensor T1 on the first water inlet pipe and the second temperature sensor T2 on the second water inlet pipe detects; PLC controls the aperture of the 8th control valve V8 according to the water temperature that the three-temperature sensor T3 on the 3rd water inlet pipe and the 4th temperature sensor T4 on the 4th water inlet pipe detects.
As improvement, the outlet pipe of First Heat Exchanger surge tank exhaust steam condensation-water drain H1d is provided with the 9th temperature sensor T9 of detection surge tank exhaust steam condensate temperature, 9th temperature sensor T9 can detect First Heat Exchanger H1 arrange the temperature of surge tank exhaust steam water of condensation, the corresponding signal input terminus of the signal wire access PLC of the 9th temperature sensor, the corresponding signal output terminal of PLC is connected with the control line of the 3rd control valve V3, PLC controls the aperture size of the 3rd control valve V3 according to the temperature height that the 9th temperature sensor T9 detects, to control the cooling water flow entering First Heat Exchanger H1.
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.
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, and whole device can share a PLC, also can be controlled by respective PLC by each unit.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. secondary de-aerator plant is reclaimed in a water of condensation de-mineralized water indirect heat exchange exhaust steam, the calcining furnace water of condensation of 135 DEG C ~ 155 DEG C, fluidized-bed water of condensation and dry ammonium water of condensation enter calcining furnace condensate pipe, fluidized-bed condensate pipe and dry ammonium condensate pipe respectively, the synthetic ammonia cooling and desalting water of 60 DEG C ~ 80 DEG C enters synthetic ammonia desalination water pipe, and the conversion cooling and desalting water of 60 DEG C ~ 95 DEG C enters conversion desalination water pipe, described calcining furnace condensate pipe, fluidized-bed condensate pipe and dry ammonium condensate pipe access water of condensation header respectively, it is characterized in that: also comprise the 3rd interchanger, 4th interchanger and the pressure-bearing surge tank closed, 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, the outlet of described water of condensation header is connected with the 3rd interchanger mixing condensation water inlet of described 3rd interchanger and the 4th interchanger mixing condensation water inlet of the 4th interchanger respectively, 3rd interchanger mixing condensation water out of described 3rd interchanger is connected with described second water inlet pipe, and the 4th interchanger mixing condensation water out of described 4th interchanger is connected with described 4th water inlet pipe, described synthetic ammonia desalination water pipe is connected with the 3rd interchanger synthetic ammonia de-mineralized water import of described 3rd interchanger, 3rd interchanger synthetic ammonia de-mineralized water outlet of described 3rd interchanger is connected with described first water inlet pipe, described conversion desalination water pipe converts de-mineralized water import with the 4th interchanger and is connected, and the 4th interchanger conversion de-mineralized water outlet of described 4th interchanger is connected with described 3rd water inlet pipe, 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, the outlet of described first control valve is connected with the First Heat Exchanger surge tank exhaust steam import of First Heat Exchanger, the First Heat Exchanger surge tank exhaust steam condensation-water drain of described First Heat Exchanger is connected with the surge tank exhaust steam water of condensation water inlet pipe of condensation water collection tank, the condensation water collection tank rising pipe of described condensation water collection tank is connected with the entrance of the second water pump, and the outlet pipe of described second water pump accesses in described pressure-bearing surge tank, First Heat Exchanger circulating cooling water inlet and the First Heat Exchanger circulating cooling water out of described First Heat Exchanger connect and compose circulation with the circulating cooling water pipe of outside respectively, the inlet duct of First Heat Exchanger circulating cooling water inlet is provided with the 3rd control valve, the outlet pipe of First Heat Exchanger surge tank exhaust steam condensation-water drain is provided with the first non-condensable gases delivery pipe stretched out straight up, the surge tank rising pipe of opening upwards is provided with 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, described first water pump outlet is through the deoxygenation head water inlet pipe of the 5th control valve access higher-pressure deaerator, the entrance of deoxygenation case water shoot access the 3rd water pump of described higher-pressure deaerator, described 3rd water pump outlet access boiler replenishing water pipe, external steam is by the 4th control valve access deoxygenation vapour pipe, the deoxygenation crown portion of described higher-pressure deaerator is connected with the deoxygenation head steam discharge pipe of discharge deoxygenation exhaust steam and non-condensable gases, 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. secondary de-aerator plant is reclaimed in water of condensation de-mineralized water indirect heat exchange exhaust steam 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. secondary de-aerator plant is reclaimed in water of condensation de-mineralized water indirect heat exchange exhaust steam 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).
4. secondary de-aerator plant is reclaimed in water of condensation de-mineralized water indirect heat exchange exhaust steam 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.
5. secondary de-aerator plant is reclaimed in water of condensation de-mineralized water indirect heat exchange exhaust steam according to claim 4, 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 °.
6. secondary de-aerator plant is reclaimed in water of condensation de-mineralized water indirect heat exchange exhaust steam 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.
7. secondary de-aerator plant is reclaimed in water of condensation de-mineralized water indirect heat exchange exhaust steam according to claim 6, 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.
8. secondary de-aerator plant is reclaimed in water of condensation de-mineralized water indirect heat exchange exhaust steam 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.
9. secondary de-aerator plant is reclaimed in water of condensation de-mineralized water indirect heat exchange exhaust steam according to claim 8, 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.
10. secondary de-aerator plant is reclaimed in water of condensation de-mineralized water indirect heat exchange exhaust steam according to claim 9, it is characterized in that: the inlet duct of described 3rd interchanger mixing condensation water inlet is provided with the 7th control valve, the inlet duct of described 4th interchanger mixing condensation water inlet is provided with the 8th control valve, the corresponding signal output terminal of described PLC is connected with the control line of the 8th control valve with described 7th control valve, described PLC controls the aperture of described 7th control valve according to the water temperature that the temperature sensor on described first water inlet pipe and the second water inlet pipe detects, described PLC controls the aperture of described 8th control valve according to the water temperature that the temperature sensor on described 3rd water inlet pipe and the 4th water inlet pipe detects, the outlet pipe of described First Heat Exchanger surge tank exhaust steam condensation-water drain is provided with the 9th temperature sensor of detection surge tank exhaust steam condensate temperature, the corresponding signal input terminus of the signal wire access PLC of described 9th temperature sensor, the corresponding signal output terminal of described PLC is connected with the control line of described 3rd control valve, and described PLC controls the aperture size of the 3rd control valve according to the temperature height that the 9th temperature sensor detects.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2010276303A (en) * | 2009-05-29 | 2010-12-09 | Daikin Ind Ltd | Heat pump type water heater |
| CN103523842A (en) * | 2013-10-23 | 2014-01-22 | 河南心连心化肥有限公司 | Deaerator exhaust steam recovery device and recovery process |
| CN203946910U (en) * | 2014-06-13 | 2014-11-19 | 云南能投有能科技股份有限公司 | Secondary deaerating type of cycles is reclaimed in the exhaust steam of water of condensation de-mineralized water indirect heat exchange |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2010276303A (en) * | 2009-05-29 | 2010-12-09 | Daikin Ind Ltd | Heat pump type water heater |
| CN103523842A (en) * | 2013-10-23 | 2014-01-22 | 河南心连心化肥有限公司 | Deaerator exhaust steam recovery device and recovery process |
| CN203946910U (en) * | 2014-06-13 | 2014-11-19 | 云南能投有能科技股份有限公司 | Secondary deaerating type of cycles is reclaimed in the exhaust steam of water of condensation de-mineralized water indirect heat exchange |
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