CN104085938A - Condensate water and demineralized water indirect heat-exchange forced-mixing one-stage deoxygenization apparatus - Google Patents
Condensate water and demineralized water indirect heat-exchange forced-mixing one-stage deoxygenization apparatus Download PDFInfo
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Abstract
The invention relates to a condensate water and demineralized water indirect heat-exchange forced-mixing one-stage deoxygenization apparatus. According to the invention, a first water inlet pipe and a third water inlet pipe positioned on an upper level, and a second water inlet pipe and a fourth water inlet pipe positioned on a lower level are connected on the circumference of a pressure-bearing buffering tank. Mixed condensate water is respectively subjected to indirect heat-exchange with synthetic ammonia demineralized water and transformation demineralized water through a third heat exchanger and a fourth heat exchanger. The processed condensate water is respectively connected into the second and the fourth water inlet pipes. After the synthetic ammonia demineralized water and the transformation demineralized water are subjected to heat-exchange through the third and fourth heat exchangers, the synthetic ammonia demineralized water and the transformation demineralized water and are respectively connected into the first and the third water inlet pipes. A buffering tank exhaust pipe is connected to the middle part of the top wall of the pressure-bearing buffering tank. A check valve and a first control valve are sequentially arranged from bottom to top on the buffering tank exhaust pipe. The lower end of a buffering tank water outlet pipe penetrates through the bottom plate of the pressure-bearing buffering tank and is connected with an inlet of a first water pump. An outlet of the first water pump is connected into a boiler water replenishing pipe. A forced-mixing impeller is arranged on the middle-lower part in the inner cavity of the pressure-bearing buffering tank. A sewage discharge pipe is connected to the bottom plate of the pressure-bearing buffering tank. The apparatus provided by the invention has the advantages of high condensate water residual heat utilization rate and reliable operation.
Description
Technical field
The present invention relates to a kind of water of condensation de-mineralized water indirect heat exchange Forced Mixing one-level de-aerator plant, can be used for the high-temperature condensation water of alkali factory production line generation and the recovery of the de-mineralized water through heating.
Background technology
For preventing heat power equipment and corrosive pipeline thereof, and prevent non-condensable gases from sneaking into steam and reduce steam quality, must remove the dissolved oxygen and other non-condensable gases that are dissolved in boiler replenishing water, often by deoxygenator, realizing.According to Henry's law and Dalton's law, for the various gases that are dissolved in the water, under certain pressure, the temperature of water is higher, and solubleness is lower; Or under certain 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 be close to total pressure on the water surface, the pressure component of various gases 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, thereby removes oxygen and other gases in water.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 a deoxygenation water inlet pipe, the lower sidewall of deoxygenation head is connected with deoxygenation vapour pipe, the top of deoxygenation head is connected with a deoxygenation 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 utilization still has 135 ℃ ~ 155 ℃.In addition, synthetic ammonia and shift conversion step can be used a large amount of de-mineralized waters as indirect cooling water, approximately 60 ℃ ~ 80 ℃ of the temperature of the synthetic ammonia cooling and desalting water after heating, approximately 60 ℃ ~ 95 ℃ of the temperature of the conversion cooling and desalting water through heating.Because of the temperature of the water of condensation that produces and cooling and desalting water higher, water quality meets again the requirement of boiler replenishing water, Ge Jian factory is often recycled to above steam condensate and cooling and desalting water in the deoxygenation case of atmospheric type deaerator, then by water pump, delivers to boiler as boiler replenishing water by deoxygenation case.
There is following weak point in above way of recycling: 1. deoxygenator is air suspended type, approximately 104 ℃ of working temperatures, and the mixed actual temperature of water of condensation and de-mineralized water is considerably beyond 104 ℃, therefore excess portion can only, by deoxygenation head and a large amount of kitings of the flash tank being communicated with deoxygenator, be wasted a large amount of residual heat resources and water resources.2. water of condensation and the de-mineralized water temperature difference are large, and by direct contact heat transfer, heat is difficult to reach balance in moment, therefore easily produce thermal explosion in deoxygenation case, affect equipment safety operation.3. there is contradiction in the continuity that the intermittence of boiler replenishing water and water of condensation produce: when not moisturizing of boiler or rate of water make-up are when little, 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 volume is limited, can not between boiler unit and productive unit, form effectively buffering.
Summary of the invention
The object of the invention is to, overcome problems of the prior art, a kind of water of condensation de-mineralized water indirect heat exchange Forced Mixing one-level de-aerator plant is provided, 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, a kind of water of condensation de-mineralized water indirect heat exchange Forced Mixing one-level de-aerator plant of the present invention, the calcining furnace water of condensation of 135 ℃ ~ 155 ℃, fluidized-bed water of condensation and dry ammonium water of condensation enter respectively calcining furnace condensate pipe, fluidized-bed condensate pipe and dry ammonium condensate pipe, the synthetic ammonia cooling and desalting water of 60 ℃ ~ 80 ℃ enters synthetic ammonia desalination water pipe, and the conversion cooling and desalting water of 60 ℃ ~ 95 ℃ enters conversion desalination water pipe, described calcining furnace condensate pipe, fluidized-bed condensate pipe and dry ammonium condensate pipe access respectively water of condensation header, also comprise the 3rd interchanger, the pressure-bearing surge tank of the 4th interchanger and sealing, on the circumference of described pressure-bearing surge tank, be vertically connected with the first water inlet pipe, the second water inlet pipe, the 3rd water inlet pipe and the 4th water inlet pipe, in the relative and short transverse of the mouth of pipe of described the first water inlet pipe and the 3rd water inlet pipe, mutually stagger, in the relative and short transverse of the mouth of pipe of described the second water inlet pipe and the 4th water inlet pipe, mutually stagger, the height of described the first water inlet pipe and the 3rd water inlet pipe is higher than described the 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 the 3rd interchanger and the 4th interchanger mixing condensation water inlet of the 4th interchanger respectively, the 3rd interchanger mixing condensation water out of described the 3rd interchanger is connected with described the second water inlet pipe, and the 4th interchanger mixing condensation water out of described the 4th interchanger is connected with described the 4th water inlet pipe, described synthetic ammonia desalination water pipe is connected with the 3rd interchanger synthetic ammonia de-mineralized water import of described the 3rd interchanger, the 3rd interchanger synthetic ammonia de-mineralized water outlet of described the 3rd interchanger is connected with described the first water inlet pipe, described conversion desalination water pipe is connected with the 4th interchanger conversion de-mineralized water import, and the 4th interchanger conversion de-mineralized water outlet of described the 4th interchanger is connected with described the 3rd water inlet pipe, the roof middle part of described pressure-bearing surge tank is connected with surge tank steam discharge pipe, and reverse checkvalve and the first control valve are installed on described surge tank steam discharge pipe from lower to upper successively, in described pressure-bearing surge tank, be provided with the surge tank rising pipe of opening upwards, 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 the first water pump outlet access 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, and the second control valve is installed on described blow-off pipe, 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 the base plate of pressure-bearing surge tank and and pressure-bearing surge tank base plate between realize sealing, the lower end of described Forced Mixing impeller shaft is connected with Forced Mixing impeller drive motor.
With respect to prior art, the present invention has obtained 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 respectively in pressure-bearing surge tank, after mixing, from surge tank rising pipe, discharge, by the first water pump, send into boiler replenishing water pipe; The flash-off steam that water surface top produces and the non-condensable gasess such as oxygen that overflow are discharged from the surge tank steam discharge pipe at pressure-bearing surge tank top.Pressure-bearing surge tank can bearing certain pressure and water level can in a big way, adjust, can make up the contradiction between the intermittence of boiler replenishing water and the continuity of water of condensation generation, between by vapour unit and boiler replenishing water system, form isolation and buffering, the fluctuation of guaranteeing 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; Also avoided 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 contain the non-condensable gasess such as oxygen, the non-condensable gasess such as the high and oxygen-free gas of mixing condensation water temp, synthetic ammonia cooling and desalting water, after conversion cooling and desalting water and mixing condensation water are mixed, temperature rises, and pressure-bearing surge tank operating pressure is saturation pressure 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, after overflowing the pressure-bearing surge tank water surface, with surge tank exhaust steam, from surge tank steam discharge pipe, discharge, thereby reach the object of deoxygenation.(4) the reverse checkvalve on surge tank steam discharge pipe can guarantee that atmosphere can not pour in down a chimney to pressure-bearing surge tank, prevents from introducing extraneous oxygen.(5) the first control valve, by controlling the quantity discharged of surge tank exhaust steam, makes to maintain certain pressure in pressure-bearing surge tank, to fully 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, reduced 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 and three water inlet pipe higher from position 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, can in pressure-bearing surge tank, form natural convection, promote abundant heat exchange.(8) along with the increase of working hour, certain impurity can be gathered in pressure-bearing surge tank bottom, and water quality can decline, and now can open the second control valve, discharges the water of water quality variation from blow-off pipe, guarantees boiler replenishing water water quality.(9) the calcining furnace water of condensation of 135 ℃ ~ 155 ℃, the dry ammonium water of condensation of the fluidized-bed water of condensation of 135 ℃ ~ 155 ℃ and 135 ℃ ~ 155 ℃ enters first respectively water of condensation header to be mixed, mixing condensation water enters respectively the 3rd interchanger and the 4th interchanger and the synthetic ammonia de-mineralized water of 60 ℃ ~ 80 ℃ and the conversion de-mineralized water of 60 ℃ ~ 95 ℃ again 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, dwindled 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) when the temperature difference of synthetic ammonia cooling and desalting water, conversion cooling and desalting water and mixing condensation water is larger, only depend on natural heat-exchange, in tank, temperature is still difficult to be evenly distributed, easily in pressure-bearing surge tank, formation temperature is poor, now open Forced Mixing impeller tank inner storing water is carried out to Forced Mixing, promote the homogeneity of temperature distribution in tank.
As preferred version of the present invention, the mouth of pipe that described the 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 with respectively the annular water distributor extending along the inner peripheral wall of horizontal plane and pressure-bearing surge tank, described in each, the middle and lower part of annular water distributor is evenly distributed with respectively to the jet hole of the axis jet of pressure-bearing surge tank, described in each axis of jet hole become with horizontal plane 30 ° ~ 45 ° angles and respectively with the axes intersect of pressure-bearing surge tank.The water inlet of every road is all by having arranged ring pipe water outlet in the tank of jet hole, and current blowing perforation oliquely downward sprays, and with parabolical, contacts with water body in tank, extended with tank in duration of contact of water body, realize 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 the base plate of pressure-bearing surge tank and and pressure-bearing surge tank base plate between realize sealing, 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 extends perpendicular to base plate and 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 bottom water flow rotation can be flashed impurity; If current are stable circulation state, 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 to present stable circulation state; The eddy current baffle plate that plate inner wall is installed can thoroughly 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 a plurality of, be divided into two groups of inner ring sewage draining exit and outer ring sewage draining exits, each inner ring sewage draining exit is evenly distributed on from pressure-bearing surge tank axis on the circumference close to, each outer ring sewage draining exit is evenly distributed on from pressure-bearing surge tank axis on the circumference away from, and each inner ring sewage draining exit and each outer ring sewage draining exit are distributed on the different diameter of base plate.The more sewage draining exit that distributes in a plurality of orientation of base plate, can improve contaminant removal effectiveness, reduces 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 are staggered in a circumferential direction, centered by pressure-bearing surge tank axis, to extraradial eight directions, be equipped with sewage draining exit, can making blowdown 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, described sampling tube stretches out outside pressure-bearing surge tank and with sampling water cooler and is connected, and online electric conductivity detector and online Ph value detector are installed on the export pipeline of described sampling water cooler.Can detect in real time in-tank mixing electrical conductivity of water and Ph value.
As preferred version of the present invention, the signal wire of described online electric conductivity detector and online Ph value detector accesses respectively the corresponding signal input terminus of PLC controller, and the corresponding signal output terminal of described PLC controller is connected with the control line of described the second control valve; When the specific conductivity that online electric conductivity detector detected and provide when PLC controller is greater than Ph value that set(ting)value or online Ph value detector provide over setting range, control the second control valve and open, the specific conductivity that online electric conductivity detector detected and provide when PLC controller is less than set(ting)value and Ph value detector provides online Ph value and controls the second control valve in setting range time and close.The Ph value that the specific conductivity that PLC controller can provide according to online electric conductivity detector and online Ph value detector provide, the keying of control disturbance impeller and the second control valve automatically, the automatization level of raising system.
As preferred version of the present invention, on described the first water inlet pipe, the second water inlet pipe, the 3rd water inlet pipe and the 4th water inlet pipe, be separately installed with temperature sensor and under meter, the different azimuth of the liquid Space of described pressure-bearing surge tank and different heights are provided with a plurality of temperature sensors 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 be measured the actual flow of each water inlet pipe.
As preferred version of the present invention, described pressure transmitter, described in each temperature sensor and described in each signal wire of under meter access respectively the corresponding signal input terminus of PLC controller, the corresponding signal output terminal of described PLC controller is connected with the control line of described the first control valve; The aperture of controlling the first control valve when PLC controller detects t>t0 or p>p0 strengthens, and the aperture of controlling the first control valve when PLC controller detects t<t0 or p<p0 reduces; Wherein t is the mean value of the water temperature that each temperature sensor is surveyed of described pressure-bearing surge tank liquid Space, and p is the force value that described pressure transmitter is surveyed; T0 is the set temperature value of PLC controller, 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 the first, second, third and the 4th water inlet pipe detects, and m1, m2, m3 and m4 are respectively the measured flow of under meter on the first, second, third and the 4th water inlet pipe; P0 is the setup pressure value of PLC controller, and p0 is the saturation pressure value of water vapor corresponding at t0 temperature, and safety coefficient gets 0.8 ~ 0.95.The set temperature value of PLC controller is got the weighted mean water temperature t0 of each water inlet pipe, there is one-to-one relationship in saturation pressure p0 and the water temperature t0 of water vapor, when in tank, temperature is greater than design temperature or tank internal pressure and is greater than setting pressure, the aperture that PLC controller is controlled the first control valve strengthens, to strengthen the discharge of surge tank exhaust steam; In tank, temperature is lower than design temperature or tank internal pressure during lower than setting pressure, and the aperture that PLC controller is controlled the first control valve reduces, and prevents from that steam discharge is excessive even to occur that tank outer air pours in down a chimney; Adopt PLC controller automatically to regulate the aperture of the first control valve according to water temperature and pressure, improved the automatization level of system, avoid the excess discharge of surge tank exhaust steam, guarantee that pressure-bearing surge tank is operated at the peak pressure/temperature of permission, not only energy-conservation but also environmental protection.
As preferred version of the present invention, the 7th control valve is installed on the inlet duct of described the 3rd interchanger mixing condensation water inlet, the 8th control valve is installed on the inlet duct of described the 4th interchanger mixing condensation water inlet, the corresponding signal output terminal of described PLC controller is connected with the control line of the 8th control valve with described the 7th control valve, and the water temperature that described PLC controller detects according to the temperature sensor on described the first water inlet pipe and the second water inlet pipe is controlled the aperture of described the 7th control valve; The water temperature that described PLC controller detects according to the temperature sensor on described the 3rd water inlet pipe and the 4th water inlet pipe is controlled the aperture of described the 8th control valve.
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, non-in order to limit the present invention.
Fig. 1 is the schematic diagram of water of condensation de-mineralized water indirect heat exchange Forced Mixing one-level de-aerator plant 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; 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 flow meter; M2. the second under meter; M3. the 3rd under meter; M4. the 4th under meter;
Q. the water cooler of sampling; 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. convert desalination water pipe;
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, water of condensation de-mineralized water indirect heat exchange Forced Mixing one-level de-aerator plant of the present invention, comprises pressure-bearing surge tank E1, the 3rd interchanger H3 and the 4th interchanger H4 of sealing.The calcining furnace water of condensation of 135 ℃ ~ 155 ℃ enters calcining furnace condensate pipe S1, the fluidized-bed water of condensation of 135 ℃ ~ 155 ℃ enters fluidized-bed condensate pipe S2, the dry ammonium water of condensation of 135 ℃ ~ 155 ℃ enters dry ammonium condensate pipe, the synthetic ammonia cooling and desalting water of 60 ℃ ~ 80 ℃ enters synthetic ammonia desalination water pipe Y1, the conversion cooling and desalting water of 60 ℃ ~ 95 ℃ enters conversion desalination water pipe Y2, calcining furnace condensate pipe S1, fluidized-bed condensate pipe S2 and dry ammonium condensate pipe S3 access respectively water of condensation header S0, also can be by other condensate pipe S4 access water of condensation header S0.
On the circumference of pressure-bearing surge tank E1, be 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, in the relative and short transverse of the mouth of pipe of the first water inlet pipe G1 and the 3rd water inlet pipe G3, mutually stagger, in the relative and short transverse of the mouth of pipe of the second water inlet pipe G2 and the 4th water inlet pipe G4, mutually stagger, 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.After synthetic ammonia cooling and desalting water and conversion cooling and desalting water heat up, access respectively the first water inlet pipe G1 and the 3rd water inlet pipe G3, after mixing condensation water for cooling, access respectively the second water inlet pipe G2 and the 4th water inlet pipe G4; The roof middle part of pressure-bearing surge tank E1 is connected with surge tank steam discharge pipe G5, and reverse checkvalve Vd and the first control valve V1 are installed on surge tank steam discharge pipe G5 from lower to upper successively.In pressure-bearing surge tank E1, be provided with the surge tank rising pipe G6 of opening upwards, 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 access boiler replenishing water pipe of the first water pump B1.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, and the second control valve V2 is installed on blow-off pipe G7.
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 is connected with the 4th interchanger conversion de-mineralized water import H4a, 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 ℃ ~ 155 ℃, the dry ammonium water of condensation of the fluidized-bed water of condensation of 135 ℃ ~ 155 ℃ and 135 ℃ ~ 155 ℃ enters first respectively water of condensation header S0 to be mixed, other water of condensation also can enter water of condensation header S0 to be mixed, mixing condensation water enters respectively the 3rd interchanger H3 and the 4th interchanger H4 and the synthetic ammonia de-mineralized water of 60 ℃ ~ 80 ℃ and the conversion de-mineralized water of 60 ℃ ~ 95 ℃ again 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, dwindled the temperature difference of mixing condensation water and de-mineralized water, make the temperature field in pressure-bearing surge tank more even.From position, higher the first water inlet pipe G1 and the 3rd water inlet pipe G3 enters respectively for the synthetic ammonia cooling and desalting water that temperature is relatively low, density is higher and conversion cooling and desalting water; The second water inlet pipe G2 and the 4th water inlet pipe G4 that the mixing condensation water that temperature is relatively high, density is lower is lower from position enter pressure-bearing surge tank E1, can in pressure-bearing surge tank, form natural convection, promote abundant heat exchange.After synthetic ammonia cooling and desalting water, conversion cooling and desalting water and mixing condensation water are mixed, from surge tank rising pipe G6, discharge, by the first water pump B1, send into boiler replenishing water pipe.The temperature of synthetic ammonia cooling and desalting water and conversion cooling and desalting water is slightly low and contain the non-condensable gasess such as oxygen, the non-condensable gasess such as the high and oxygen-free gas of mixing condensation water temp, synthetic ammonia cooling and desalting water, after conversion cooling and desalting water and mixing condensation water are mixed, temperature rises, and the operating pressure of pressure-bearing surge tank E1 is the corresponding saturation pressure of 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, after overflowing the pressure-bearing surge tank water surface, with surge tank exhaust steam, from surge tank steam discharge pipe G5, discharge, thereby reach the object of deoxygenation.Reverse checkvalve Vd on surge tank steam discharge pipe G5 can guarantee that atmosphere can not pour in down a chimney to pressure-bearing surge tank E1, prevents from introducing extraneous oxygen.The 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, to fully 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, reduced unit steam coal consumption.Along with the increase of working hour, pressure-bearing surge tank E1 can gather certain impurity in bottom, and water quality can decline, and now can open the second control valve V2, and the water of discharging water quality variation from blow-off pipe G7, guarantees boiler replenishing water water quality.
As improvement, the first temperature sensor T1 and first flow meter M1 are installed on the first water inlet pipe G1, the second temperature sensor T2 and the second under meter M2 are installed on the second water inlet pipe G2, three-temperature sensor T3 and the 3rd under meter M3 are installed on the 3rd water inlet pipe G3, the 4th temperature sensor T4 and the 4th under meter M4 are installed on the 4th water inlet pipe G4.Different azimuth and the different heights of the liquid Space of pressure-bearing surge tank E1 are provided with a plurality of temperature sensors altogether, for example, at height different sites, 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.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 flow meter M1, the second under meter M2, the 3rd under meter M3, the 4th under meter M4 and pressure transmitter P accesses respectively the corresponding signal input terminus of PLC controller, and the corresponding signal output terminal of PLC controller is connected with the control line of the first control valve V1.
The aperture of controlling the first control valve V1 when PLC controller detects t>t0 or p>p0 strengthens, and the aperture of controlling the first control valve V1 when PLC controller detects t<t0 or p<p0 reduces; Wherein t is the mean value of the water temperature that each temperature sensor is surveyed of pressure-bearing surge tank liquid Space, for example, be the mean value of the 5th temperature sensor T5, the 6th temperature sensor T6, the 7th temperature sensor T7 and the 8th temperature sensor water temperature that T8 surveys; P is the force value that pressure transmitter P surveys; T0 is the set temperature value of PLC controller, 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 flow meter M1, the second under meter M2, the 3rd under meter M3 and the measured flow of the 4th under meter M4.P0 is the setup pressure value of PLC controller, and p0 is the saturation pressure value of water vapor corresponding at t0 temperature, and safety coefficient gets 0.8 ~ 0.95.
The set temperature value of PLC controller is got the weighted mean water temperature t0 of each water inlet pipe, there is one-to-one relationship in saturation pressure p0 and the water temperature t0 of water vapor, when in tank, temperature is greater than design temperature or tank internal pressure and is greater than setting pressure, the aperture that PLC controller is controlled the first control valve V1 strengthens, to strengthen the discharge of surge tank exhaust steam; In tank, temperature is lower than design temperature or tank internal pressure during lower than setting pressure, and the aperture that PLC controller is controlled the first control valve V1 reduces, and prevents from that steam discharge is excessive even to occur that tank outer air pours in down a chimney.Adopt PLC controller automatically to regulate the aperture of the first control valve V1 according to water temperature and pressure, improved the automatization level of system, avoid the excess discharge of surge tank exhaust steam, guarantee that pressure-bearing surge tank is operated at the peak pressure/temperature of permission, not only energy-conservation but also environmental protection.
For improving automatization level, on the inlet duct of the 3rd interchanger mixing condensation water inlet H3c, the 7th control valve V7 is installed, on the inlet duct of the 4th interchanger mixing condensation water inlet H4c, the 8th control valve V8 is installed, the corresponding signal output terminal of PLC controller is connected with the control line of the 8th control valve V8 with the 7th control valve V7, and the water temperature that PLC controller detects according to the first temperature sensor T1 on the first water inlet pipe and the second temperature sensor T2 on the second water inlet pipe is controlled the aperture of the 7th control valve V7; The water temperature that PLC controller detects according to the three-temperature sensor T3 on the 3rd water inlet pipe and the 4th temperature sensor T4 on the 4th water inlet pipe is controlled the aperture of the 8th control valve V8.
The intracavity bottom of pressure-bearing surge tank E1 can be provided with sampling tube E1e, sampling tube E1e stretches out outside pressure-bearing surge tank E1 and with sampling water cooler Q and is connected, online electric conductivity detector Q1 and online Ph value detector Q2 are installed, to detect in real time in-tank mixing electrical conductivity of water and Ph value on the export pipeline of sampling water cooler Q.
For improving the automatization level of system, the signal wire of online electric conductivity detector Q1 and online Ph value detector Q2 accesses respectively the corresponding signal input terminus of PLC controller, and the corresponding signal output terminal of PLC controller is connected with the control line of the second control valve V2; When the specific conductivity that online electric conductivity detector Q1 detected and provide when PLC controller is greater than Ph value that set(ting)value or online Ph value detector Q2 provide over setting range, controlling the second control valve V2 opens, the specific conductivity that online electric conductivity detector Q1 detected and provide when PLC controller is less than Ph value that set(ting)value and online Ph value detector Q2 provide and controls the second control valve V2 in setting range time and close, the specific conductivity providing according to online electric conductivity detector Q1 and the Ph value that Ph value detector Q2 provides are online provided, automatically control the keying of the second control valve V2.
As shown in Figure 2, as improvement, the mouth of pipe that 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 are positioned at pressure-bearing surge tank is connected with respectively the annular water distributor extending along the inner peripheral wall of horizontal plane and pressure-bearing surge tank, the 3rd water inlet pipe G3 of take in Fig. 2 is example, the middle and lower part of each annular water distributor is evenly distributed with respectively to the jet hole of the axis jet of pressure-bearing surge tank, the axis of each jet hole become with horizontal plane 30 ° ~ 45 ° angles and respectively with the axes intersect of pressure-bearing surge tank.The water inlet of every road is all by having arranged ring pipe water outlet in the tank of jet hole, and current blowing perforation oliquely downward sprays, and with parabolical, contacts with water body in tank, extended with tank in duration of contact of water body, realize abundant heat exchange, avoid thermal explosion.
As shown in Figure 1, when the temperature difference of synthetic ammonia cooling and desalting water, conversion cooling and desalting water and mixing condensation water is larger, only depend on natural heat-exchange, the interior temperature of tank is still difficult to be evenly distributed, and easily in pressure-bearing surge tank E1, formation temperature is poor.Can Forced Mixing impeller E1c 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 the base plate of pressure-bearing surge tank and and pressure-bearing surge tank base plate between realize sealing, 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 tank inner storing water is carried out to Forced Mixing, promote the homogeneity of temperature distribution in tank.
Because impurity accumulates in the bottom of pressure-bearing surge tank, during blowdown, be difficult to discharge with current, can disturbance impeller E1d be installed at the intracavity bottom of pressure-bearing surge tank, disturbance impeller E1d is fixedly connected on disturbance impeller shaft, disturbance impeller shaft vertically downward through the base plate of pressure-bearing surge tank and and pressure-bearing surge tank base plate between realize sealing, the lower end of disturbance impeller shaft is connected with disturbance impeller drive motor, opens disturbance impeller E1d bottom water flow rotation can be flashed impurity, is 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 extends perpendicular to base plate and along base plate diametric(al), eddy current baffle plate E1b can thoroughly 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 a plurality of, for example be divided into two groups of inner ring sewage draining exit and outer ring sewage draining exits, each inner ring sewage draining exit is evenly distributed on from pressure-bearing surge tank axis on the circumference close to, each outer ring sewage draining exit is evenly distributed on from pressure-bearing surge tank axis on the circumference away from, 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 are staggered in a circumferential direction, the 45 ° of settings of staggering successively in phase place, four inner ring sewage draining exits layout that assumes diamond in shape, 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 present invention's better possible embodiments, non-so 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 requirement of the present invention.
Claims (10)
1. a water of condensation de-mineralized water indirect heat exchange Forced Mixing one-level de-aerator plant, the calcining furnace water of condensation of 135 ℃ ~ 155 ℃, fluidized-bed water of condensation and dry ammonium water of condensation enter respectively calcining furnace condensate pipe, fluidized-bed condensate pipe and dry ammonium condensate pipe, the synthetic ammonia cooling and desalting water of 60 ℃ ~ 80 ℃ enters synthetic ammonia desalination water pipe, and the conversion cooling and desalting water of 60 ℃ ~ 95 ℃ enters conversion desalination water pipe, described calcining furnace condensate pipe, fluidized-bed condensate pipe and dry ammonium condensate pipe access respectively water of condensation header, it is characterized in that: also comprise the 3rd interchanger, the pressure-bearing surge tank of the 4th interchanger and sealing, on the circumference of described pressure-bearing surge tank, be vertically connected with the first water inlet pipe, the second water inlet pipe, the 3rd water inlet pipe and the 4th water inlet pipe, in the relative and short transverse of the mouth of pipe of described the first water inlet pipe and the 3rd water inlet pipe, mutually stagger, in the relative and short transverse of the mouth of pipe of described the second water inlet pipe and the 4th water inlet pipe, mutually stagger, the height of described the first water inlet pipe and the 3rd water inlet pipe is higher than described the 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 the 3rd interchanger and the 4th interchanger mixing condensation water inlet of the 4th interchanger respectively, the 3rd interchanger mixing condensation water out of described the 3rd interchanger is connected with described the second water inlet pipe, and the 4th interchanger mixing condensation water out of described the 4th interchanger is connected with described the 4th water inlet pipe, described synthetic ammonia desalination water pipe is connected with the 3rd interchanger synthetic ammonia de-mineralized water import of described the 3rd interchanger, the 3rd interchanger synthetic ammonia de-mineralized water outlet of described the 3rd interchanger is connected with described the first water inlet pipe, described conversion desalination water pipe is connected with the 4th interchanger conversion de-mineralized water import, and the 4th interchanger conversion de-mineralized water outlet of described the 4th interchanger is connected with described the 3rd water inlet pipe, the roof middle part of described pressure-bearing surge tank is connected with surge tank steam discharge pipe, and reverse checkvalve and the first control valve are installed on described surge tank steam discharge pipe from lower to upper successively, in described pressure-bearing surge tank, be provided with the surge tank rising pipe of opening upwards, 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 the first water pump outlet access 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, and the second control valve is installed on described blow-off pipe, 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 the base plate of pressure-bearing surge tank and and pressure-bearing surge tank base plate between realize sealing, the lower end of described Forced Mixing impeller shaft is connected with Forced Mixing impeller drive motor.
2. water of condensation de-mineralized water indirect heat exchange Forced Mixing one-level de-aerator plant according to claim 1, it is characterized in that: the mouth of pipe that described the 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 with respectively the annular water distributor extending along the inner peripheral wall of horizontal plane and pressure-bearing surge tank, described in each, the middle and lower part of annular water distributor is evenly distributed with respectively to the jet hole of the axis jet of pressure-bearing surge tank, described in each axis of jet hole become with horizontal plane 30 ° ~ 45 ° angles and respectively with the axes intersect of pressure-bearing surge tank.
3. water of condensation de-mineralized water indirect heat exchange Forced Mixing one-level de-aerator plant 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 the base plate of pressure-bearing surge tank and and pressure-bearing surge tank base plate between realize sealing, 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 extends perpendicular to base plate and along base plate diametric(al).
4. water of condensation de-mineralized water indirect heat exchange Forced Mixing one-level de-aerator plant according to claim 1, it is characterized in that: described sewage draining exit is provided with a plurality of, be divided into two groups of inner ring sewage draining exit and outer ring sewage draining exits, each inner ring sewage draining exit is evenly distributed on from pressure-bearing surge tank axis on the circumference close to, each outer ring sewage draining exit is evenly distributed on from pressure-bearing surge tank axis on the circumference away from, and each inner ring sewage draining exit and each outer ring sewage draining exit are distributed on the different diameter of base plate.
5. water of condensation de-mineralized water indirect heat exchange Forced Mixing one-level de-aerator plant 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. water of condensation de-mineralized water indirect heat exchange Forced Mixing one-level de-aerator plant according to claim 1, it is characterized in that: the intracavity bottom of described pressure-bearing surge tank is provided with sampling tube, described sampling tube stretches out outside pressure-bearing surge tank and with sampling water cooler and is connected, and online electric conductivity detector and online Ph value detector are installed on the export pipeline of described sampling water cooler.
7. water of condensation de-mineralized water indirect heat exchange Forced Mixing one-level de-aerator plant according to claim 1, it is characterized in that: the signal wire of described online electric conductivity detector and online Ph value detector accesses respectively the corresponding signal input terminus of PLC controller, and the corresponding signal output terminal of described PLC controller is connected with the control line of described the second control valve; When the specific conductivity that online electric conductivity detector detected and provide when PLC controller is greater than Ph value that set(ting)value or online Ph value detector provide over setting range, control the second control valve and open, the specific conductivity that online electric conductivity detector detected and provide when PLC controller is less than set(ting)value and Ph value detector provides online Ph value and controls the second control valve in setting range time and close.
8. water of condensation de-mineralized water indirect heat exchange Forced Mixing one-level de-aerator plant according to claim 1, it is characterized in that: on described the first water inlet pipe, the second water inlet pipe, the 3rd water inlet pipe and the 4th water inlet pipe, be separately installed with temperature sensor and under meter, the different azimuth of the liquid Space of described pressure-bearing surge tank and different heights are provided with a plurality of temperature sensors altogether, and the gas-phase space of described pressure-bearing surge tank is provided with pressure transmitter.
9. water of condensation de-mineralized water indirect heat exchange Forced Mixing one-level de-aerator plant according to claim 8, it is characterized in that: described pressure transmitter, described in each temperature sensor and described in each signal wire of under meter access respectively the corresponding signal input terminus of PLC controller, the corresponding signal output terminal of described PLC controller is connected with the control line of described the first control valve; The aperture of controlling the first control valve when PLC controller detects t>t0 or p>p0 strengthens, and the aperture of controlling the first control valve when PLC controller detects t<t0 or p<p0 reduces; Wherein t is the mean value of the water temperature that each temperature sensor is surveyed of described pressure-bearing surge tank liquid Space, and p is the force value that described pressure transmitter is surveyed; T0 is the set temperature value of PLC controller, 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 the first, second, third and the 4th water inlet pipe detects, and m1, m2, m3 and m4 are respectively the measured flow of under meter on the first, second, third and the 4th water inlet pipe; P0 is the setup pressure value of PLC controller, and p0 is the saturation pressure value of water vapor corresponding at t0 temperature, and safety coefficient gets 0.8 ~ 0.95.
10. water of condensation de-mineralized water indirect heat exchange Forced Mixing one-level de-aerator plant according to claim 9, it is characterized in that: the 7th control valve is installed on the inlet duct of described the 3rd interchanger mixing condensation water inlet, the 8th control valve is installed on the inlet duct of described the 4th interchanger mixing condensation water inlet, the corresponding signal output terminal of described PLC controller is connected with the control line of the 8th control valve with described the 7th control valve, the water temperature that described PLC controller detects according to the temperature sensor on described the first water inlet pipe and the second water inlet pipe is controlled the aperture of described the 7th control valve, the water temperature that described PLC controller detects according to the temperature sensor on described the 3rd water inlet pipe and the 4th water inlet pipe is controlled the aperture of described the 8th control valve.
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| JP2013154267A (en) * | 2012-01-27 | 2013-08-15 | Tlv Co Ltd | Low-pressure steam heating apparatus |
| CN203479052U (en) * | 2013-09-10 | 2014-03-12 | 唐山佳华煤化工有限公司 | Exhaust steam recovery device for deaerator |
| CN203946912U (en) * | 2014-06-13 | 2014-11-19 | 云南能投有能科技股份有限公司 | Water of condensation de-mineralized water indirect heat exchange Forced Mixing one-level deaerating type of cycles |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202054679U (en) * | 2011-05-11 | 2011-11-30 | 张祥成 | Filtering system for recycling condensing water of steam boiler |
| JP2013154267A (en) * | 2012-01-27 | 2013-08-15 | Tlv Co Ltd | Low-pressure steam heating apparatus |
| CN203479052U (en) * | 2013-09-10 | 2014-03-12 | 唐山佳华煤化工有限公司 | Exhaust steam recovery device for deaerator |
| CN203946912U (en) * | 2014-06-13 | 2014-11-19 | 云南能投有能科技股份有限公司 | Water of condensation de-mineralized water indirect heat exchange Forced Mixing one-level deaerating type of cycles |
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