JP5013063B2 - Supplying water for boiler feed water - Google Patents

Description

  The present invention relates to a method for supplying make-up water for boiler feed water, and in particular, in a load device, steam generated by storing make-up water as boiler feed water in a storage tank and supplying the boiler feed water from the storage tank to a steam boiler for heating. The present invention relates to a method for supplying makeup water to a water storage tank in a steam boiler device that collects and condenses condensate obtained by condensing steam to a water storage tank through a condensate path extending from a load device.

  Steam that supplies boiler feedwater to a steam boiler, heats it, uses the steam generated thereby in the load device, and mixes and recycles condensate obtained by condensing the steam with boiler feedwater to the steam boiler Boiler devices are known. Since such a steam boiler device reuses condensate as part of boiler feed water, the amount of makeup water can be reduced, and the steam boiler can be operated economically.

  In this steam boiler device, supply of boiler feed water to the steam boiler is usually performed by storing make-up water derived from raw water such as tap water and groundwater in a water storage tank, and using the make-up water stored in the water storage tank as boiler water supply. Supplying to steam boiler. Condensate is collected into a water storage tank through a condensate path extending from the load device, and mixed with makeup water in the water storage tank.

  By the way, in the case of a once-through boiler, for example, the steam boiler used in the above-described steam boiler apparatus includes a large number of heat transfer tubes for heating the boiler water supplied from the boiler feed water to generate steam. Since this heat transfer tube is formed using a non-passivated metal such as carbon steel, it is susceptible to corrosion, particularly pitting corrosion, under the influence of dissolved oxygen contained in boiler feed water. This corrosion often causes fatal destruction such as opening of holes in the heat transfer tube within a short time, and thus prevents stable operation of the steam boiler.

  In addition, the heat transfer tube easily adheres to the hardness contained in the boiler feed water, that is, the scale generated by calcium ions or magnesium ions. This scale lowers the thermal conductivity of the heat transfer tube and hinders smooth heating of boiler water.

  Therefore, in the steam boiler apparatus, in order to suppress corrosion and scale generation in the steam boiler, the makeup water supplied to the water storage tank is usually softened and deoxygenated (for example, Patent Document 1 and Patent). Reference 2). Here, the softening of the makeup water is performed by replacing calcium ions and magnesium ions in the makeup water with sodium ions by treatment of the makeup water using a sodium-type cation exchange resin. On the other hand, the deoxygenation treatment is performed, for example, by passing makeup water through a gas separation membrane.

  However, since the raw water used as makeup water is tap water or groundwater as described above, the water quality varies depending on geological factors. For example, the hardness concentration of raw water may be high or low depending on the region, and is likely to fluctuate in the same region due to seasonal factors and other factors. For this reason, sodium-type cation exchange resins used for water softening are easy to break through in areas where the hardness concentration of makeup water is high, and a portion of the hardness in makeup water can be removed in a relatively short time. There is a possibility of disappearing. In this case, it becomes difficult to suppress scale generation in the steam boiler.

  On the other hand, since the dissolved oxygen concentration of raw water is affected by temperature, it tends to fluctuate constantly in an environment where the temperature of raw water is likely to fluctuate. In general, makeup water tends to increase the concentration of dissolved oxygen when the water temperature decreases. Therefore, the gas separation membrane is in a high-load state when the temperature of makeup water decreases, and the dissolved oxygen in the makeup water permeates. It becomes easy.

  Further, in a steam boiler, not only corrosion due to the influence of dissolved oxygen in boiler feed water occurs, but also corrosion caused by ion components such as chloride ions and sulfate ions in boiler feed water.

  Furthermore, softening the make-up water removes the hardness, so scale formation can be suppressed, but at the same time, hydrogen carbonate salts such as sodium hydrogen carbonate are generated due to sodium ions supplied by ion exchange. To do. This bicarbonate is a major component of the acid consumption (pH 4.8) of makeup water. Boiler feed water with high acid consumption (pH 4.8) generates carbon dioxide by decomposition of bicarbonate when heated in a steam boiler, and discharges this carbon dioxide into the condensate path. And since a condensate path | route is often formed using the non-passivation metal similarly to the heat exchanger tube of a steam boiler, it is easy to advance corrosion under the influence of the carbon dioxide gas from a steam boiler. This corrosion may cause a hole in the condensate path that hinders smooth recovery of the condensate, and may cause iron ions and other metal ions, which are impurity components in boiler feed water, to elute into the condensate.

  Therefore, in consideration of the fact that the steam boiler apparatus is difficult to suppress corrosion in the steam boiler and the condensate path and to suppress scale generation in the steam boiler only by softening and deoxygenating the makeup water, Usually, various chemical | medical agents are added with respect to boiler feed water etc. (patent document 1 and patent document 2).

JP 2003-120904 A, paragraphs [0005] and [0025]. JP 2004-19970, paragraphs [0009] and [0011]

  However, the addition of chemicals to boiler feed water or the like increases the operating cost of the steam boiler device. Further, since steam water is concentrated in accordance with the generation of steam, steam boilers often drain part of boiler water from the viewpoint of chemical concentration management and dilute boiler water with new boiler feed water. In this case, the boiler water to be drained may cause environmental pollution due to the chemical, and therefore it is necessary to perform an appropriate drainage treatment such as decomposition and separation of the chemical.

  An object of the present invention is to effectively suppress corrosion in a steam boiler and a condensate path and scale generation in the steam boiler without adding chemicals to boiler feed water.

  The present invention stores the make-up water as boiler feed water in a water storage tank, uses the steam generated by supplying the boiler feed water from the water storage tank to the steam boiler and heating it in the load device, and is obtained by condensing the steam. The present invention relates to a method for supplying make-up water to a water storage tank in a steam boiler device that collects condensate into a water storage tank through a condensate path extending from a load device and reuses it. In this supply method, one resin unit is selected from a resin unit group including at least two resin units each having a sodium type cation exchange resin, and the selected resin unit is supplied from makeup water by ion exchange with a sodium type ion exchange resin. Using a cross-flow type filtration device that uses one of the nanofiltration membrane and reverse osmosis membrane to remove the hardness component, the blow amount from the cross-flow type filtration device is set to a predetermined blow amount, and the hardness A process B for filtering the makeup water from which the components have been removed, and a process C for removing the dissolved oxygen contained in the makeup water by passing the makeup water filtered in the cross-flow filtration device through the deoxygenation device at a predetermined flow rate. And between the process D for supplying the makeup water that has passed through the deoxygenation device to the water storage tank, and between the process A and the process B, the hardness concentration of the makeup water, the acid consumption (p And a step E of measuring 4.8) and the water temperature.

  Here, when the hardness concentration measured in step E exceeds a predetermined concentration, another resin unit is selected in the resin unit group and step A is executed, and the acid consumption (pH 4. When 8) exceeds a predetermined value, the amount of blow from the cross-flow type filtration device is set to be larger than the predetermined amount in step B, and when the water temperature measured in step E is lower than the predetermined temperature, in step C The make-up water is passed through the deoxygenator at a flow rate less than the predetermined flow rate.

  In such a method for supplying boiler water supply water, hardness of the makeup water is removed in step A. In the subsequent process B, the makeup water is obtained after the ionic components having a corrosion promoting action for steam boilers such as chloride ions and sulfate ions and the hydrogen carbonate generated in the process A are removed by the nanofiltration membrane or the reverse osmosis membrane. In step C, dissolved oxygen is removed. And the supplementary water processed in this way is supplied to a water storage tank in the process D, and is stored. In this series of steps, the makeup water is measured in Step E between Hardness A, Hardness Concentration, Acid Consumption (pH 4.8) and Water Temperature in Step E.

  Here, when the measured hardness concentration exceeds a predetermined concentration, that is, when there is a hardness leak in the makeup water from the resin unit due to breakthrough of the sodium-type cation exchange resin, etc., the resin unit Switch the resin unit to another in the group and execute step A. As a result, in the replenishing water thereafter, the hardness component is removed by the sodium cation exchange resin of the other resin unit in the process A, and the hardness component is more reliably removed.

  In addition, when the measured acid consumption (pH 4.8) exceeds a predetermined value, that is, the bicarbonate concentration of makeup water to be filtered in the cross-flow type filtration device increases, a nanofiltration membrane or a reverse osmosis membrane When it is predicted that the acid consumption (both pH 4.8) of boiler feedwater will increase due to a decrease in the ability to remove bicarbonate, the amount of blow from the cross-flow filter is set to be higher than the predetermined amount Then, process B is executed. As a result, the makeup water that is filtered in the crossflow filtration device is diluted with the newly-supplied makeup water, and the bicarbonate concentration decreases. Thus, the cross-flow type filtration apparatus is prevented from reducing the bicarbonate removal capability, and the makeup water after filtration is prevented from increasing in the bicarbonate concentration. The rise in 8) is suppressed.

  Furthermore, when the measured temperature of the makeup water is lower than the predetermined temperature, that is, when the dissolved oxygen concentration in the makeup water is increased, the flow rate of the makeup water is set to be lower than the predetermined flow rate in Step C. As a result, the make-up water has a longer residence time in the deoxygenation device, and dissolved oxygen is more reliably removed.

  In this supply method, for example, while performing steps A, B, C, D, and E, in the resin unit group, the sodium cation exchange resin of the resin unit other than the resin unit selected for step A is regenerated. . In this way, the resin unit other than the resin unit used for step A can be set in a state in which the ion-exchange capacity of the sodium-type ion exchange resin is increased. When the concentration exceeds a predetermined concentration, the resin unit can be smoothly switched to another in step A.

  In addition, the deoxygenation device used in this supply method is usually of a type in which the retention time of the make-up water becomes long when the flow rate of the make-up water is lowered, for example, a type in which make-up water is passed through the gas separation membrane One type selected from the group consisting of: a type that allows makeup water to pass under a reduced pressure environment, and a type that allows makeup water to pass under a heating environment.

  Since the method for supplying boiler water supply water according to the present invention includes the above-described steps, corrosion in the steam boiler and the condensate route and scale generation in the steam boiler can be performed without adding chemicals to the boiler feed water. It can be effectively suppressed.

  With reference to FIG. 1, the steam boiler apparatus which can implement the supply method of the supplementary water for boiler feed water which concerns on one Embodiment of this invention is demonstrated. In FIG. 1, a steam boiler device 1 is for supplying steam to a load device 2 that is a steam using facility such as a heat exchanger, a steam kettle, a reboiler, or an autoclave, and includes a water supply device 10 and a steam boiler 20. And a condensate path 30 is mainly provided.

  The water supply device 10 is for supplying boiler feed water to the steam boiler 20, a storage tank 40 for storing boiler feed water, a supply path 50 for supplying makeup water used as boiler supply water to the storage tank 40, and A control device 70 is mainly provided. The water storage tank 40 has a water supply path 41 extending from the bottom to the steam boiler 20. The water supply path 41 communicates with the steam boiler 20, and has a water supply pump 42 for sending the boiler water stored in the water storage tank 40 to the steam boiler 20.

  The supply path 50 has a water injection path 51. This water injection channel 51 is for supplying makeup water to a water storage tank 40 from a raw water tank (not shown) in which raw water supplied from a water source such as tap water, industrial water or groundwater is stored. A pretreatment device 52, a water softening device 53, a preliminary filtration device 54, a cross flow filtration device 55, and a deoxygenation device 56 are provided in this order toward the tank 40. Further, in the water injection channel 51, a hardness sensor 57, an acid consumption (pH 4.8) sensor 58, and a water temperature sensor 59 are disposed between the preliminary filtration device 54 and the crossflow filtration device 55. Further, the water injection channel 51 has a flow rate control valve 60 between the crossflow filtration device 55 and the deoxygenation device 56.

  The pretreatment device 52 is a filtration device filled with activated carbon capable of adsorbing an oxidizing agent such as sodium hypochlorite dissolved in makeup water from the raw water tank, and oxidizes sodium hypochlorite from raw water. It is for removing an agent.

  As shown in FIG. 2, the water softening device 53 includes a resin unit group 61 including two resin units, a first resin unit 61a and a second resin unit 61b. In the water softening device 53, the water injection path 51 is branched into two paths, a first path 51a and a second path 51b, by the switching valve 62, and the first path 51a communicates with the first resin unit 61a. The second path 51b communicates with the second resin unit 61b. The first path 51 a and the second path 51 b merge together at the downstream side of the resin units 61 a and 61 b and extend to the preliminary filtration device 54.

  Here, each resin unit 61a, 61b is filled with sodium-type cation exchange resin. The sodium-type cation exchange resin is for replacing the hardness component contained in the makeup water treated in the pretreatment device 52, that is, calcium ions and magnesium ions with sodium ions, and converting the makeup water into softened water. is there. The switching valve 62 is an electromagnetic valve and is used to select the water injection path 51 as either the first path 51a or the second path 51b.

  In the water softening device 53, the first resin unit 61a and the second resin unit 61b are detachable, and the sodium-type cation exchange resin can be exchanged.

  The preliminary filtration device 54 is for removing solid substances such as suspended substances and dust mixed in the makeup water softened by the water softening device 53, and for filtering and separating the solid matter. A filter medium (not shown) such as a wind filter, a pleated filter or a mesh filter is provided.

  The cross-flow filtration device 55 is for filtering and separating various dissolved components contained in the makeup water treated in the preliminary filtration device 54, that is, various ionic components and low molecular weight substances. As shown in FIG. 2, the pressure pump 80 and a filtration membrane module 81 disposed downstream of the pressure pump 80 are mainly provided. The filtration membrane module 81 includes a treatment liquid channel 82 and a water inlet channel 83. And the concentrated liquid path 84 is connected.

  The filtration membrane module 81 is configured such that when makeup water is introduced from the inlet channel 83, the makeup water filtered out from the treatment liquid channel 82 and the concentrated makeup water from the concentrate channel 84 flow out. Has been. Further, the concentrated liquid path 84 is branched into a drainage path 85 and a reflux path 86, and the reflux path 86 is connected to a water inlet path 83 on the upstream side of the pressurizing pump 80. The drainage channel 85 has a blow control valve 87 for controlling the drainage amount of makeup water, that is, the blow amount.

  The filtration membrane module 81 includes a filtration membrane (not shown) for filtering dissolved components contained in the makeup water. The filtration membrane used here is a nanofiltration membrane. The nanofiltration membrane is formed using a synthetic polymer such as a polyamide-based or polyether-based material that is generally referred to as an NF (Nanofiltration) membrane, and is an AMST (Association of Membrane Separation Technology) standard AMST- 002, “The molecular weight range of the separation target substance used at an operating pressure of 1.5 MPa and showing a removal rate of 90% or more shows 200 to 1,000, and the sodium chloride concentration of the test solution is 500 to 2,000 mg / liter. , A membrane having a sodium chloride removal rate of 5% or more and less than 93% under an evaluation condition of an operating pressure of 0.3 to 1.5 MPa ”. Incidentally, nanofiltration membranes are commercially available from various companies and can be easily obtained.

  In the filtration membrane module 81, the nanofiltration membrane is used in various shapes. That is, the nanofiltration membrane is used in various shapes such as a flat membrane type, a hollow fiber membrane type, a tubular type, and a Nomoris type.

  The treatment liquid path 82 extends from the filtration membrane module 81 and is for supplying makeup water filtered in the filtration membrane module 81 to the deoxygenation device 56.

  The deoxygenation device 56 is for removing dissolved oxygen in the make-up water filtered in the cross-flow type filter device 55, and the deoxygenation capability increases as the residence time of the make-up water passing through increases. For example, a type in which make-up water is passed through a gas separation membrane to remove dissolved oxygen (for example, a form in which make-up water is passed through the inside of the hollow fiber-like gas separation membrane while depressurizing the outside to remove dissolved oxygen. In a variety of types, such as a type that removes dissolved oxygen by passing make-up water under reduced pressure, or a type that removes dissolved oxygen by passing make-up water while heating Is used.

  The hardness component sensor 57 is for measuring the concentration of hardness component contained in the makeup water supplied from the preliminary filtration device 54, and is, for example, a colorimetric type, electrode type or titration type sensor. The acid consumption (pH 4.8) sensor 58 is for measuring the acid consumption (pH 4.8) of makeup water from the preliminary filtration device 54. For example, a colorimetric type, an electrode type or a titration type is used. Sensor. The water temperature sensor 59 is for measuring the temperature of the makeup water supplied from the preliminary filtration device 54, and is, for example, a sensor such as a thermistor, a thermocouple, or a resistance temperature detector.

  The flow rate adjustment valve 60 is an electromagnetic valve, and can arbitrarily adjust the flow rate of makeup water flowing from the crossflow filtration device 55 to the deoxygenation device 56.

  The control device 70 switches the switching valve based on the hardness content information, the acid consumption (pH 4.8) information, and the water temperature information measured by the hardness sensor 57, the acid consumption (pH 4.8) sensor 58, and the water temperature sensor 59, respectively. 62, for controlling the blow control valve 87 and the flow control valve 60.

  The steam boiler 20 is a once-through boiler, and as shown in FIG. 4, an annular storage portion 21 capable of storing boiler feed water supplied from a water supply path 41, and a large number of heat transfer tubes 22 rising from the storage portion 21 (FIG. 4). Only two are shown), and mainly includes an annular header 23 provided at the upper end of the heat transfer tube 22, a steam supply passage 24 extending from the header 23 to the load device 2, and a combustion device 25 such as a burner. The combustion device 25 can radiate combustion gas from the header 23 side toward the storage portion 21 to heat the heat transfer tube 22.

  The heat transfer tube 22 is formed using a non-passivated metal. A non-passivated metal refers to a metal that does not passivate naturally in a neutral aqueous solution, and is usually a metal other than stainless steel, titanium, aluminum, chromium, nickel, zirconium, and the like. Specifically, carbon steel, cast iron, copper, copper alloy, and the like. Carbon steel may be passivated in the presence of a high concentration of chromate ions even in a neutral aqueous solution. This passivation is due to the influence of chromate ions, and the neutral aqueous solution. It's hard to say that it's a natural passivation inside. Therefore, carbon steel belongs to the category of non-passivated metals here. In addition, copper and copper alloys are considered to be metals that are unlikely to corrode due to the influence of moisture due to their noble position in the electrochemical column (emf series), but they are naturally passive in neutral aqueous solutions. Since it does not convert to a non-passivated metal, it belongs to the category of

  The condensate path 30 is formed using a non-passivated metal like the heat transfer tube 22, and extends from the load device 2 to the water storage tank 40. In addition, the condensate path 30 has a steam trap 31. The steam trap 31 is for separating steam and water. The tip of the condensate passage 30 is preferably disposed in the boiler feed water in order to prevent air from being normally involved in the boiler feed water stored in the water storage tank 40. It is particularly preferable that they are arranged in the vicinity.

  Next, the operation method of the above steam boiler apparatus 1 will be described while touching the supply method of boiler water supply water. Here, in the initial state, the control device 70 switches the switching valve 62 to the first path 51a side, and the blow control valve 87 so that the blow amount from the crossflow filtration device 55 becomes the predetermined blow amount X. Further, the flow rate adjustment valve 60 is set so that the flow rate of the makeup water flowing from the crossflow filtration device 55 to the deoxygenation device 56 becomes the predetermined flow rate Y.

  During operation of the steam boiler device 1, makeup water is supplied from the raw water tank to the water storage tank 40 through the water injection channel 51, and this makeup water is stored in the water storage tank 40 as boiler feed water.

  At this time, the makeup water from the raw water tank is first supplied to the pretreatment device 52 through the water injection channel 51, where the oxidant is adsorbed and removed by the activated carbon. Subsequently, makeup water from the pretreatment device 52 flows to the water softening device 53. The makeup water that has flowed to the water softening device 53 flows to the first path 51a via the switching valve 62 and passes through the first resin unit 61a. Thereby, the hardness component contained in the makeup water is ion-exchanged with sodium ions by the sodium-type cation exchange resin, and becomes softened water from which the hardness component has been removed. This softened water contains an acid consumption (pH 4.8) component, that is, a hydrogen carbonate such as sodium hydrogen carbonate, which is generated as a result of supplying sodium ions by ion exchange.

  Incidentally, the sodium-type cation exchange resin used in the water softening device 53 is easily deteriorated due to the influence of the oxidizing agent, and the ion exchange capacity tends to be lowered. In this embodiment, the makeup water supplied to the water softening device 53 is Since the oxidizing agent is removed in the pretreatment device 52, the sodium-type cation exchange resin is hardly deteriorated. Therefore, the water softening device 53 can soften the makeup water stably over a long period of time.

  The make-up water that has become softened in the water softening device 53 is then filtered in the pre-filtering device 54 to remove suspended solids and solids such as dust, and then further filtered in the cross-flow filter 55. It is processed. In the cross-flow filtration device 55, makeup water from the preliminary filtration device 54 is continuously supplied to the filtration membrane module 81 through the water inlet 83 by the pressurizing pump 80. Part of the supplied makeup water passes through the filtration membrane and flows out to the treatment liquid path 82, and the remainder flows out to the concentrated liquid path 84 without passing through the filtration membrane. Further, part of the makeup water that has flowed out to the concentrate channel 84 is blown out of the system via the drainage channel 85, and the remainder is returned to the inlet channel 83 via the reflux channel 86. For this reason, the replenishing water supplied to the filtration membrane module 81 circulates in the apparatus while being partially concentrated.

The makeup water that permeates the filtration membrane is filtered by the filtration membrane. Accordingly, the makeup water is an ion component such as chloride ion (Cl ⁻ ) or sulfate ion (SO ₄ ²⁻ ) (hereinafter “corrosion promoting ion component”) that causes the heat transfer tube 22 of the steam boiler 20 to corrode. In addition, the hydrogen carbonate generated in the water softening device 53 is removed.

  Incidentally, since the oxidant is removed from the replenishing water from the preliminary filtration device 54 by the pretreatment device 52 and the solid matter is removed by the preliminary filtration device 54, the filtration membrane of the crossflow filtration device 55 is Deterioration due to oxidation hardly occurs, and clogging hardly occurs. Therefore, the crossflow filtration device 55 can stably remove the above-described corrosion promoting ion components and hydrogen carbonate from the makeup water over a long period of time.

  The makeup water filtered by the crossflow filtration device 55 flows out of the crossflow filtration device 55 through the treatment liquid path 82, and subsequently deoxygenated by the deoxygenation device 56. Thereby, the dissolved oxygen which accelerates | stimulates corrosion, especially pitting corrosion of the heat exchanger tube 22 of the steam boiler 20, etc. is removed from makeup water.

  As a result of the above, in the water storage tank 40, makeup water treated in the deoxygenation device 56, that is, softened water that has been deoxygenated and from which the corrosion-promoting ionic components and bicarbonate have been removed is stored as boiler feed water. become.

  When the water supply pump 42 is operated in a state where makeup water is stored in the water storage tank 40, the makeup water stored in the water storage tank 40, that is, boiler water supply, is supplied to the steam boiler 20 through the water supply path 41. Boiler feed water supplied to the steam boiler 20 is stored as boiler water in the storage unit 21. The boiler water rises in the heat transfer tubes 22 while being heated by the combustion device 25 through the heat transfer tubes 22 and gradually becomes steam. Then, the steam generated in each heat transfer tube 22 is collected in the header 23 and supplied to the load device 2 through the steam supply path 24.

  The steam supplied to the load device 2 flows through the load device 2 to the condensate passage 30 where it loses latent heat and partly changes to condensed water, and the steam and water are separated in the steam trap 31 so that the temperature is high. It becomes the condensate. The condensate thus generated is collected into the water storage tank 40 through the condensate path 30 and mixed with the makeup water stored in the water storage tank 40 to be reused as boiler feed water. At this time, since the boiler feed water stored in the water storage tank 40 is heated by the high-temperature condensate, the heating burden on the steam boiler 20 is reduced. Therefore, the steam boiler apparatus 1 can suppress the fuel cost for operating the steam boiler 20, and can be operated economically.

  During operation of the steam boiler device 1 as described above, boiler feed water stored as boiler water in the steam boiler 20 contacts the inner surface of the heat transfer tube 22 and the like. In general, the heat transfer tube 22 or the like made of a non-passivated metal is susceptible to corrosion due to the influence of boiler water. However, in this embodiment, since dissolved oxygen and corrosion accelerating ion components are removed from the boiler feed water, the steam boiler 20 is corrosive to the heat transfer tubes 22 and the like, particularly pitting corrosion and thinning which are local corrosion. Progress of general corrosion is suppressed.

  Moreover, in this steam boiler apparatus 1, since the boiler feed water supplied to the steam boiler 20 is softened water from which the hardness has been removed, the heat transfer tube 22 is also restrained from adhering to the scale.

  Furthermore, since the hydrogen carbonate is removed from the boiler feed water stored as boiler water in the steam boiler 20, it is difficult to generate carbon dioxide that causes corrosion of the condensate path 30 during heating. For this reason, in this steam boiler apparatus 1, corrosion of the condensate path 30 is also suppressed.

  During the operation of the steam boiler device 1, the hardness component sensor 57, the acid consumption (pH 4.8) sensor 58, and the water temperature sensor 59 are always the hardness component of the makeup water that flows from the preliminary filtration device 54 to the crossflow filtration device 55. Concentration, acid consumption (pH 4.8) and water temperature are each measured. The purpose of measuring the hardness concentration of the makeup water with the hardness sensor 57 is to confirm the treatment status of the makeup water in the water softening device 53, that is, the water softening status. Further, the acid consumption (pH 4.8) of the makeup water is measured by the acid consumption (pH 4.8) sensor 58 to determine the amount of bicarbonate contained in the makeup water from the water softening device 53. The purpose is that. Furthermore, the purpose of measuring the temperature of the makeup water with the water temperature sensor 59 is to predict the amount of dissolved oxygen contained in the makeup water. In the makeup water, the lower the water temperature, the higher the solubility of dissolved oxygen and the more dissolved oxygen amount. Therefore, the tendency of the dissolved oxygen amount can be predicted by the water temperature.

  When the hardness concentration of make-up water measured by the hardness sensor 57 exceeds a predetermined concentration Z set in advance, the breakthrough of the sodium-type cation exchange resin (ion exchange capacity) in the first resin unit 61a of the water softening device 53. Therefore, the control device 70 operates the switching valve 62 to switch the water injection path 51 from the first path 51a to the second path 51b. Thereby, the makeup water from the pretreatment device 52 flows to the second path 51b and is supplied to the second resin unit 61b, and is subjected to ion exchange treatment with the sodium-type cation exchange resin.

  While the water injection channel 51 is switched to the second channel 51b, the first resin unit 61a is removed from the water softening device 53, and the sodium-type cation exchange resin is replaced with a new one. In this way, when the hardness concentration of the make-up water measured by the hardness sensor 57 exceeds the predetermined concentration Z set in advance when the second resin unit 61b is used, the controller 70 causes the water injection channel 51 to be set. By switching from the second path 51b to the first path 51a, the first resin unit 61a in which the sodium-type ion exchange resin has been replaced can be subjected to ion exchange treatment of the makeup water. As described above, if the sodium-type cation exchange resin filled in the resin unit other than the resin unit selected in the resin unit group 61 (that is, the resin unit in use) is replaced while not in use, makeup water When the hardness component concentration exceeds a predetermined concentration Z set in advance, the resin unit can be quickly changed to the other one by switching the switching valve 62. Therefore, the makeup water is softened more reliably in the water softening device 53. As a result, in the water storage tank 40, makeup water having a low hardness is stored as boiler feed water. Therefore, the steam boiler 20 can generate scale effectively without adding chemicals to the boiler feed water. To be suppressed.

  When the acid consumption (pH 4.8) measured by the acid consumption (pH 4.8) sensor 58 exceeds a predetermined value Q, the makeup water from the water softening device 53 has a bicarbonate amount. It can be determined that there are many. Therefore, the control device 70 controls the blow control valve 87 and sets the blow amount of the makeup water circulating in the cross flow filtration device 55 to be larger than the predetermined blow amount X. As a result, in the filtration membrane module 81, the amount of newly supplied makeup water is increased and the circulating makeup water is diluted, so that the bicarbonate concentration in the makeup water to be filtered decreases. As a result, the amount of bicarbonate passing through the filtration membrane is reduced, and the makeup water supplied from the crossflow filtration device 55 to the deoxygenation device 56 is prevented from rising in the bicarbonate concentration. Therefore, since the generation of carbon dioxide gas is suppressed in the steam boiler, corrosion of the condensate passage 30 is suppressed without adding chemicals to the boiler feed water.

  When the acid consumption (pH 4.8) measured by the acid consumption (pH 4.8) sensor 58 returns to the predetermined value Q or less, the control device 70 controls the blow control valve 87 to cross-flow. The blow amount from the mold filtration device 55 is returned to the predetermined blow amount X. As a result, the steam boiler device 1 can suppress the waste of make-up water to the minimum, and can be economically operated.

  Further, when the water temperature of the make-up water measured by the water temperature sensor 59 becomes lower than the predetermined water temperature T, the amount of dissolved oxygen in the make-up water is increased, and it is expected that the deoxygenation process in the deoxygenator 56 is insufficient. Therefore, the control device 70 controls the flow rate control valve 60 to reduce the flow rate of the makeup water flowing from the crossflow filtration device 55 to the deoxygenation device 56 to be less than the predetermined flow rate Y. As a result, the deoxygenation device 56 has a reduced supply flow rate of the make-up water and a longer stay time of the make-up water, thereby increasing the ability to remove dissolved oxygen from the make-up water. Therefore, the water storage tank 40 is supplied with makeup water with a small amount of dissolved oxygen even when the temperature of the makeup water decreases.

  When the water temperature of the make-up water measured by the water temperature sensor 59 returns to the predetermined water temperature T or higher, the control device 70 controls the flow rate control valve 60 and supplies the make-up water flowing from the crossflow filtration device 55 to the deoxygenation device 56. The flow rate is returned to the predetermined flow rate Y.

  As a result, the water storage tank 40 stores the makeup water from which dissolved oxygen has been removed more reliably as boiler feed water. Therefore, the steam boiler apparatus 1 does not need to add chemicals to the boiler feed water. In addition, the corrosion of the steam boiler 20, particularly the progress of pitting corrosion is effectively suppressed.

Modification (1) In the above-described embodiment, the water softening device 53 replaces the sodium-type cation exchange resin of the resin unit that is not in use. When not in use, it can be regenerated in a state where it is mounted on the water softening device 53.

  In this case, a sodium chloride aqueous solution preparation device is provided in the water softening device 53, and the sodium chloride aqueous solution is supplied from this preparation device into an unused resin unit. Thereby, the hardness component adhering to the sodium-type cation exchange resin is again exchanged with sodium ions, and the sodium-type cation exchange resin has an increased ion exchange capacity with the hardness component.

(2) In the above embodiment, the water softening device 53 uses the resin unit group 61 having the two resin units 61a and 61b, but the resin unit group 61 has three or more resin units. May be.

(3) In the above-described embodiment, the hardness sensor 57, the acid consumption (pH 4.8) sensor 58, and the water temperature sensor 59 are arranged between the preliminary filtration device 54 and the crossflow filtration device 55, and make-up water. Concentration, acid consumption (pH 4.8) and water temperature are measured, but the hardness, acid consumption (pH 4.8) and water temperature of make-up water are measured with the water softening device 53 and the prefiltration device 54. Can also be measured. However, in order to increase the deoxygenation capacity of the deoxygenation device 56, the temperature of the makeup water is preferably measured immediately before the crossflow filtration device 55 as in the above-described embodiment.

(4) In the above-described embodiment, the nanofiltration membrane is used as the filtration membrane of the crossflow filtration device 55. However, the nanofiltration membrane can be changed to a reverse osmosis membrane. The reverse osmosis membrane is formed using a synthetic polymer such as polyamide, generally called RO (Reverse Osmosis) membrane. In AMST-002 of AMST (Association of Membrane Separation Technology) standard, “ A membrane with a sodium chloride concentration of 500 to 2,000 mg / liter and an operating pressure of 0.5 to 3.0 MPa under a sodium chloride removal rate of 93% or more ” It is distinguished from. Incidentally, reverse osmosis membranes are commercially available from various companies and can be easily obtained.

  Reverse osmosis membranes are used in various shapes, similar to nanofiltration membranes. That is, the reverse osmosis membrane is used in various shapes such as a flat membrane type, a hollow fiber membrane type, a tubular type, and a Nomoris type.

  The reverse osmosis membrane used in the cross-flow filtration device 55 has a higher ability to remove the corrosion-promoting ionic component and carbonate contained in the makeup water than the nanofiltration membrane. The consumption (pH 4.8) can be further reduced, and corrosion of the steam boiler 20 and the condensate passage 30 can be more effectively suppressed.

(5) In the above-described embodiments, a case where a once-through boiler is used as the steam boiler 20 is taken as an example, but the present invention can be similarly implemented even when another type of steam boiler 20 is used. it can.

1 is a schematic diagram of a steam boiler device that can implement a method for supplying makeup water according to an embodiment of the present invention. Schematic of the water softening device used in the steam boiler device. Schematic of the crossflow type filtration apparatus used in the said steam boiler apparatus. The partial cross section schematic of the steam boiler used in the said steam boiler apparatus.

Explanation of symbols

DESCRIPTION OF SYMBOLS 1 Steam boiler apparatus 2 Load apparatus 20 Steam boiler 30 Condensate path 40 Reservoir tank 50 Replenishment path 53 Water softening apparatus 55 Cross flow type filtration apparatus 56 Deoxygenation apparatus 57 Hardness component sensor 58 Acid consumption (pH 4.8) sensor 59 Water temperature Sensor 60 Flow control valve 61 Resin unit group 61a First resin unit 61b Second resin unit 87 Blow control valve

Claims (3)

The supply water is stored in a storage tank as boiler supply water, steam generated by supplying the boiler supply water from the storage tank to the steam boiler and heating is used in the load device, and the steam is condensed and recovered. In a steam boiler apparatus that collects and reuses water to the water storage tank through a condensate path extending from the load device, a method for supplying the makeup water to the water storage tank,
One resin unit is selected from a resin unit group including at least two resin units having a sodium type cation exchange resin, and the hardness of the replenished water is determined by ion exchange of the selected resin unit with the sodium type ion exchange resin. Removing step A;
The replenishment in which the hardness component is removed by setting a blow amount from the cross flow filtration device to a predetermined blow amount using a cross flow filtration device using one of a nanofiltration membrane and a reverse osmosis membrane Step B for filtering water;
A step C of passing the makeup water filtered in the crossflow filtration device through a deoxygenation device at a predetermined flow rate to remove dissolved oxygen contained in the makeup water;
Supplying the makeup water that has passed through the deoxygenation device to the water storage tank;
Between the step A and the step B, the step E for measuring the hardness concentration, the acid consumption (pH 4.8) and the water temperature of the makeup water,
When the hardness concentration measured in the step E exceeds a predetermined concentration, another resin unit is selected in the resin unit group and the step A is executed, and the acid consumption (pH 4. When 8) exceeds a predetermined value, a blow amount from the crossflow filtration device is set to be larger than the predetermined blow amount in step B, and the water temperature measured in step E is lower than a predetermined temperature. Passing the makeup water through the deoxygenator at a flow rate less than the predetermined flow rate in step C
Supply method of makeup water for boiler water supply.   The said sodium-type cation exchange resin of resin units other than the resin unit selected for the process A is reproduced | regenerated in the said resin unit group, performing the process A, B, C, D, and E. The supply method of the makeup water for boiler feed water as described. The deoxygenation device includes a type that allows the makeup water to pass through a gas separation membrane, a type that allows the makeup water to pass under a reduced pressure environment, and a type that allows the makeup water to pass under a heating environment. The method for supplying boiler water supply water according to claim 1 or 2, wherein the supply water is of one type selected from the group consisting of:

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