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CN112897737A - Drop induced crystallization softening combination matching system and use method - Google Patents

Drop induced crystallization softening combination matching system and use method Download PDF

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CN112897737A
CN112897737A CN202110067847.1A CN202110067847A CN112897737A CN 112897737 A CN112897737 A CN 112897737A CN 202110067847 A CN202110067847 A CN 202110067847A CN 112897737 A CN112897737 A CN 112897737A
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crystal
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CN112897737B (en
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宋武昌
孙韶华
贾瑞宝
米记茹
潘章斌
张素珍
陈发明
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SHANDONG PROVINCE CITY WATER SUPPLY AND DRAINAGE WATER QUALITY MONITORING CENTER
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F7/00—Aeration of stretches of water
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
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    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
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    • C02F2001/5218—Crystallization
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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Abstract

The invention discloses a drop induced crystallization softening combination matching system and a use method thereof, and the drop induced crystallization softening combination matching system comprises a drop aeration device and a crystal inducing pool, wherein the crystal inducing pool comprises a lower induced crystallization sedimentation pool, the drop aeration device comprises a plurality of water pools with sequentially reduced heights, water flow enters from a first water pool at the highest position and sequentially overflows to a water pool at the next lower position to be discharged, the water pool at the lower position is communicated with the upper end part of a water inlet channel through a water inlet pipeline, the lower end part of the water inlet channel is communicated with the bottom part of the induced crystallization sedimentation pool, the water inlet pipeline comprises a self-flowing pipeline and a pressurizing pipeline, the self-flowing pipeline is not provided with a pump, a self-flowing pipeline is provided with a self-flowing pipeline switch valve, the pressurizing pipeline is provided with a pressurizing water pump, and the pressurizing pipeline is provided with. According to the invention, by adopting a drop induced crystallization softening combined process starting mode and a matched system, hardness ions in water can be crystallized and separated out, so that the purpose of hardness removal is achieved, and the treatment cost is reduced while the treatment effect is maintained.

Description

Drop induced crystallization softening combination matching system and use method
Technical Field
The invention relates to the technical field of water treatment engineering, in particular to a drop induced crystallization softening combination matching system and a using method thereof.
Background
The excessive hardness of drinking water has important influence on the life of urban residents, and medical research shows that high-hardness water can cause certain diseases of human beings, for example, the high-hardness water can cause diarrhea and dyspepsia, gastrointestinal dysfunction and other symptoms. Meanwhile, the high hardness causes poor drinking water drinking property, and although the high hardness water can be boiled to generate substances such as sediment, scale and the like, people can also feel uneasy and complain about the mind after drinking the water for a long time, and the health of people is also negatively influenced. It is imperative to seek a more efficient and safe method for removing water hardness.
In recent years, the softening method in domestic and foreign water treatment mainly comprises the following steps: ion exchange softening based on the ion exchange principle, membrane softening based on the electrodialysis principle, chemical softening based on the solubility product, or precipitation softening. The chemical crystallization circulation granulation method is an improvement of a precipitation softening method, and is characterized in that crystal seeds and alkaline agents (sodium hydroxide and sodium carbonate) are put into water, calcium ions and magnesium ions in the water are subjected to chemical reaction to generate precipitated crystals which are attached to the surfaces of the crystal seeds, the crystal grains grow slowly along with the continuous attachment of precipitates, and finally large-particle precipitates are formed and are deposited at the bottom of water to be discharged. The chemical crystallization circulation granulation method meets the requirements of the current social development by virtue of high efficiency, small occupied area and no waste generation, and has wide application and development prospects. In addition, the hardness of iron, manganese and the like in water can be precipitated by an aeration oxidation method.
The existing water treatment softening method is mostly a single treatment process, and the calcium, magnesium, iron and manganese hardness is not generally removed simultaneously, but is rarely removed simultaneously by a drop aeration method and a chemical crystallization circulating granulation method. In addition, the existing crystallization softening tank provides power for the crystal grain layer to maintain a fluidized state by means of water pump pressurization, so that the power consumption is large and not intensive enough. If it is considered that the pressure generated by the height difference is used to maintain the fluidized state of the seed layer, the initial fluidization of the seed layer cannot be accomplished because the water pressure required to accomplish the initial fluidization is greater than the pressure required to maintain the fluidized state.
Disclosure of Invention
The invention aims to overcome the defects in the prior art and provides a drop induced crystallization softening combination matching system. The drop induced crystallization softening combined system of the invention leads hardness ions such as iron, manganese, calcium, magnesium and the like in water to be crystallized and separated out through drop aeration and chemical crystallization circulation granulation, thereby reducing the hardness of water. The crystal inducing softening tank can utilize the water head generated by the height difference to enable the crystal inducing contact tank to maintain a fluidized state, the crystal grains cannot be gradually stopped, the water pressure is not too high to cause crystal grain loss, the pressure required by initial fluidization is higher than the pressure required by stable fluidization, therefore, when the height difference can just meet the pressure required by the crystallization fluidization state in the crystal inducing tank, the crystal inducing tank cannot be automatically started to enable the crystal grains at the bottom of the tank to start fluidization at the moment, the original water head and the water pump are combined to generate enough pressure to flush the bottom crystals, the water pump is stopped after the initial fluidization is completed, and the original water head is utilized to maintain the fluidized state of the crystal grains.
The invention also provides a use method of the drop induced crystallization softening combination matching system. According to the invention, by adopting a drop induced crystallization softening combined process starting mode and a matched system, hardness ions in water can be crystallized and separated out, so that the purpose of hardness removal is achieved, and the treatment cost is reduced while the treatment effect is maintained.
The utility model provides a drop induction crystallization softens combination supporting system, includes drop aeration equipment, lures brilliant pond, it includes the induced crystallization sedimentation tank of lower part to lure brilliant pond, drop aeration equipment includes a plurality of highly the pond that reduce in proper order, and rivers get into from the first pond of highest position, and the pond overflow of following low position and go out in proper order, and the pond of low position passes through inlet channel and inlet channel's upper end intercommunication, inlet channel's lower tip and induced crystallization sedimentation tank bottom intercommunication, inlet channel includes gravity flow pipeline, pressure line, the gravity flow pipeline does not establish the pump, is equipped with gravity flow pipeline switch valve on the gravity flow pipeline, is equipped with pressure water pump on the pressure line, is equipped with pressure line switch valve on the pressure line.
The front section of the pressurizing pipeline is provided with a water suction bell mouth, the pressurizing pipeline and the gravity flow pipeline are connected to the same pipeline of the water inlet channel at the gradually expanding pipe, the tail end of the pipeline of the water inlet channel leads to the bottom of the crystal inducing pool, the pressurizing pipeline is opened for use when the crystal inducing pool is started, the gravity flow pipeline is not opened for use at the moment, the valve of the pressurizing pipeline is closed after the starting is completed, and the gravity flow pipeline is used for maintaining fluidization.
A use method of a drop induced crystallization softening combination matching system comprises the following steps:
1) when the crystal inducing tank is started, a switch valve of a self-flow pipeline is closed, a switch valve of a pressurizing pipeline is opened, a pressurizing water pump of the pressurizing pipeline is started, water is injected into an original pipeline from a self-sucking water bell mouth through the pressurizing water pump, pressurized water flow flushes crystal grains of the crystal inducing tank from the tail end of the pipeline of a water inlet channel, a crystal grain layer is initially fluidized under the action of water flow, and the crystal grain layer reaches the crystal face position after the crystal grain layer is expanded from the crystal face position before the crystal grain layer is expanded;
2) then the switch valve of the gravity flow pipeline is opened, and the pressurizing water pump and the switch valve of the pressurizing pipeline are closed at the same time, so that the inlet water enters the crystal inducing pool through the gravity flow pipeline and flows out from the tail end of the pipeline, and the crystal grain layer maintains a fluidized state under the water pressure generated by the height difference.
In the step 1), in order to enable the crystal grains in the crystal inducing pool to smoothly complete an initial fluidized state, the pressure generated by the height difference between the drop aeration device and the lower part of the crystal inducing pool and a water pump are combined to flush the crystals at the bottom of the crystal inducing pool, after the crystal grains are fluidized, the water pump is stopped, the original water head is used for maintaining the fluidized state, and the flushing strength required by the initial fluidized state of the crystal grains is completed;
the expansion of the grain layer occurs due to partial or total suspension of the grain layer in the ascending water stream during the initial fluidization of the grain layer, and the expansion rate of the grain layer is expressed by the volume of the grain layer after expansion and the volume of the grain layer before expansion, that is, the volume of the grain layer after expansion and the volume of the grain layer before expansion are expressed as
Figure BDA0002904824160000031
Wherein e is the expansion rate of the seed layer,%, V0 is the volume before washing, m3V is the volume at which the initial fluidization is completed, m3。
In the crystal inducing pool, the added crystal inducing particles are quartz sand, and the flushing calculation formula of the crystal particle layer is as follows:
Figure BDA0002904824160000032
in the formula,
Figure BDA0002904824160000033
wherein q is the washing strength of the crystal grain layer, and the unit L/(s-square meter); rho is the density of the crystal grains and has the unit of kg/m3，ρ0Is the density of water in kg/m3D is the grain size of the crystal grain, the unit m, mu is the kinetic viscosity coefficient of water, mu is 1 × 10-3N·s/m2And e is the expansion rate of the grain layer in m0Is the porosity in% of the grain layer before expansion.
Flow and pressure of the bottom tube outflow:
when the bottom of the crystal inducing tank is washed by water, the flow rate of the washing water flowing through the unit area of the crystal grain layer is called washing intensity, and the washing intensity is expressed by the following formula:
q＝Q/A,
wherein the unit of Q is L/(s-square meter), and Q is the backwashing water flow of the crystal grain layer, L/s; a is the plane area of crystal grain layer and square meter.
The expansion rate of the grain layer is represented by volume change, the same plane area A of the grain layer is represented by the base area of a quadrangular prism which has the same volume and the same thickness as the expanded grain layer,
the required amount of flushing water Q a,
according to
Figure BDA0002904824160000041
Calculating the water flow velocity v, m/s of a pipe orifice at the bottom of the pool, wherein d is the diameter m of the pipe;
by the momentum theorem f t m v,
f＝P*π(d/2)2,m＝ρ*v*π(d/2)2t, obtaining
P＝ρv2，
Wherein f is force in units of N, m is mass in units of kg, P is pressure in units of Pa, d is pipe diameter in units of m, ρ is density of water in units of kg/m3V is water flow speed, unit m/s, t is time, unit s, push out bottom pipeline outlet pressure P, convert to water head HPowderIn the unit m.
Calculation of head loss:
and (3) solving the on-way head loss hf and the local head loss hj of the pipeline by using the flow velocity v of the pipeline, wherein the unit is m.
Pipeline on-way head loss hf: in the flowing process of the liquid, the flowing resistance generated on the uniform flow section with the unchanged flowing direction, the roughness of the wall surface, the shape and the area of the flow cross section is the on-way resistance, the influence of the on-way resistance causes the energy loss or the head loss in the flowing process of the fluid, and the on-way resistance is uniformly distributed on the whole uniform flow section and is in direct proportion to the length of the pipe section;
pipeline local head loss hj: in the process of flowing of liquid, the other type of resistance occurs in a flow area with a sharp change on a flow boundary, energy loss is mainly concentrated in the flow area and the adjacent flow area, the energy loss or the resistance which is concentrated occurs is called local resistance, head loss caused by the local resistance is called local head loss, and local head loss occurs at the connection positions of an inlet and an outlet of a pipeline, a variable-section pipeline and the pipeline;
according to the calculation, the lift of the pressurizing pump in the pressurizing pipeline is calculated to be H ═ hf + hj + HPowder-HHeight difference；
Total pressure H required to complete the initial fluidization regimeGeneral assembly＝H+HHeight differenceAnd when the pump lift reaches H, the crystal grain layer in the crystal inducing pool reaches the flushing intensity q required for completing the initial fluidization state.
The invention has the beneficial effects that:
1. the invention separates out the hardness ions of iron, manganese, calcium, magnesium and the like in water by water drop aeration and chemical crystallization circulation granulation, simultaneously removes the hardness of iron, manganese, calcium and magnesium in water, and reduces the hardness of water, thereby solving the problems that the water treatment softening method in the prior art adopts a single treatment process, the hardness of calcium, magnesium and iron and manganese is generally removed simultaneously, and the hardness of calcium, magnesium, iron and manganese is removed simultaneously by the water drop aeration method and the chemical crystallization circulation granulation method in the absence of water. The initial fluidization of the crystal grain layer is completed by utilizing the booster water pump, and meanwhile, the fluidization state is maintained by fully utilizing the height difference between the drop aeration tank and the induced crystallization tank, so that the treatment effect is improved, and the treatment cost is reduced.
2. The crystal inducing softening tank can utilize the water head generated by the height difference to ensure that the crystal inducing contact tank can maintain a fluidized state, can not be gradually stopped, and can not cause crystal grain loss due to overlarge water pressure, and the pressure required by initial fluidization is higher than the pressure required by stable fluidization, so that when the height difference can just meet the pressure required by the crystallization fluidization state in the crystal inducing tank, the crystal inducing tank cannot be automatically started to ensure that the crystal grains at the bottom of the tank start to fluidize, the original water head and the water pump are combined to generate enough pressure to flush the crystals at the bottom, the water pump is stopped after the initial fluidization is completed, the original water head is utilized to maintain the fluidized state of the crystal grains, and the treatment cost is reduced while the treatment effect is maintained.
3. The invention can accurately simulate the actual using state by adopting a formula model of a drop induced crystallization softening combined process, and can reduce the treatment cost and increase the economic benefit while maintaining the treatment effect and enabling hardness ions in water to be crystallized and separated out so as to achieve the purpose of hardness removal. The problems that the conventional crystallization softening tank supplies power to a crystal grain layer to maintain a fluidized state in a multi-purpose water pump pressurizing mode, and the power consumption is large and not intensive enough are solved; and in the prior art, because the water pressure required for completing the initial fluidization is larger than the pressure required for maintaining the fluidization state, the pressure generated by the height difference is utilized to maintain the fluidization state of the crystal grain layer, and the initial fluidization of the crystal grain layer can not be completed.
Drawings
FIG. 1 is a first schematic view of a drop induced crystallization softening combined process with a pressurized water pump according to the present invention;
FIG. 2 is an equivalent diagram of the effective bottom area of the seed layer;
fig. 3 is an equivalent diagram of the effective bottom area of the seed layer of fig. 2.
In the figure, 1, a water suction bell mouth, 2, a gate valve, 3, a pressurized water pump, 4, a pressurized pipeline switch valve, 5, a divergent pipe, 6, a gravity pipeline switch valve, 7, a crystal face position after the expansion of a crystal layer, 8, a crystal face position before the expansion of the crystal layer and 9, a pipeline end.
Detailed Description
In order to make those skilled in the art better understand the technical solution of the present invention, the technical solution in the embodiment of the present invention will be clearly and completely described below with reference to the drawings in the embodiment of the present invention, and it is obvious that the described embodiment is only a part of the embodiment of the present invention, and not all embodiments.
As shown in fig. 1-3, a drop-induced crystallization softening combination supporting system, including drop aeration equipment, lure brilliant pond including the induced crystallization sedimentation tank of lower part, drop aeration equipment includes a plurality of highly pond that reduce in proper order, and rivers get into from the first pond of highest position, overflow and go out to the pond of following low position in proper order, and the pond of low position passes through inlet channel and inhalant canal's upper end intercommunication, and the lower tip of inhalant canal and induced crystallization sedimentation tank bottom intercommunication, inlet channel includes gravity flow pipeline, pressurization pipeline, the gravity flow pipeline does not establish the pump, is equipped with gravity flow switch valve 6 on the gravity flow pipeline, is equipped with pressure water pump 3 on the pressurization pipeline, is equipped with pressure pipeline switch valve 4 on the pressurization pipeline.
The pressurization pipeline anterior segment is equipped with the horn mouth 1 that absorbs water, and pressurization pipeline and gravity flow pipeline are received the same pipeline of inhalant canal in gradually expanding 5 departments on, and inhalant canal's pipeline end 9 leads to lures brilliant bottom of the pool, and the pressurization pipeline uses when luring brilliant pond to start, and the gravity flow pipeline does not use this moment, closes the valve of pressurization pipeline after accomplishing the start-up, uses the gravity flow pipeline to maintain the fluidization.
A use method of a drop induced crystallization softening combination matching system comprises the following steps:
1) before the crystal inducing pool is started, the crystal surface position of the crystal grain layer is as the height shown by the crystal surface position 8 before the crystal grain layer expands in the figure, when the crystal inducing pool is started, a switch valve of a self-flow pipeline is closed, a switch valve of a pressurizing pipeline is opened, a pressurizing water pump of the pressurizing pipeline is started, water is injected into an original pipeline from a water self-sucking bell mouth 1 through the pressurizing water pump 3, pressurized water flow flushes crystal grains of the crystal inducing pool from the tail end 9 of the pipeline, the crystal grain layer finishes initial fluidization under the action of water flow, and the crystal grain layer reaches the crystal surface position 7 after the crystal grain layer expands from the crystal surface position 8 before the crystal grain layer expands;
2) then the switch valve of the gravity flow pipeline is opened, and the pressurizing water pump 3 and the switch valve of the pressurizing pipeline are closed at the same time, so that the inlet water enters the crystal inducing pool through the gravity flow pipeline and flows out from the tail end 9 of the pipeline, and the crystal grain layer maintains a fluidized state under the water pressure generated by the height difference.
Step 1), in order to make the crystal grains in the crystal inducing pool smoothly complete the initial fluidization state, the pressure generated by the height difference between the drop aeration device and the lower part of the crystal inducing pool and the water pump are utilized to jointly flush the crystals at the bottom of the crystal inducing pool, the water pump is stopped after the crystal grains are fluidized, the original water head is utilized to maintain the fluidization state, and the flushing strength required by the initial fluidization state of the crystal grains is completed, and the method is obtained through the following steps:
the size of the crystal grains in the crystal inducing pool is gradually changed, calcium ions in water are continuously crystallized and separated out, calcium carbonate generated by crystallization on the surfaces of the crystal grains is light calcium carbonate, the gaps are large, the stacking density is small, and the relative density of the whole crystal grains is reduced. The volume of the crystal grains is gradually increased, the density is gradually reduced, the buoyancy force is gradually increased, and the crystal grains are easier to be washed by water. The pressure required at the first start-up is at a maximum.
The volume of the layer is increased by suspending the layer partially or completely in the ascending water stream during the initial fluidization of the layer, i.e., the layer is expanded, and the expansion ratio is represented by the volume of the layer after expansion and the volume of the layer before expansion, i.e., the expansion ratio
Figure BDA0002904824160000071
Where e is the expansion ratio of the seed layer, V0 is the volume before flushing, and V is the volume at the completion of the initial fluidization.
In the crystal inducing pool, the added crystal inducing particles are quartz sand, and the flushing calculation formula of the crystal particle layer is as follows:
Figure BDA0002904824160000081
wherein,
Figure BDA0002904824160000082
wherein q is the washing strength of the crystal grain layer, and the unit L/(s-square meter); rho is the density of the crystal grains and has the unit of kg/m3In kg/m of water density3D is the grain size of the crystal grain, the unit m, mu is the kinetic viscosity coefficient of water, mu is 1 × 10-3N·s/m2And e is the expansion rate of the grain layer in m0Is the porosity in% of the grain layer before expansion.
Flow and pressure of the bottom tube outflow:
when the bottom of the crystal inducing tank is washed by water, the flow rate of the washing water flowing through the unit area of the crystal grain layer is called washing intensity, and the washing intensity is expressed by the following formula:
q＝Q/A,
wherein q is the washing strength of the crystal grain layer, L/(s-square meter); q is the backwashing water flow rate of the crystal grain layer, L/s; a is the plane area of crystal grain layer and square meter.
The bottom volume of the crystal inducing pool is not a simple cylinder, the expansion rate of the crystal grain layer is represented by volume change, and the same plane area A of the crystal grain layer is represented by the bottom area of a quadrangular prism which has the same volume and the same thickness as the expanded crystal grain layer.
The required amount of flushing water Q a,
according to
Figure BDA0002904824160000083
The flow velocity v of the water at the bottom of the cell at the orifice can be determined, where d is the diameter of the tube.
By the momentum theorem f t m v,
f＝P*π(d/2)2,m＝ρ*v*π(d/2)2t, obtaining
P＝ρv2，
Wherein, P is pressure, Pa is unit, d is pipe diameter, m is unit, rho is density of water, kg/m3 is unit, v is water velocity, m/s is unit, t is time, s is unit, bottom pipeline outlet pressure P is pushed out and converted into water head HPowderIn the unit m.
Calculation of head loss:
and then, calculating the on-way head loss hf and the local head loss hj of the pipeline by utilizing the flow velocity v of the pipeline.
Pipeline on-way head loss hf: in the flowing process of the liquid, the flow resistance generated on the uniform flow section with constant flowing direction, wall roughness, and shape and area of the flow cross section is called as along-way resistance or friction resistance. The effect of on-way resistance, which causes loss of energy or head loss during fluid flow, is evenly distributed throughout the uniform flow section, proportional to the length of the pipe section.
Pipeline local head loss hj: in the process of flowing liquid, another type of resistance occurs in a flow area with a sharp change of a flow boundary, energy loss is mainly concentrated in the flow area and a nearby flow area, the concentrated energy loss or resistance is called local resistance or local loss, and head loss caused by the local resistance is called local head loss. Usually, local head loss occurs at the inlet and outlet of the pipeline, the variable cross-section pipeline, the joint of the pipeline and other positions.
From the above calculation, the head of the pressurizing pump in the pressurizing pipeline can be calculated to be H ═ hf + hj + HPowder-HHeight difference；
Total pressure H required to complete the initial fluidization regimeGeneral assembly＝H+HHeight difference. Aims to make full use of the original height difference and save energy. Namely, when the pump head reaches H, the crystal grain layer in the crystal inducing pool can reach the flushing intensity q required for completing the initial fluidization state.
In the description of the present invention, the terms "upper", "lower", "front", "rear", "left", "right", "top", "bottom", "vertical", "horizontal", and the like indicate orientations or positional relationships based on those shown in the drawings, and are only for the purpose of describing the present invention but do not require that the present invention must be constructed or operated in a specific orientation, and thus, should not be construed as limiting the present invention. The terms "connected" and "connected" in the present invention should be interpreted broadly, and may be connected or disconnected, for example; the terms may be directly connected or indirectly connected through intermediate components, and specific meanings of the terms may be understood as specific conditions by those skilled in the art.
The above description is of the preferred embodiment of the present invention, and the description of the specific embodiment is only for better understanding of the idea of the present invention. It will be appreciated by those skilled in the art that various modifications and equivalents may be made in accordance with the principles of the invention and are considered to be within the scope of the invention.

Claims (6)

1. The utility model provides a drop induction crystallization softens combination supporting system, includes drop aeration equipment, lures brilliant pond, characterized by, it includes the induced crystallization sedimentation tank of lower part to lure brilliant pond, drop aeration equipment includes a plurality of highly pond that reduce in proper order, and rivers get into from the first pond of highest position, and overflow and go out to the pond of following low position in proper order, and the pond of low position passes through inlet channel and inlet channel's upper end intercommunication, inlet channel's lower tip and induced crystallization sedimentation tank bottom intercommunication, inlet channel includes gravity flow pipeline, pressurization pipeline, the gravity flow pipeline does not establish the pump, is equipped with gravity flow pipeline switch valve on the gravity flow pipeline, is equipped with pressure water pump on the pressurization pipeline, is equipped with pressure line switch valve on the pressurization pipeline.
2. The drop induced crystallization softening combination matching system as claimed in claim 1, wherein the front section of the pressurizing pipeline is provided with a water suction bell mouth, the pressurizing pipeline and the gravity flow pipeline are connected to the same pipeline of the water inlet channel at the gradually expanding part, the pipeline end of the water inlet channel is communicated with the bottom of the crystal inducing pool, the pressurizing pipeline is opened for use when the crystal inducing pool is started, the gravity flow pipeline is not opened for use, the valve of the pressurizing pipeline is closed after the start, and the gravity flow pipeline is used for maintaining fluidization.
3. A method of using a drop induced crystallization softening combination kit as claimed in claim 1 or 2, comprising the steps of:
1) when the crystal inducing tank is started, a switch valve of a self-flow pipeline is closed, a switch valve of a pressurizing pipeline is opened, a pressurizing water pump of the pressurizing pipeline is started, water is injected into an original pipeline from a self-sucking water bell mouth through the pressurizing water pump, pressurized water flow flushes crystal grains of the crystal inducing tank from the tail end of the pipeline of a water inlet channel, a crystal grain layer is initially fluidized under the action of water flow, and the crystal grain layer reaches the crystal face position after the crystal grain layer is expanded from the crystal face position before the crystal grain layer is expanded;
2) then the switch valve of the gravity flow pipeline is opened, and the pressurizing water pump and the switch valve of the pressurizing pipeline are closed at the same time, so that the inlet water enters the crystal inducing pool through the gravity flow pipeline and flows out from the tail end of the pipeline, and the crystal grain layer maintains a fluidized state under the water pressure generated by the height difference.
4. The use method of the drop induced crystallization softening combination supporting system as claimed in claim 3, wherein in the step 1), in order to make the crystal grains in the crystal inducing tank smoothly complete the initial fluidization state, the pressure generated by the height difference between the drop aeration device and the lower part of the crystal inducing tank and the water pump are combined to flush the crystals at the bottom of the crystal inducing tank, after the crystal grains are fluidized, the water pump is stopped, the original water head is used for maintaining the fluidization state, and the flushing strength required by the crystal grains to complete the initial fluidization state is achieved;
the expansion of the grain layer occurs due to partial or total suspension of the grain layer in the ascending water stream during the initial fluidization of the grain layer, and the expansion rate of the grain layer is expressed by the volume of the grain layer after expansion and the volume of the grain layer before expansion, that is, the volume of the grain layer after expansion and the volume of the grain layer before expansion are expressed as
Figure FDA0002904824150000021
Wherein e is the expansion rate of the seed layer,%, V0 is the volume before washing, m3V is the volume at which the initial fluidization is completed, m3。
5. The use method of the drop induced crystallization softening combination matching system as claimed in claim 4, wherein in the crystal inducing tank, the added crystal inducing particles are quartz sand, and the flushing calculation formula of the crystal particle layer is as follows:
Figure FDA0002904824150000022
in the formula,
Figure FDA0002904824150000023
wherein q is the washing strength of the crystal grain layer, and the unit L/(s-square meter); rho is the density of the crystal grains and has the unit of kg/m3，ρ0Is the density of water inkg/m3D is the grain size of the crystal grain, the unit m, mu is the kinetic viscosity coefficient of water, mu is 1 × 10-3N·s/m2And e is the expansion rate of the grain layer in m0Is the porosity in% of the grain layer before expansion.
Flow and pressure of the bottom tube outflow:
when the bottom of the crystal inducing tank is washed by water, the flow rate of the washing water flowing through the unit area of the crystal grain layer is called washing intensity, and the washing intensity is expressed by the following formula:
q＝Q/A,
wherein Q is the backwash water flow rate of the crystal grain layer, L/s; a is the plane area of crystal grain layer and square meter.
6. The method of using the drop induced crystallization softening combination complete set system as claimed in claim 5, wherein the expansion rate of the grain layer is represented by volume change, the same plane area A of the grain layer is represented by the base area of a quadrangular prism with the same volume and thickness as the expanded grain layer,
the required amount of flushing water Q a,
according to
Figure FDA0002904824150000031
Calculating the water flow velocity v, m/s of a pipe orifice at the bottom of the pool, wherein d is the diameter m of the pipe;
by the momentum theorem f t m v,
f＝P*π(d/2)2,m＝ρ*v*π(d/2)2t, obtaining
P＝ρv2，
Wherein f is force in units of N, m is mass in units of kg, P is pressure in units of Pa, d is pipe diameter in units of m, ρ is density of water in units of kg/m3V is water flow speed, unit m/s, t is time, unit s, push out bottom pipeline outlet pressure P, convert to water head HPowderIn the unit m.
Calculation of head loss:
calculating the on-way head loss hf and the local head loss hj of the pipeline by using the flow velocity v of the pipeline;
pipeline on-way head loss hf: in the flowing process of the liquid, the flowing resistance generated on the uniform flow section with the unchanged flowing direction, the roughness of the wall surface, the shape and the area of the flow cross section is the on-way resistance, the influence of the on-way resistance causes the energy loss or the head loss in the flowing process of the fluid, and the on-way resistance is uniformly distributed on the whole uniform flow section and is in direct proportion to the length of the pipe section;
pipeline local head loss hj: in the process of flowing of liquid, the other type of resistance occurs in a flow area with a sharp change on a flow boundary, energy loss is mainly concentrated in the flow area and the adjacent flow area, the energy loss or the resistance which is concentrated occurs is called local resistance, head loss caused by the local resistance is called local head loss, and local head loss occurs at the connection positions of an inlet and an outlet of a pipeline, a variable-section pipeline and the pipeline;
according to the calculation, the lift of the pressurizing pump in the pressurizing pipeline is calculated to be H ═ hf + hj + HPowder-HHeight difference；
Total pressure H required to complete the initial fluidization regimeGeneral assembly＝H+HHeight differenceAnd when the pump lift reaches H, the crystal grain layer in the crystal inducing pool reaches the flushing intensity q required for completing the initial fluidization state.
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