CN103790059B - Adopt the medium consistency refining device and method of middle underflow pump charging - Google Patents
Adopt the medium consistency refining device and method of middle underflow pump charging Download PDFInfo
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Abstract
The invention discloses the medium consistency refining devices and methods therefor adopting middle underflow pump charging.In this device, the charging aperture of dense double wire decker is connected with pulp-inlet pipe, and discharging opening is connected with the charging aperture of spiral smashing conveyor; The discharging opening of spiral smashing conveyor is connected with the charging aperture of standpipe, and the discharging opening of institute's standpipe is connected with the charging aperture of middle underflow pump; The feed end of separator tube is connected with the discharging opening of middle underflow pump by middle underflow pump grout outlet, the discharge end of separator tube with in the charging aperture of dense disc mill be connected; Described overflow pipe is connected with the overfall on separator tube; In the discharging opening of dense disc mill be connected with grout outlet; The water inlet of water sealed tank by pipeline with in the back flow water pump of dense double wire decker export and be connected; The present invention, by regulating, controlling flow and the concentration of the low-consistency stock in pulp-inlet pipe road, ensure that the paper pulp in the standpipe before middle underflow pump has stable liquid level and stable concentration, and in effectively ensureing, dense disc mill obtains stable refining pulp quality and effect.
Description
Technical field
The present invention relates to a kind of making beating technology of pulping and paper-making, particularly relate to a kind of medium consistency refining device and method adopting middle underflow pump charging.
Background technology
In dense disc mill obtain in China paper mill in recent years and apply more widely, and in keeping entering, the concentration of paper pulp of dense disc mill and the stable of flow have important impact for the good beating results of acquisition.When disc mill dense during certain density paper pulp enters is pulled an oar, if in pulping process, in the power of motor of dense disc mill and the flow of paper pulp all maintain in the excursion of the permission that sets, or in the dense power of disc mill motor and the ratio of pulp flow maintain in the excursion of the permission that sets, in then can ensureing, dense disc mill is pulled an oar under stable refining strength, and obtains stable beating results.In dense disc mill pull an oar under the pulp density of 6 ~ 12%, the poor fluidity of paper pulp, must adopt middle underflow pump to carry, and the equipment being equipped with vavuum pump and turbulator etc. auxiliary.But find in actual production, the slurry adopting middle underflow pump to export is a kind of Pulsating Flow, the pressure of paper pulp and flowed fluctuation are comparatively large, cause bad impact to the normal work of disc mill.On the other hand, when the working condition in producing is unstable, the concentration of paper pulp also produces fluctuation to a certain degree.When by the pressure of paper pulp in dense disc mill mill district, flow and concentration there is larger fluctuation time, in dense disc mill cannot pull an oar under stable refining strength, refining process is difficult to control, thus causes the instability of defibrination quality and refining effect.
Chinese invention patent application 201010522397.2 provides a kind of medium consistency refining pumping method, the method is by regulating the plain boiled water control valve on white water piping, to in add plain boiled water in dense standpipe, to diluting through the slurry that dehydration is concentrated, its concentration is made to reach setting value, underflow material in formation; Because in dense slurry fluidity very poor, be difficult to middle underflow material and the plain boiled water that adds to mix, and in agitating device is not set in dense standpipe, in inevitably causing middle underflow pump to export, dense slurry concentration is unstable, and have impact on the effect of making beating.During although the method that Chinese invention patent application 201010522397.2 provides have adjusted to a certain extent dense pump and in the pulsation of pulp pressure between dense disc mill and pulp flow; But paper pulp is incompressible fluid, and the capacity of buffer is limited, and middle underflow pump and in pipeline between dense disc mill does not arrange overflow mechanism, therefore still there is fluctuation to a certain degree through the pulp flow of buffer and pressure; And buffer and in slurry control valve that pipeline between dense disc mill and pipeline are installed expand enter in the pressure of paper pulp before dense disc mill and the degree of flowed fluctuation, have impact on the stability of beating results; In addition, middle underflow pump and in pipeline between dense disc mill does not arrange overflow mechanism, the pulp flow entering disc mill can only be realized by the aperture controlling the valve on middle underflow pump pulp pipeline, therefore, frequent must regulate the valve on middle underflow pump pulp pipeline with dense disc mill in meeting to the requirement of pulp flow, and this expands the pulsation of pulp flow and pressure.
Summary of the invention
The object of the invention is to the shortcoming overcoming prior art, a kind of medium consistency refining devices and methods therefor obtaining the employing middle underflow pump charging of stable refining pulp quality and effect is provided.
Object of the present invention is achieved through the following technical solutions:
Adopt the medium consistency refining device of middle underflow pump charging, comprise flow control system, in dense double wire decker, spiral smashing conveyor, standpipe, middle underflow pump, separator tube, in dense disc mill, water sealed tank and white water pump; In described, the charging aperture of dense double wire decker is connected with pulp-inlet pipe, and discharging opening is connected with the charging aperture of spiral smashing conveyor; The discharging opening of described spiral smashing conveyor is connected with the charging aperture of standpipe, and the discharging opening of described standpipe is connected with the charging aperture of middle underflow pump; The feed end of separator tube is connected with the discharging opening of middle underflow pump by middle underflow pump grout outlet, the discharge end of separator tube with in the charging aperture of dense disc mill be connected; Described overflow pipe is connected with the overfall on separator tube; Overfall on described separator tube be arranged on separator tube leading portion front 1/3 ?2/3 tube wall on; In described, the discharging opening of dense disc mill is connected with grout outlet; The water inlet of described water sealed tank by pipeline with in the back flow water pump of dense double wire decker export and be connected; The water inlet of described white water pump is connected with the delivery port of water sealed tank by pipeline, and the delivery port of white water pump is connected with pulp-inlet pipe by white water pipe;
Described separator tube is ladder pipe, the internal diameter of the separator tube leading portion be connected with middle underflow pump grout outlet is 1.5 ~ 2 times of middle underflow pump grout outlet internal diameter, with in the internal diameter of separator tube back segment that is connected of dense disc mill charging aperture be 3 ~ 5 times of middle underflow pump grout outlet internal diameter, described separator tube back segment directly with in the charging aperture of dense disc mill be connected.
Described flow control system comprises flowmeter, densimeter, liquid level gauge enter to starch control valve, pulp control valve, overflow control valve, plain boiled water control valve and Programmable Logic Controller; Flowmeter, densimeter are connected with Programmable Logic Controller respectively with liquid level gauge; Flowmeter comprises first-class gauge, second gauge, the 3rd flowmeter and the 4th flowmeter; Densimeter comprises the first densimeter and the second densimeter; Described pulp-inlet pipe is arranged for regulate pulp flow enter to starch control valve, described middle underflow pump grout outlet being arranged for regulating middle underflow pump to export the flow control valve of paper pulp, described overflow pipe being arranged the overflow control valve for regulating paper pulp spillway discharge; Described white water pipe is arranged the plain boiled water control valve for regulating plain boiled water flow; Pulp-inlet pipe is provided with the first densimeter and first-class gauge, standpipe is provided with liquid level gauge, separator tube leading portion is provided with the second densimeter and second gauge, overflow pipe is provided with the 3rd flowmeter, grout outlet is provided with the 4th flowmeter.
For realizing the object of the invention further, preferably, the second described densimeter is connected with the first densimeter, and the first densimeter is connected with plain boiled water control valve; Liquid level gauge is connected with first-class gauge, first-class gauge with enter to starch control valve and be connected; 4th flowmeter is connected with second gauge, and second gauge is connected with middle underflow pump pulp control valve; Second gauge is also connected with the 3rd flowmeter, and the 3rd flowmeter is connected with overflow control valve.It is described that to enter to starch control valve, middle underflow pump pulp control valve, overflow control valve and plain boiled water control valve be manual modulation valve or automatic regulating valve; Described when to enter to starch control valve, middle underflow pump pulp control valve, overflow control valve and plain boiled water control valve be automatic regulating valve, enter to starch control valve, middle underflow pump pulp control valve, overflow control valve be connected with Programmable Logic Controller respectively with plain boiled water control valve.In described, dense disc mill, middle underflow pump and water sealed tank are all arranged in same plane; Or middle underflow pump and water sealed tank are all arranged in same plane, in dense disc mill be arranged in another higher plane.The axial length of described separator tube is not less than 3 meters, and wherein after separator tube leading portion and separator tube, Length Ratio is 0.5:1 ?2:1.
Adopt a medium consistency refining method for middle underflow pump charging, comprise following technique:
1) refining strength value R0 required for dense Disc Refiner Beating Process in setting, then according in the rated power W0 of dense disc mill, determine, based on the paper pulp stream value Q0 of dense disc mill in the passing through of rated power W0, to make R0=W0/Q0;
2) dense double wire decker in being delivered to by pulp by pulp-inlet pipe, is carried out dehydration to slurry and is concentrated into setting value; By regulating the plain boiled water control valve on white water piping to add plain boiled water to pulp-inlet pipe, the pulp density of dense double wire decker in entering is made to reach setting value; The concentration of paper pulp in real-time detection pulp-inlet pipe, and control the aperture of plain boiled water control valve; When the pulp density that the middle underflow pump that densimeter detects in real time exports departs from range of set value, in entering, the setting value of the pulp density of dense double wire decker needs to adjust, be specially: when the pulp density that the middle underflow pump that densimeter detects in real time exports is higher than range of set value, reduce the setting value of the pulp density of dense double wire decker in entering; When the pulp density that the middle underflow pump that densimeter detects in real time exports is lower than range of set value, improve the setting value of the pulp density of dense double wire decker in entering;
3) slurry concentrated through dehydration is carried out fragmentation by spiral smashing conveyor, and deliver into standpipe;
4) paper pulp of standpipe is transported to separator tube through middle underflow pump grout outlet by middle underflow pump, flow control system detects the pulp flow Qin of middle underflow pump output in real time by the second gauge on separator tube leading portion, detect the pulp flow Qout by disc mill in real time by the 4th flowmeter on grout outlet, detect by the 3rd flowmeter on overflow pipe the pulp flow Qy overflowed from overflow pipe in real time; Then the aperture of middle underflow pump pulp control valve and flow spill valve is controlled by flow control system, pulp flow Q0 large 10% that the pulp flow Qin that in fill process, middle underflow pump exports is set than disc mill or more, thus make in overflow pipe, have paper pulp to overflow all the time; Flow control system according in the operating power W of dense disc mill and the pulp flow Qout by disc mill that detects in real time, calculate real-time refining strength R=W/Qout, ratio R/the R0 controlling the refining strength of real-time refining strength and setting is 95 ~ 105%, as the ratio R/R0<95% of the refining strength of real-time refining strength and setting, the aperture of flow spill valve is strengthened by flow control system, increase the pulp flow Qy by overflow pipe, be reduced by the pulp flow Qout of disc mill; As the ratio R/R0>105% of the refining strength of real-time refining strength and setting, reduced the aperture of flow spill valve by flow control system, be reduced by the pulp flow Qy of overflow pipe, increase the pulp flow Qout by disc mill; By above adjustment, the ratio R/R0 finally making the refining strength of real-time refining strength and setting is 95 ~ 105%, reaches the object of stable refining strength; In separator tube, the flow velocity of paper pulp declines, and after the flow pulsation of paper pulp effectively weakens or eliminates, dense disc mill in entering, in warp, the slurry of dense disc mill process exports from grout outlet.
Compared with prior art, the present invention has the following advantages:
1, the present invention is by regulating, controlling flow and the concentration of the low-consistency stock in pulp-inlet pipe road, ensure that the paper pulp in the standpipe before middle underflow pump has stable liquid level and stable concentration well, ensure that middle underflow pump has stable pumpability, in effectively ensureing, dense disc mill obtains stable refining pulp quality and effect.
2, the present invention take middle underflow pump and in connecting pipe between dense disc mill arranges overflow pipe and flow spill valve, detected in real time by flow control system, control by the dense disc mill mill pulp flow in district and the spillway discharge by overflow pipe, the power of dense disc mill is made to maintain in the excursion of the permission that sets with the ratio of the pulp flow by grinding district, ensure that disc mill is pulled an oar under stable refining strength, thus obtain stable refining pulp quality and effect.
3, the present invention by middle underflow pump and in connecting pipe between dense disc mill is arranged with in the staged separator tube that is directly connected of dense disc mill charging aperture, and overfall is set on separator tube, the pressure of paper pulp and flow pulsation are obtained gradually, cushion fully, discharges and greatly reduce, ensure the pressure of the paper pulp of dense disc mill in entering and the stable of flow;
4, the present invention exports pulp flow and controlling water kick amount by stablizing middle underflow pump, ensure that disc mill obtains stable beating results, greatly reduce the frequency regulating middle underflow pump outlet valve, middle underflow pump is run under stable flow, and decreases the pulsation of pulp flow and pressure.
Accompanying drawing explanation
Fig. 1 is the structural representation that embodiment 1 adopts the medium consistency refining device of middle underflow pump charging.
Fig. 2 is the structural representation that embodiment 2 adopts the medium consistency refining device of middle underflow pump charging.
Detailed description of the invention
Below in conjunction with drawings and Examples, the invention will be further described, but the scope of protection of present invention is not limited to the scope that embodiment is stated.
Embodiment 1
As shown in Figure 1, adopt the medium consistency refining device of middle underflow pump charging, comprise flow control system, in dense double wire decker 2, spiral smashing conveyor 3, standpipe 4, middle underflow pump 5, separator tube 7, in dense disc mill 8, water sealed tank 11 and white water pump 12; In described, the charging aperture of dense double wire decker 2 is connected with pulp-inlet pipe 1, and its discharging opening is connected with the charging aperture of spiral smashing conveyor 3; The discharging opening of described spiral smashing conveyor 3 is connected with the charging aperture of standpipe 4, and the discharging opening of described standpipe 4 is connected with the charging aperture of middle underflow pump 5; The feed end of separator tube 7 is connected with the discharging opening of middle underflow pump 5 by middle underflow pump grout outlet 6, the discharge end of separator tube 7 with in the charging aperture of dense disc mill 8 be connected; Described overflow pipe 10 and the overfall 7 on separator tube 7 ?3 to be connected, overfall on described separator tube 77 ?3 be arranged on separator tube leading portion 7 ?1 front 1/3 ?2/3 tube wall on; In described, the discharging opening of dense disc mill 8 is connected with grout outlet 9; The water inlet of described water sealed tank 11 by pipeline with in the back flow water pump of dense double wire decker 2 export and be connected; The water inlet of described white water pump 12 is connected by the delivery port of pipeline with water sealed tank 11, and the delivery port of white water pump 12 is connected with pulp-inlet pipe 1 by white water pipe 26;
Separator tube 7 is ladder pipe, the separator tube leading portion 7 be connected with middle underflow pump grout outlet 6 ?1 internal diameter be 1.5 ~ 2 times of middle underflow pump grout outlet 6 internal diameter, with in the separator tube back segment 7 that is connected of dense disc mill 8 charging aperture ?2 internal diameter be 3 ~ 5 times of middle underflow pump grout outlet 6 internal diameter, the axial length of separator tube 7 is not less than 3 meters; Wherein after separator tube leading portion and separator tube, Length Ratio is 0.5:1 ?2:1; Described separator tube back segment 7 ?2 directly with in the charging aperture of dense disc mill 8 be connected;
Flow control system comprises flowmeter, densimeter, liquid level gauge enter to starch control valve 13, pulp control valve 14, overflow control valve 15, plain boiled water control valve 16 and Programmable Logic Controller (PLC); Flowmeter, densimeter are connected with Programmable Logic Controller respectively with liquid level gauge; Flowmeter comprises first-class gauge 18, second gauge 21, the 3rd flowmeter 22 and the 4th flowmeter 23; Densimeter comprises the first densimeter 17 and the second densimeter 20; Pulp-inlet pipe 1 is provided with can be used for regulate pulp flow enter to starch control valve 13, middle underflow pump grout outlet 6 is provided with and can be used for regulating middle underflow pump to export the pulp control valve 14 of pulp flow, overflow pipe 10 is provided with the overflow control valve 15 that can be used for regulating paper pulp spillway discharge; Described white water pipe 26 is provided with the plain boiled water control valve 16 that can be used for regulating plain boiled water flow; Pulp-inlet pipe 1 is provided with the first densimeter 17 and first-class gauge 18, standpipe 4 is provided with liquid level gauge 19, separator tube leading portion 7 ?be provided with the second densimeter 20 and second gauge 21 on 1, overflow pipe 10 is provided with the 3rd flowmeter 22, grout outlet 9 is provided with the 4th flowmeter 23; Second densimeter 20 is connected with the first densimeter 17, and the first densimeter 17 is connected with plain boiled water control valve 16, and the first densimeter 17 controls the aperture of plain boiled water control valve 16; Liquid level gauge 19 is connected with first-class gauge 18, first-class gauge 18 with enter to starch control valve 13 and be connected, first-class gauge 18 controls the aperture into slurry control valve 13; 4th flowmeter 23 is connected with second gauge 21, and second gauge 21 is connected with pulp control valve 14, and second gauge 21 controls the aperture of pulp control valve 14; Second gauge 21 is also connected with the 3rd flowmeter 22, and the 3rd flowmeter 22 is connected with overflow control valve 15, the aperture of the 3rd flowmeter 22 controlling water kick control valve 15.
Middle underflow pump grout outlet 6 and separator tube back segment 7 ?2 are respectively arranged with the first Pressure gauge 24 and the second Pressure gauge 25;
Enter to starch control valve 13, pulp control valve 14, overflow control valve 15 and plain boiled water control valve 16 for manual modulation valve or automatic regulating valve; When entering to starch control valve 13, pulp control valve 14, overflow control valve 15 and plain boiled water control valve 16 for automatic regulating valve, be connected with Programmable Logic Controller respectively.Flow control system passes through the value of the real-time detectable concentration meter of Programmable Logic Controller and flowmeter, and the mode regulated with PID controls, regulates aperture, the action of each valve.
In dense disc mill 8 be arranged on 1st floor of workshop, in that is to say, dense disc mill 8, middle underflow pump 5 are all arranged in same plane with water sealed tank 11.
The method of the medium consistency refining of the middle underflow pump charging of this employing said apparatus, comprises following technical process:
1) the refining strength value R0=110kWh/t in setting required for dense Disc Refiner Beating Process starches, again according in the rated power W0=315kW of dense disc mill, calculate, setting one based on the paper pulp stream value Q0=2.86t of dense disc mill in the passing through of rated power W0 starch/hour, make R0=W0/Q0;
2) by pulp-inlet pipe 1 by mass concentration be 4 ~ 5% slurry transferring in dense double wire decker 2, dehydration is carried out to slurry and is concentrated into setting value mass concentration 12%; By regulating the plain boiled water control valve 16 on white water piping to add plain boiled water to pulp-inlet pipe 1, the pulp density of dense double wire decker in entering is made to reach setting value mass concentration 4%; In this process, the first densimeter detects the concentration of paper pulp in pulp-inlet pipe in real time, and controls the aperture of plain boiled water control valve 16;
Detect the pulp density of middle underflow pump output particular by the second densimeter 20 in real time, then adjust the setting value of the pulp density of dense double wire decker 2 in entering; And controlled the aperture of plain boiled water control valve 16 by the first densimeter 17, thus regulate the concentration of paper pulp on pulp-inlet pipe 1; Detected the liquid level of paper pulp in standpipe by the liquid level gauge 19 on standpipe 4 in real time, then regulate the flow of paper pulp in pulp-inlet pipe 1;
When the pulp density that the first densimeter 17 on pulp-inlet pipe detects in real time be less than 3.7% or be greater than 4.3% time, plain boiled water control valve on white water piping needs adjustment, be specially: when the pulp quality concentration that the first densimeter 17 on pulp-inlet pipe 1 detects in real time lower than 3.7% time, need the aperture of the plain boiled water control valve reduced on white water piping; When the pulp density that the first densimeter 17 on pulp-inlet pipe 1 detects in real time higher than 4.3% time, need the aperture of the plain boiled water control valve strengthened on white water piping;
When the pulp density value that middle underflow pump that the second densimeter on separator tube 7 detects in real time exports be less than 11% or be greater than 13% time, in entering, the concentration set point of the paper pulp of dense double wire decker 2 needs to adjust, be specially: when the pulp density value that the middle underflow pump that the second densimeter 20 on separator tube 7 detects in real time exports is less than 11%, need to improve the concentration set point of the paper pulp of dense double wire decker in entering; When the pulp density value that the middle underflow pump that the second densimeter 20 on separator tube 7 detects in real time exports is greater than 13%, need to reduce the concentration set point of the paper pulp of dense double wire decker 2 in entering;
3) slurry concentrated through dehydration is carried out fragmentation by spiral smashing conveyor, and deliver into standpipe;
4) paper pulp of standpipe 4 is transported to separator tube 7 through middle underflow pump grout outlet by middle underflow pump 5, in separator tube 7, the flow velocity of paper pulp declines, after the flow pulsation of paper pulp effectively weakens or eliminates, dense disc mill 8 in entering, through in the slurry that processes of dense disc mill 8 export from grout outlet;
Flow control system by separator tube leading portion 7 ?second gauge 21 on 1 detect the pulp flow Qin that middle underflow pump exports in real time, detect the pulp flow Qout by disc mill in real time by the 4th flowmeter 23 on grout outlet, detect by the 3rd flowmeter 22 on overflow pipe the pulp flow Qy overflowed from overflow pipe in real time; Then the aperture of middle underflow pump pulp control valve 14 and flow spill valve 15 is controlled by flow control system (second gauge 21 and the 3rd flowmeter 22), make the pulp flow Q0 large 10 ~ 15% that the pulp flow Qin that in fill process, middle underflow pump exports sets than disc mill, thus make in overflow pipe, have paper pulp to overflow all the time.
Flow control system according in the operating power W of dense the disc mill 8 and pulp flow Qout by disc mill that detects in real time, calculate real-time refining strength R=W/Qout, ratio R/the R0 controlling the refining strength of real-time refining strength and setting is 95 ~ 105%, as the ratio R/R0<95% of the refining strength of real-time refining strength and setting, the aperture of flow spill valve is strengthened by flow control system, increase the pulp flow Qy by overflow pipe, thus be reduced by the pulp flow Qout of disc mill; As the ratio R/R0>105% of the refining strength of real-time refining strength and setting, reduced the aperture of flow spill valve by flow control system, be reduced by the pulp flow Qy of overflow pipe, thus increase the pulp flow Qout by disc mill; By above adjustment, the ratio R/R0 finally making the refining strength of real-time refining strength and setting is 95 ~ 105%, reaches the object of stable refining strength.
Embodiment 2
Fig. 2 is the schematic diagram of the medium consistency refining device of the employing middle underflow pump charging of the present embodiment.As shown in Figure 2, embodiment 2 is with the difference of embodiment 1, and in embodiment 2, dense disc mill 8 is arranged on 2nd floors of workshop, and in embodiment 1 in dense disc mill be arranged on 1st floor of workshop.Middle underflow pump 5 and water sealed tank 11 are all arranged in same plane, and in dense disc mill 8 be arranged in another higher plane.
The method of the medium consistency refining of the middle underflow pump charging of this employing Fig. 2 device, comprises following technical process:
1) the refining strength value R0=70kWh/t in setting required for dense Disc Refiner Beating Process starches, again according in the rated power W0=315kW of dense disc mill, calculate, setting one based on the paper pulp stream value Q0=4.5t of dense disc mill in the passing through of rated power W0 starch/hour, make R0=W0/Q0;
2) dense double wire decker 2 during the pulp being 4 ~ 5% by mass concentration by pulp-inlet pipe 1 is delivered to, carries out dehydration to slurry and is concentrated into setting value mass concentration 10%; By regulating the plain boiled water control valve 16 on white water piping to add plain boiled water to pulp-inlet pipe 1, the pulp density of dense double wire decker in entering is made to reach setting value mass concentration 4%; In this process, the first densimeter detects the concentration of paper pulp in pulp-inlet pipe in real time, and controls the aperture of plain boiled water control valve 16;
Detect the pulp density of middle underflow pump output particular by the second densimeter 20 in real time, then adjust the setting value of the pulp density of dense double wire decker 2 in entering; And controlled the aperture of plain boiled water control valve 16 by the first densimeter 17, thus regulate the concentration of paper pulp on pulp-inlet pipe 1; Detected the liquid level of paper pulp in standpipe by the liquid level gauge 19 on standpipe 4 in real time, then regulate the flow of paper pulp in pulp-inlet pipe 1;
When the pulp density that the first densimeter 17 on pulp-inlet pipe detects in real time be less than 3.7% or be greater than 4.3% time, plain boiled water control valve on white water piping needs adjustment, be specially: when the pulp quality concentration that the first densimeter 17 on pulp-inlet pipe 1 detects in real time lower than 3.7% time, need the aperture of the plain boiled water control valve reduced on white water piping; When the pulp density that the first densimeter 17 on pulp-inlet pipe 1 detects in real time higher than 4.3% time, need the aperture of the plain boiled water control valve strengthened on white water piping;
When the pulp density value that middle underflow pump that the second densimeter on separator tube 7 detects in real time exports be less than 9% or be greater than 11% time, in entering, the concentration set point of the paper pulp of dense double wire decker 2 needs to adjust, be specially: when the pulp density value that the middle underflow pump that the second densimeter 20 on separator tube 7 detects in real time exports is less than 9%, need to improve the concentration set point of the paper pulp of dense double wire decker in entering; When the pulp density value that the middle underflow pump that the second densimeter 20 on separator tube 7 detects in real time exports is greater than 11%, need to reduce the concentration set point of the paper pulp of dense double wire decker 2 in entering;
3) slurry concentrated through dehydration is carried out fragmentation by spiral smashing conveyor, and deliver into standpipe;
4) paper pulp of standpipe 4 is transported to separator tube 7 through middle underflow pump grout outlet by middle underflow pump 5, in separator tube 7, the flow velocity of paper pulp declines, after the flow pulsation of paper pulp effectively weakens or eliminates, dense disc mill 8 in entering, through in the slurry that processes of dense disc mill 8 export from grout outlet;
Flow control system by separator tube leading portion 7 ?second gauge 21 on 1 detect the pulp flow Qin that middle underflow pump exports in real time, detect the pulp flow Qout by disc mill in real time by the 4th flowmeter 23 on grout outlet, detect by the 3rd flowmeter 22 on overflow pipe the pulp flow Qy overflowed from overflow pipe in real time; Then the aperture of middle underflow pump pulp control valve 14 and flow spill valve 15 is controlled by flow control system (second gauge 21 and the 3rd flowmeter 22), make the pulp flow Q0 large 10 ~ 15% that the pulp flow Qin that in fill process, middle underflow pump exports sets than disc mill, thus make in overflow pipe, have paper pulp to overflow all the time.
Flow control system according in the operating power W of dense the disc mill 8 and pulp flow Qout by disc mill that detects in real time, calculate real-time refining strength R=W/Qout, ratio R/the R0 controlling the refining strength of real-time refining strength and setting is 95 ~ 105%, be specially: as the ratio R/R0<95% of the refining strength of real-time refining strength and setting, the aperture of flow spill valve is strengthened by flow control system, increase the pulp flow Qy by overflow pipe, thus be reduced by the pulp flow Qout of disc mill; As the ratio R/R0>105% of the refining strength of real-time refining strength and setting, reduced the aperture of flow spill valve by flow control system, be reduced by the pulp flow Qy of overflow pipe, thus increase the pulp flow Qout by disc mill.
Embodiment 3
The method of the medium consistency refining of the middle underflow pump charging of this employing Fig. 2 device, comprises following technical process:
1) the refining strength value R0=45kWh/t in setting required for dense Disc Refiner Beating Process starches, again according in the rated power W0=132kW of dense disc mill, calculate, setting one based on the paper pulp stream value Q0=2.93t of dense disc mill in the passing through of rated power W0 starch/hour, make R0=W0/Q0;
2) dense double wire decker 2 during the pulp being 4 ~ 5% by mass concentration by pulp-inlet pipe 1 is delivered to, carries out dehydration to slurry and is concentrated into setting value mass concentration 9%; By regulating the plain boiled water control valve 16 on white water piping to add plain boiled water to pulp-inlet pipe 1, the pulp density of dense double wire decker in entering is made to reach setting value mass concentration 4%; In this process, the first densimeter detects the concentration of paper pulp in pulp-inlet pipe in real time, and controls the aperture of plain boiled water control valve 16;
Detect the pulp density of middle underflow pump output particular by the second densimeter 20 in real time, then adjust the setting value of the pulp density of dense double wire decker 2 in entering; And controlled the aperture of plain boiled water control valve 16 by the first densimeter 17, thus regulate the concentration of paper pulp on pulp-inlet pipe 1; Detected the liquid level of paper pulp in standpipe by the liquid level gauge 19 on standpipe 4 in real time, then regulate the flow of paper pulp in pulp-inlet pipe 1;
When the pulp density that the first densimeter 17 on pulp-inlet pipe detects in real time be less than 3.7% or be greater than 4.3% time, plain boiled water control valve on white water piping needs adjustment, be specially: when the pulp quality concentration that the first densimeter 17 on pulp-inlet pipe 1 detects in real time lower than 3.7% time, need the aperture of the plain boiled water control valve reduced on white water piping; When the pulp density that the first densimeter 17 on pulp-inlet pipe 1 detects in real time higher than 4.3% time, need the aperture of the plain boiled water control valve strengthened on white water piping;
When the pulp density value that middle underflow pump that the second densimeter on separator tube 7 detects in real time exports be less than 8% or be greater than 10% time, in entering, the concentration set point of the paper pulp of dense double wire decker 2 needs to adjust, be specially: when the pulp density value that the middle underflow pump that the second densimeter 20 on separator tube 7 detects in real time exports is less than 8%, need to improve the concentration set point of the paper pulp of dense double wire decker in entering; When the pulp density value that the middle underflow pump that the second densimeter 20 on separator tube 7 detects in real time exports is greater than 10%, need to reduce the concentration set point of the paper pulp of dense double wire decker 2 in entering;
3) slurry concentrated through dehydration is carried out fragmentation by spiral smashing conveyor, and deliver into standpipe;
4) paper pulp of standpipe 4 is transported to separator tube 7 through middle underflow pump grout outlet by middle underflow pump 5, in separator tube 7, the flow velocity of paper pulp declines, after the flow pulsation of paper pulp effectively weakens or eliminates, dense disc mill 8 in entering, through in the slurry that processes of dense disc mill 8 export from grout outlet;
Flow control system by separator tube leading portion 7 ?second gauge 21 on 1 detect the pulp flow Qin that middle underflow pump exports in real time, detect the pulp flow Qout by disc mill in real time by the 4th flowmeter 23 on grout outlet, detect by the 3rd flowmeter 22 on overflow pipe the pulp flow Qy overflowed from overflow pipe in real time; Then the aperture of middle underflow pump pulp control valve 14 and flow spill valve 15 is controlled by flow control system (second gauge 21 and the 3rd flowmeter 22), make the pulp flow Q0 large 10 ~ 15% that the pulp flow Qin that in fill process, middle underflow pump exports sets than disc mill, thus make in overflow pipe, have paper pulp to overflow all the time.
Flow control system according in the operating power W of dense the disc mill 8 and pulp flow Qout by disc mill that detects in real time, calculate real-time refining strength R=W/Qout, ratio R/the R0 controlling the refining strength of real-time refining strength and setting is 95 ~ 105%, be specially: as the ratio R/R0<95% of the refining strength of real-time refining strength and setting, the aperture of flow spill valve is strengthened by flow control system, increase the pulp flow Qy by overflow pipe, thus be reduced by the pulp flow Qout of disc mill; As the ratio R/R0>105% of the refining strength of real-time refining strength and setting, reduced the aperture of flow spill valve by flow control system, be reduced by the pulp flow Qy of overflow pipe, thus increase the pulp flow Qout by disc mill.
Claims (6)
1. adopt the medium consistency refining device of middle underflow pump charging, comprise flow control system, in dense double wire decker, spiral smashing conveyor, standpipe, middle underflow pump, separator tube, in dense disc mill and white water pump; In described, the charging aperture of dense double wire decker is connected with pulp-inlet pipe, and discharging opening is connected with the charging aperture of spiral smashing conveyor; The discharging opening of described spiral smashing conveyor is connected with the charging aperture of standpipe, and the discharging opening of described standpipe is connected with the charging aperture of middle underflow pump; The feed end of separator tube is connected with the discharging opening of middle underflow pump by middle underflow pump grout outlet, the discharge end of separator tube with in the charging aperture of dense disc mill be connected; It is characterized in that, overflow pipe is connected with the overfall on separator tube; Overfall on described separator tube be arranged on separator tube leading portion front 1/3 ?2/3 tube wall on; In described, the discharging opening of dense disc mill is connected with grout outlet; Described medium consistency refining device also comprises water sealed tank, the water inlet of described water sealed tank by pipeline with in the back flow water pump of dense double wire decker export and be connected; The water inlet of described white water pump is connected with the delivery port of water sealed tank by pipeline, and the delivery port of white water pump is connected with pulp-inlet pipe by white water pipe;
Described separator tube is ladder pipe, the internal diameter of the separator tube leading portion be connected with middle underflow pump grout outlet is 1.5 ~ 2 times of middle underflow pump grout outlet internal diameter, with in the internal diameter of separator tube back segment that is connected of dense disc mill charging aperture be 3 ~ 5 times of middle underflow pump grout outlet internal diameter, described separator tube back segment directly with in the charging aperture of dense disc mill be connected;
Described flow control system comprises flowmeter, densimeter, liquid level gauge, enters to starch control valve, pulp control valve, overflow control valve, plain boiled water control valve and Programmable Logic Controller; Flowmeter, densimeter are connected with Programmable Logic Controller respectively with liquid level gauge; Flowmeter comprises first-class gauge, second gauge, the 3rd flowmeter and the 4th flowmeter; Densimeter comprises the first densimeter and the second densimeter; Described pulp-inlet pipe is arranged for regulate pulp flow enter to starch control valve, described middle underflow pump grout outlet being arranged for regulating middle underflow pump to export the flow control valve of paper pulp, described overflow pipe being arranged the overflow control valve for regulating paper pulp spillway discharge; Described white water pipe is arranged the plain boiled water control valve for regulating plain boiled water flow; Pulp-inlet pipe is provided with the first densimeter and first-class gauge, standpipe is provided with liquid level gauge, separator tube leading portion is provided with the second densimeter and second gauge, overflow pipe is provided with the 3rd flowmeter, grout outlet is provided with the 4th flowmeter.
2. the medium consistency refining device of the employing middle underflow pump charging according to claim 1, is characterized in that, the second described densimeter is connected with the first densimeter, and the first densimeter is connected with plain boiled water control valve; Liquid level gauge is connected with first-class gauge, first-class gauge with enter to starch control valve and be connected; 4th flowmeter is connected with second gauge, and second gauge is connected with middle underflow pump pulp control valve; Second gauge is also connected with the 3rd flowmeter, and the 3rd flowmeter is connected with overflow control valve.
3. the medium consistency refining device of the employing middle underflow pump charging according to claim 1, is characterized in that, described to enter to starch control valve, middle underflow pump pulp control valve, overflow control valve and plain boiled water control valve be manual modulation valve or automatic regulating valve; Described when to enter to starch control valve, middle underflow pump pulp control valve, overflow control valve and plain boiled water control valve be automatic regulating valve, enter to starch control valve, middle underflow pump pulp control valve, overflow control valve be connected with Programmable Logic Controller respectively with plain boiled water control valve.
4. the medium consistency refining device of the employing middle underflow pump charging according to claim 1, is characterized in that, in described, dense disc mill, middle underflow pump and water sealed tank are all arranged in same plane; Or middle underflow pump and water sealed tank are all arranged in same plane, in dense disc mill be arranged in another higher plane.
5. the medium consistency refining device of the employing middle underflow pump charging according to claim 1, is characterized in that, the axial length of described separator tube is not less than 3 meters, and wherein after separator tube leading portion and separator tube, Length Ratio is 0.5:1 ?2:1.
6. adopt a medium consistency refining method for middle underflow pump charging, it is characterized in that comprising following technique:
1) refining strength value R0 required for dense Disc Refiner Beating Process in setting, then according in the rated power W0 of dense disc mill, determine, based on the paper pulp stream value Q0 of dense disc mill in the passing through of rated power W0, to make R0=W0/Q0;
2) dense double wire decker in being delivered to by pulp by pulp-inlet pipe, is carried out dehydration to slurry and is concentrated into setting value; By regulating the plain boiled water control valve on white water piping to add plain boiled water to pulp-inlet pipe, the pulp density of dense double wire decker in entering is made to reach setting value; The concentration of paper pulp in real-time detection pulp-inlet pipe, and control the aperture of plain boiled water control valve; When the pulp density that the middle underflow pump that densimeter detects in real time exports departs from range of set value, in entering, the setting value of the pulp density of dense double wire decker needs to adjust, be specially: when the pulp density that the middle underflow pump that densimeter detects in real time exports is higher than range of set value, reduce the setting value of the pulp density of dense double wire decker in entering; When the pulp density that the middle underflow pump that densimeter detects in real time exports is lower than range of set value, improve the setting value of the pulp density of dense double wire decker in entering;
3) slurry concentrated through dehydration is carried out fragmentation by spiral smashing conveyor, and deliver into standpipe;
4) paper pulp of standpipe is transported to separator tube through middle underflow pump grout outlet by middle underflow pump, flow control system detects the pulp flow Qin of middle underflow pump output in real time by the second gauge on separator tube leading portion, detect the pulp flow Qout by disc mill in real time by the 4th flowmeter on grout outlet, detect by the 3rd flowmeter on overflow pipe the pulp flow Qy overflowed from overflow pipe in real time; Then the aperture of middle underflow pump pulp control valve and flow spill valve is controlled by flow control system, pulp flow Q0 large 10% that the pulp flow Qin that in fill process, middle underflow pump exports is set than disc mill or more, thus make in overflow pipe, have paper pulp to overflow all the time; Flow control system according in the operating power W of dense disc mill and the pulp flow Qout by disc mill that detects in real time, calculate real-time refining strength R=W/Qout, ratio R/the R0 controlling the refining strength of real-time refining strength and setting is 95 ~ 105%, as the ratio R/R0<95% of the refining strength of real-time refining strength and setting, the aperture of flow spill valve is strengthened by flow control system, increase the pulp flow Qy by overflow pipe, be reduced by the pulp flow Qout of disc mill; As the ratio R/R0>105% of the refining strength of real-time refining strength and setting, reduced the aperture of flow spill valve by flow control system, be reduced by the pulp flow Qy of overflow pipe, increase the pulp flow Qout by disc mill; By above adjustment, the ratio R/R0 finally making the refining strength of real-time refining strength and setting is 95 ~ 105%, reaches the object of stable refining strength; In separator tube, the flow velocity of paper pulp declines, and after the flow pulsation of paper pulp effectively weakens or eliminates, dense disc mill in entering, in warp, the slurry of dense disc mill process exports from grout outlet.
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| CN106283807A (en) * | 2016-11-02 | 2017-01-04 | 芬欧汇川(中国)有限公司 | Mechanical pulp defibrination production line |
| CN106368037A (en) * | 2016-11-28 | 2017-02-01 | 芬欧汇川(中国)有限公司 | Pulping machine and long fiber beating degree control method and system thereof |
| CN109675678B (en) * | 2019-03-04 | 2024-03-22 | 思念食品(河南)有限公司 | Cereal pulp density on-line control pulping system and cereal pulping method |
| CN110575676A (en) * | 2019-09-25 | 2019-12-17 | 泉州洛江吉如机械设计有限公司 | sanitary towel production is with concentrated light-operated wall from mechanical equipment |
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| DE2916379A1 (en) * | 1979-04-23 | 1980-11-13 | Schultz & Nauth Collodin Kleb | INVERTED PAPER GLUE AND METHOD FOR THE PRODUCTION THEREOF |
| CN1456746A (en) * | 2003-05-28 | 2003-11-19 | 华南理工大学 | Disc refiner non-powered feeding and moderate concentration pulping method and device |
| CN2657770Y (en) * | 2003-05-28 | 2004-11-24 | 华南理工大学 | Moderately density beating device of powerless supply beating of disc mill |
| CN101476258A (en) * | 2009-01-16 | 2009-07-08 | 华南理工大学 | Constant-quantity constant-pressure pulping method and apparatus for disk milling machine |
| CN101705633A (en) * | 2009-10-30 | 2010-05-12 | 华南理工大学 | Device for controlling pulping process and control method thereof |
| CN201843017U (en) * | 2010-10-26 | 2011-05-25 | 华南理工大学 | Middle-concentration pulping and pumping device |
| CN101974860B (en) * | 2010-10-26 | 2012-05-30 | 华南理工大学 | Method for medium-consistency refining and pumping |
| CN201850463U (en) * | 2010-10-26 | 2011-06-01 | 华南理工大学 | Variable-consistency pulp beating device |
| CN203715985U (en) * | 2014-01-24 | 2014-07-16 | 华南理工大学 | Medium-underflow pulping device adopting medium-underflow pump to charge |
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