CN203715985U - Medium-underflow pulping device adopting medium-underflow pump to charge - Google Patents
Medium-underflow pulping device adopting medium-underflow pump to charge Download PDFInfo
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- CN203715985U CN203715985U CN201420047355.1U CN201420047355U CN203715985U CN 203715985 U CN203715985 U CN 203715985U CN 201420047355 U CN201420047355 U CN 201420047355U CN 203715985 U CN203715985 U CN 203715985U
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Abstract
The utility model discloses a medium-underflow pulping device adopting a medium-underflow pump to charge. A charging port of a medium-underflow dual-net dehydrator of the device is connected with a pulp inlet pipe; a discharging port of the medium-underflow dual-net dehydrator of the device is connected with the charging port of a crushing spiral conveyor; the discharging port of the crushing spiral conveyor is connected with the charging port of an upright pipe of which the discharging port is connected with the charging port of the medium-underflow pump; the charging end of a buffer pipe is connected with the discharging port of the medium-underflow pump by a pulp outlet pipe of the medium-underflow pump; the discharging end of the buffer pipe is connected with the charging port of a medium-underflow disc mill; an overflow pipe is connected with an overflow port of the buffer pipe; the discharging port of the medium-underflow disc mill is connected with the pulp outlet pipe; the water inlet of a water seal slot is connected with a whitewater slot outlet of the medium-underflow dual-net dehydrator by a pipeline. By adjusting and controlling the flow and concentration of low-concentration paper pulp in a pulp inlet pipeline, stable liquid level and stable concentration of paper pulp in the upright pipe in the front of the medium-underflow pump are ensured and the medium-underflow disc mill is effectively enabled to obtain stable and pulping quality and effect.
Description
Technical field
The utility model relates to a kind of making beating technology of pulping and paper-making, particularly relates to a kind of medium consistency refining device that adopts middle underflow pump charging.
Background technology
In dense disc mill obtained in recent years more widely application in China paper mill, and in keeping entering, concentration and the stable of flow of the paper pulp of dense disc mill have important impact for obtaining good beating results.When in certain density paper pulp enters, dense disc mill 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 permission of a setting, or in the power of dense disc mill motor and the ratio of pulp flow maintain in the excursion of permission of a setting, in can ensureing, dense disc mill is pulled an oar under stable making beating intensity, and obtains stable beating results.In dense disc mill under 6～12% pulp density, pull an oar, the poor fluidity of paper pulp, must adopt middle underflow pump to carry, and be equipped with the auxiliary equipment such as vavuum pump and turbulator.But, in actual production, find, adopting the slurry of middle underflow pump output is a kind of Pulsating Flow, pressure and the flowed fluctuation of paper pulp are larger, and the normal work of disc mill has been caused to bad impact.On the other hand, in the time that the working condition in production is unstable, the concentration of paper pulp also produces fluctuation to a certain degree.When by pressure, flow and the concentration of paper pulp in dense disc mill mill district while there is larger fluctuation, in dense disc mill cannot under stable making beating intensity, pull an oar, refining process is difficult to control, thereby causes the unstable 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 concentrated slurry of dehydration, make its concentration 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, inevitably cause middle underflow pump output in dense slurry concentration unstable, and affected the effect of making beating.Although the method that Chinese invention patent application 201010522397.2 provides in having regulated to a certain extent dense pump and in pulp pressure between dense disc mill and the pulsation of pulp flow; But paper pulp is incompressible fluid, and the capacity of buffer is limited, and middle underflow pump and in overflow mechanism is not set on pipeline between dense disc mill, therefore still there is fluctuation to a certain degree through pulp flow and the pressure of buffer; And buffer and in the slurry control valve installed on pipeline between dense disc mill and pipeline expanded enter in the pressure of paper pulp and the degree of flowed fluctuation before dense disc mill, affected the stability of beating results; In addition, middle underflow pump and in overflow mechanism is not set on pipeline between dense disc mill, the pulp flow that enters disc mill can only be realized by the aperture of controlling the valve on middle underflow pump pulp pipeline, therefore, must frequently regulate valve on middle underflow pump pulp pipeline with the requirement of dense disc mill to pulp flow in meeting, and this expand the pulsation of pulp flow and pressure.
Utility model content
The purpose of this utility model is to overcome the shortcoming of prior art, and a kind of medium consistency refining device of the employing middle underflow pump charging that obtains stable refining pulp quality and effect is provided.
The purpose of this utility model 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 ?on 2/3 tube wall; 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 outlet of dense double wire decker 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 being 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 the 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 that 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 and liquid level gauge are connected with Programmable Logic Controller respectively; Flowmeter comprises first flow meter, the second flowmeter, the 3rd flowmeter and the 4th flowmeter; Densimeter comprises the first densimeter and the second densimeter; What on described pulp-inlet pipe, be provided for regulating pulp flow enters to starch control valve, is provided for regulating the flow control valve of middle underflow pump output paper pulp on described middle underflow pump grout outlet, is provided for regulating the overflow control valve of paper pulp spillway discharge on described overflow pipe; In described white water pipe, be provided for regulating the plain boiled water control valve of plain boiled water flow; On pulp-inlet pipe, be provided with the first densimeter and first flow meter, on standpipe, be provided with liquid level gauge, on separator tube leading portion, be provided with the second densimeter and the second flowmeter, on overflow pipe, be provided with the 3rd flowmeter, on grout outlet, be provided with the 4th flowmeter.
For further realizing the utility model object, 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 flow meter, first flow meter with enter to starch control valve and be connected; The 4th flowmeter is connected with the second flowmeter, and the second flowmeter is connected with middle underflow pump pulp control valve; The second flowmeter 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 entering to starch control valve, middle underflow pump pulp control valve, overflow control valve and plain boiled water control valve and being automatic regulating valve, enter to starch control valve, middle underflow pump pulp control valve, overflow control valve and 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.
Compared with prior art, the utlity model has following advantage:
1, the utility model is by regulating, control flow and the concentration of the low-consistency stock in pulp-inlet pipe road, ensure that well the paper pulp in the standpipe before middle underflow pump has stable liquid level and stable concentration, ensure that middle underflow pump has stable pumpability, in effectively ensureing, dense disc mill obtains stable refining pulp quality and effect.
2, the utility model take middle underflow pump and in overflow pipe and flow spill valve are set in connecting pipe between dense disc mill, detect in real time, control the pulp flow in dense disc mill mill district in passing through and by the spillway discharge of overflow pipe by flow control system, the power of dense disc mill and the ratio of the pulp flow by mill district are maintained in the excursion of permission of a setting, guarantee disc mill is pulled an oar under stable making beating intensity, thereby has obtained stable refining pulp quality and effect.
3, the utility model by middle underflow pump and in arrange in connecting pipe between dense disc mill with in the staged separator tube that is directly connected of dense disc mill charging aperture, and overfall is set on separator tube, pressure and the flow pulsation of paper pulp is obtained gradually, cushion fully, discharge and greatly reduce, ensure the pressure of the paper pulp of dense disc mill in entering and stablizing of flow;
4, the utility model is by stablizing middle underflow pump output pulp flow and controlling water kick amount, ensure that disc mill obtains stable beating results, greatly reduce the frequency that regulates middle underflow pump outlet valve, middle underflow pump has been moved under stable flow, and reduced the pulsation of pulp flow and pressure.
Brief description of the drawings
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 utility model is described in further detail, but the claimed scope of the utility model is not limited to the scope that embodiment explains.
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 overfall 7 on separator tube 7 ?3 be connected, overfall on described separator tube 77 ?3 be arranged on separator tube leading portion 7 ?1 front 1/3 ?on 2/3 tube wall; 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 outlet of dense double wire decker 2 be connected; The water inlet of described white water pump 12 is connected with the delivery port of water sealed tank 11 by pipeline, 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 being connected with middle underflow pump grout outlet 6 ?1 internal diameter be 1.5～2 times of middle underflow pump grout outlet 6 internal diameters, with in the separator tube back segment 7 that is connected of dense disc mill 8 charging apertures ?2 internal diameter be 3～5 times of middle underflow pump grout outlet 6 internal diameters, 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 that 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 and liquid level gauge are connected with Programmable Logic Controller respectively; Flowmeter comprises first flow meter 18, the second flowmeter 21, the 3rd flowmeter 22 and the 4th flowmeter 23; Densimeter comprises the first densimeter 17 and the second densimeter 20; On pulp-inlet pipe 1, be provided with can be used for regulating pulp flow enter to starch control valve 13, on middle underflow pump grout outlet 6, be provided with the pulp control valve 14 that can be used for regulating middle underflow pump output pulp flow, on overflow pipe 10, be provided with the overflow control valve 15 that can be used for regulating paper pulp spillway discharge; In described white water pipe 26, be provided with the plain boiled water control valve 16 that can be used for regulating plain boiled water flow; On pulp-inlet pipe 1, be provided with the first densimeter 17 and first flow meter 18, on standpipe 4, be provided with liquid level gauge 19, on separator tube leading portion 7 ?1, be provided with the second densimeter 20 and the second flowmeter 21, on overflow pipe 10, be provided with the 3rd flowmeter 22, on grout outlet 9, be provided with the 4th flowmeter 23; The 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 is controlled the aperture of plain boiled water control valve 16; Liquid level gauge 19 is connected with first flow meter 18, first flow meter 18 with enter to starch control valve 13 and be connected, first flow meter 18 is controlled into the aperture of slurry control valve 13; The 4th flowmeter 23 is connected with the second flowmeter 21, and the second flowmeter 21 is connected with pulp control valve 14, and the second flowmeter 21 is controlled the aperture of pulp control valve 14; The second flowmeter 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 valves 15.
On middle underflow pump grout outlet 6 and separator tube back segment 7 ?2, be respectively arranged with the first Pressure gauge 24 and the second Pressure gauge 25;
Entering to starch control valve 13, pulp control valve 14, overflow control valve 15 and plain boiled water control valve 16 is manual modulation valve or automatic regulating valve; While 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 is by the value of the real-time detectable concentration meter of Programmable Logic Controller and flowmeter, with mode control, the aperture that regulates each valve, the action of PID adjusting.
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 needed making beating intensity level of dense Disc Refiner Beating Process R0=110kWh/t slurry in setting, the rated power W0=315kW of dense disc mill in foundation again, calculate, set a paper pulp stream value Q0=2.86t slurry based on dense disc mill in the passing through of rated power W0/hour, make R0=W0/Q0;
2) dense double wire decker 2 during the slurry that is 4～5% by pulp-inlet pipe 1 by mass concentration is delivered to, dewaters and is concentrated into setting value mass concentration 12% slurry; By regulating the plain boiled water control valve 16 on white water piping to add plain boiled water to pulp-inlet pipe 1, make the pulp density of dense double wire decker in entering 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;
Specifically detect in real time the pulp density of middle underflow pump output by the second densimeter 20, then adjust the setting value of the pulp density of dense double wire decker 2 in entering; And control the aperture of plain boiled water control valve 16 by the first densimeter 17, thereby regulate the concentration of paper pulp on pulp-inlet pipe 1; Detect in real time the liquid level of paper pulp in standpipe by the liquid level gauge 19 on standpipe 4, then regulate the flow of paper pulp in pulp-inlet pipe 1;
The pulp density detecting in real time when the first densimeter 17 on pulp-inlet pipe is less than 3.7% or while being greater than 4.3%, plain boiled water control valve on white water piping needs to adjust, be specially: the pulp quality concentration detecting in real time when the first densimeter 17 on pulp-inlet pipe 1 lower than 3.7% time, need to reduce the aperture of the plain boiled water control valve on white water piping; The pulp density detecting in real time when the first densimeter 17 on pulp-inlet pipe 1 higher than 4.3% time, need to strengthen the aperture of the plain boiled water control valve on white water piping;
The pulp density value of the middle underflow pump output detecting in real time when the second densimeter on separator tube 7 is less than 11% or while being greater than 13%, in entering, the concentration set point of the paper pulp of dense double wire decker 2 need to be adjusted, be specially: when the pulp density value of the middle underflow pump output detecting in real time when the second densimeter 20 on separator tube 7 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 of the middle underflow pump output detecting in real time when the second densimeter 20 on separator tube 7 is greater than 13%, need to reduce the concentration set point of the paper pulp of dense double wire decker 2 in entering;
3) will carry out fragmentation by spiral smashing conveyor through the concentrated slurry of dehydration, and deliver into standpipe;
4) middle underflow pump 5 is transported to separator tube 7 by the paper pulp of standpipe 4 through middle underflow pump grout outlet, 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 processed of dense disc mill 8 export from grout outlet;
Flow control system detects the pulp flow Qin of middle underflow pump output in real time by the second flowmeter 21 on separator tube leading portion 7 ?1, detect in real time by the pulp flow Qout of disc mill by the 4th flowmeter 23 on grout outlet, detect in real time by the 3rd flowmeter 22 on overflow pipe the pulp flow Qy overflowing from overflow pipe; Then control the aperture of middle underflow pump pulp control valve 14 and flow spill valve 15 by flow control system (the second flowmeter 21 and the 3rd flowmeter 22), pulp flow Q0 that the pulp flow Qin of the output of middle underflow pump in fill process is set than disc mill is large 10～15%, thereby makes have all the time paper pulp to overflow in overflow pipe.
The operating power W of dense disc mill 8 and the real-time pulp flow Qout that passes through disc mill detecting in flow control system basis, calculate making beating intensity R=W/Qout in real time, ratio R/the R0 that controls the making beating intensity of pull an oar in real time intensity and setting is 95～105%, in the time of the ratio R/R0<95% of the making beating intensity of real-time making beating intensity and setting, strengthen the aperture of flow spill valve by flow control system, increase by the pulp flow Qy of overflow pipe, thereby reduce by the pulp flow Qout of disc mill; In the time of the ratio R/R0>105% of the making beating intensity of real-time making beating intensity and setting, reduce the aperture of flow spill valve by flow control system, reduce by the pulp flow Qy of overflow pipe, thereby increase by the pulp flow Qout of disc mill; By above adjusting, the ratio R/R0 of the making beating intensity of finally make to pull an oar in real time intensity and setting is 95～105%, reaches the object of stable making beating intensity.
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 is all arranged in same plane with water sealed tank 11, 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 needed making beating intensity level of dense Disc Refiner Beating Process R0=70kWh/t slurry in setting, the rated power W0=315kW of dense disc mill in foundation again, calculate, set a paper pulp stream value Q0=4.5t slurry based on dense disc mill in the passing through of rated power W0/hour, make R0=W0/Q0;
2) dense double wire decker 2 during the pulp that is 4～5% by pulp-inlet pipe 1 by mass concentration is delivered to, dewaters and is concentrated into setting value mass concentration 10% slurry; By regulating the plain boiled water control valve 16 on white water piping to add plain boiled water to pulp-inlet pipe 1, make the pulp density of dense double wire decker in entering 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;
Specifically detect in real time the pulp density of middle underflow pump output by the second densimeter 20, then adjust the setting value of the pulp density of dense double wire decker 2 in entering; And control the aperture of plain boiled water control valve 16 by the first densimeter 17, thereby regulate the concentration of paper pulp on pulp-inlet pipe 1; Detect in real time the liquid level of paper pulp in standpipe by the liquid level gauge 19 on standpipe 4, then regulate the flow of paper pulp in pulp-inlet pipe 1;
The pulp density detecting in real time when the first densimeter 17 on pulp-inlet pipe is less than 3.7% or while being greater than 4.3%, plain boiled water control valve on white water piping needs to adjust, be specially: the pulp quality concentration detecting in real time when the first densimeter 17 on pulp-inlet pipe 1 lower than 3.7% time, need to reduce the aperture of the plain boiled water control valve on white water piping; The pulp density detecting in real time when the first densimeter 17 on pulp-inlet pipe 1 higher than 4.3% time, need to strengthen the aperture of the plain boiled water control valve on white water piping;
The pulp density value of the middle underflow pump output detecting in real time when the second densimeter on separator tube 7 is less than 9% or while being greater than 11%, in entering, the concentration set point of the paper pulp of dense double wire decker 2 need to be adjusted, be specially: when the pulp density value of the middle underflow pump output detecting in real time when the second densimeter 20 on separator tube 7 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 of the middle underflow pump output detecting in real time when the second densimeter 20 on separator tube 7 is greater than 11%, need to reduce the concentration set point of the paper pulp of dense double wire decker 2 in entering;
3) will carry out fragmentation by spiral smashing conveyor through the concentrated slurry of dehydration, and deliver into standpipe;
4) middle underflow pump 5 is transported to separator tube 7 by the paper pulp of standpipe 4 through middle underflow pump grout outlet, 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 processed of dense disc mill 8 export from grout outlet;
Flow control system detects the pulp flow Qin of middle underflow pump output in real time by the second flowmeter 21 on separator tube leading portion 7 ?1, detect in real time by the pulp flow Qout of disc mill by the 4th flowmeter 23 on grout outlet, detect in real time by the 3rd flowmeter 22 on overflow pipe the pulp flow Qy overflowing from overflow pipe; Then control the aperture of middle underflow pump pulp control valve 14 and flow spill valve 15 by flow control system (the second flowmeter 21 and the 3rd flowmeter 22), pulp flow Q0 that the pulp flow Qin of the output of middle underflow pump in fill process is set than disc mill is large 10～15%, thereby makes have all the time paper pulp to overflow in overflow pipe.
The operating power W of dense disc mill 8 and the real-time pulp flow Qout that passes through disc mill detecting in flow control system basis, calculate making beating intensity R=W/Qout in real time, ratio R/the R0 that controls the making beating intensity of pull an oar in real time intensity and setting is 95～105%, be specially: in the time of the ratio R/R0<95% of the making beating intensity of real-time making beating intensity and setting, strengthen the aperture of flow spill valve by flow control system, increase by the pulp flow Qy of overflow pipe, thereby reduce by the pulp flow Qout of disc mill; In the time of the ratio R/R0>105% of the making beating intensity of real-time making beating intensity and setting, reduce the aperture of flow spill valve by flow control system, reduce by the pulp flow Qy of overflow pipe, thereby increase by the pulp flow Qout of 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 needed making beating intensity level of dense Disc Refiner Beating Process R0=45kWh/t slurry in setting, the rated power W0=132kW of dense disc mill in foundation again, calculate, set a paper pulp stream value Q0=2.93t slurry based on dense disc mill in the passing through of rated power W0/hour, make R0=W0/Q0;
2) dense double wire decker 2 during the pulp that is 4～5% by pulp-inlet pipe 1 by mass concentration is delivered to, dewaters and is concentrated into setting value mass concentration 9% slurry; By regulating the plain boiled water control valve 16 on white water piping to add plain boiled water to pulp-inlet pipe 1, make the pulp density of dense double wire decker in entering 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;
Specifically detect in real time the pulp density of middle underflow pump output by the second densimeter 20, then adjust the setting value of the pulp density of dense double wire decker 2 in entering; And control the aperture of plain boiled water control valve 16 by the first densimeter 17, thereby regulate the concentration of paper pulp on pulp-inlet pipe 1; Detect in real time the liquid level of paper pulp in standpipe by the liquid level gauge 19 on standpipe 4, then regulate the flow of paper pulp in pulp-inlet pipe 1;
The pulp density detecting in real time when the first densimeter 17 on pulp-inlet pipe is less than 3.7% or while being greater than 4.3%, plain boiled water control valve on white water piping needs to adjust, be specially: the pulp quality concentration detecting in real time when the first densimeter 17 on pulp-inlet pipe 1 lower than 3.7% time, need to reduce the aperture of the plain boiled water control valve on white water piping; The pulp density detecting in real time when the first densimeter 17 on pulp-inlet pipe 1 higher than 4.3% time, need to strengthen the aperture of the plain boiled water control valve on white water piping;
The pulp density value of the middle underflow pump output detecting in real time when the second densimeter on separator tube 7 is less than 8% or while being greater than 10%, in entering, the concentration set point of the paper pulp of dense double wire decker 2 need to be adjusted, be specially: when the pulp density value of the middle underflow pump output detecting in real time when the second densimeter 20 on separator tube 7 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 of the middle underflow pump output detecting in real time when the second densimeter 20 on separator tube 7 is greater than 10%, need to reduce the concentration set point of the paper pulp of dense double wire decker 2 in entering;
3) will carry out fragmentation by spiral smashing conveyor through the concentrated slurry of dehydration, and deliver into standpipe;
4) middle underflow pump 5 is transported to separator tube 7 by the paper pulp of standpipe 4 through middle underflow pump grout outlet, 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 processed of dense disc mill 8 export from grout outlet;
Flow control system detects the pulp flow Qin of middle underflow pump output in real time by the second flowmeter 21 on separator tube leading portion 7 ?1, detect in real time by the pulp flow Qout of disc mill by the 4th flowmeter 23 on grout outlet, detect in real time by the 3rd flowmeter 22 on overflow pipe the pulp flow Qy overflowing from overflow pipe; Then control the aperture of middle underflow pump pulp control valve 14 and flow spill valve 15 by flow control system (the second flowmeter 21 and the 3rd flowmeter 22), pulp flow Q0 that the pulp flow Qin of the output of middle underflow pump in fill process is set than disc mill is large 10～15%, thereby makes have all the time paper pulp to overflow in overflow pipe.
The operating power W of dense disc mill 8 and the real-time pulp flow Qout that passes through disc mill detecting in flow control system basis, calculate making beating intensity R=W/Qout in real time, ratio R/the R0 that controls the making beating intensity of pull an oar in real time intensity and setting is 95～105%, be specially: in the time of the ratio R/R0<95% of the making beating intensity of real-time making beating intensity and setting, strengthen the aperture of flow spill valve by flow control system, increase by the pulp flow Qy of overflow pipe, thereby reduce by the pulp flow Qout of disc mill; In the time of the ratio R/R0>105% of the making beating intensity of real-time making beating intensity and setting, reduce the aperture of flow spill valve by flow control system, reduce by the pulp flow Qy of overflow pipe, thereby increase by the pulp flow Qout of disc mill.
Claims (5)
1. the medium consistency refining device that adopts middle underflow pump charging, is characterized in that, 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 ?on 2/3 tube wall; 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 outlet of dense double wire decker 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 being 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 the 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 that 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 and liquid level gauge are connected with Programmable Logic Controller respectively; Flowmeter comprises first flow meter, the second flowmeter, the 3rd flowmeter and the 4th flowmeter; Densimeter comprises the first densimeter and the second densimeter; What on described pulp-inlet pipe, be provided for regulating pulp flow enters to starch control valve, is provided for regulating the flow control valve of middle underflow pump output paper pulp on described middle underflow pump grout outlet, is provided for regulating the overflow control valve of paper pulp spillway discharge on described overflow pipe; In described white water pipe, be provided for regulating the plain boiled water control valve of plain boiled water flow; On pulp-inlet pipe, be provided with the first densimeter and first flow meter, on standpipe, be provided with liquid level gauge, on separator tube leading portion, be provided with the second densimeter and the second flowmeter, on overflow pipe, be provided with the 3rd flowmeter, on grout outlet, be provided with the 4th flowmeter.
2. the medium consistency refining device of employing middle underflow pump according to claim 1 charging, 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 flow meter, first flow meter with enter to starch control valve and be connected; The 4th flowmeter is connected with the second flowmeter, and the second flowmeter is connected with middle underflow pump pulp control valve; The second flowmeter is also connected with the 3rd flowmeter, and the 3rd flowmeter is connected with overflow control valve.
3. the medium consistency refining device of employing middle underflow pump according to claim 1 charging, 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 entering to starch control valve, middle underflow pump pulp control valve, overflow control valve and plain boiled water control valve and being automatic regulating valve, enter to starch control valve, middle underflow pump pulp control valve, overflow control valve and be connected with Programmable Logic Controller respectively with plain boiled water control valve.
4. the medium consistency refining device of employing middle underflow pump according to claim 1 charging, is characterized in that, described in dense disc mill, middle underflow pump and water sealed tank be 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 employing middle underflow pump according to claim 1 charging, 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.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420047355.1U CN203715985U (en) | 2014-01-24 | 2014-01-24 | Medium-underflow pulping device adopting medium-underflow pump to charge |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201420047355.1U CN203715985U (en) | 2014-01-24 | 2014-01-24 | Medium-underflow pulping device adopting medium-underflow pump to charge |
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| CN203715985U true CN203715985U (en) | 2014-07-16 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103790059A (en) * | 2014-01-24 | 2014-05-14 | 华南理工大学 | Device and method for medium-concentration beating fed through medium-concentration pulp pump |
| CN106283807A (en) * | 2016-11-02 | 2017-01-04 | 芬欧汇川(中国)有限公司 | Mechanical pulp defibrination production line |
| CN106676932A (en) * | 2017-03-07 | 2017-05-17 | 黄可柽 | High-concentration metering grinder |
-
2014
- 2014-01-24 CN CN201420047355.1U patent/CN203715985U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103790059A (en) * | 2014-01-24 | 2014-05-14 | 华南理工大学 | Device and method for medium-concentration beating fed through medium-concentration pulp pump |
| CN106283807A (en) * | 2016-11-02 | 2017-01-04 | 芬欧汇川(中国)有限公司 | Mechanical pulp defibrination production line |
| CN106676932A (en) * | 2017-03-07 | 2017-05-17 | 黄可柽 | High-concentration metering grinder |
| CN106676932B (en) * | 2017-03-07 | 2019-01-25 | 黄可柽 | Highly concentrated metering fiberizer |
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