CN117819216A - Ash supply system for full-automatic well cementation operation and control method thereof - Google Patents

Ash supply system for full-automatic well cementation operation and control method thereof Download PDF

Info

Publication number
CN117819216A
CN117819216A CN202410253554.6A CN202410253554A CN117819216A CN 117819216 A CN117819216 A CN 117819216A CN 202410253554 A CN202410253554 A CN 202410253554A CN 117819216 A CN117819216 A CN 117819216A
Authority
CN
China
Prior art keywords
pressure
ash
constant
control valve
tank
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
CN202410253554.6A
Other languages
Chinese (zh)
Other versions
CN117819216B (en
Inventor
侯林
史元
蒋荣星
耿艳峰
陈�峰
邵振友
季威
张梦非
刘添翼
康诗雨
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
China Oilfield Services Ltd
Original Assignee
China Oilfield Services Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by China Oilfield Services Ltd filed Critical China Oilfield Services Ltd
Priority to CN202410253554.6A priority Critical patent/CN117819216B/en
Publication of CN117819216A publication Critical patent/CN117819216A/en
Application granted granted Critical
Publication of CN117819216B publication Critical patent/CN117819216B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • E—FIXED CONSTRUCTIONS
    • E21—EARTH OR ROCK DRILLING; MINING
    • E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
    • E21B33/00—Sealing or packing boreholes or wells
    • E21B33/10—Sealing or packing boreholes or wells in the borehole
    • E21B33/13—Methods or devices for cementing, for plugging holes, crevices or the like
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
    • B65G—TRANSPORT OR STORAGE DEVICES, e.g. CONVEYORS FOR LOADING OR TIPPING, SHOP CONVEYOR SYSTEMS OR PNEUMATIC TUBE CONVEYORS
    • B65G53/00—Conveying materials in bulk through troughs, pipes or tubes by floating the materials or by flow of gas, liquid or foam
    • B65G53/34—Details
    • B65G53/66—Use of indicator or control devices, e.g. for controlling gas pressure, for controlling proportions of material and gas, for indicating or preventing jamming of material

Landscapes

  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Geology (AREA)
  • Mining & Mineral Resources (AREA)
  • Mechanical Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Environmental & Geological Engineering (AREA)
  • Fluid Mechanics (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Control Of Fluid Pressure (AREA)

Abstract

The invention discloses an ash supply system for full-automatic well cementation operation and a control method thereof, which solve the technical problems of strong dependence on artificial experience, poor operation consistency, low slurry density control precision caused by insufficient ash supply stability and the like in well cementation ash supply operation. The device comprises an ash storage tank, a constant pressure tank, an air source, an ash supply and air inlet pipeline, a monitoring system, a control valve group, a man-machine interaction interface, a data acquisition system and an automatic control system. According to the invention, the valve position signals of the reserve, pressure and control valve groups of the ash supply system are acquired in real time through the data acquisition system, and the control instructions from the man-machine interaction interface are received, and after calculation through the automatic control system, the control signals of the opening degrees of the control valves on the ash supply and air blowing pipelines are obtained, so that stable control of the ash supply amount and the air inflow is realized, the ash supply amount is ensured to be matched with the ash demand of the subsequent well cementation slurry mixing equipment, the labor intensity of operators is reduced, and errors caused by human factors are avoided.

Description

Ash supply system for full-automatic well cementation operation and control method thereof
Technical Field
The invention belongs to the technical field of well cementation and ash supply, and particularly relates to an ash supply system for full-automatic well cementation operation and a control method thereof.
Background
The cementing operation is a key link in the well drilling and completion engineering, and the operation process of injecting cement slurry with certain density and volume into the bottom of the well under a specific high-pressure condition is needed, so that the aims of protecting the casing, sealing the stratum, establishing an oil gas outflow channel and the like are achieved. Cement slurry density is an important monitoring parameter for well cementation operation, uniform and stable slurry mixing and up to standard density are key preconditions for realizing high-quality well cementation.
Currently, cement slurry density is controlled during cementing operations primarily by adjusting the flow of dry cement into the mixing equipment. However, most of the existing ash supply systems adopt pneumatic conveying mode, the fluid in the ash supply and air inlet pipelines is complex gas-solid (air-dry cement ash) two-phase flow, the dry cement ash flow is comprehensively influenced by a plurality of factors such as operating pressure, conveying gas speed, cement powder property, ash conveying pipeline size and layout, and no reliable metering means for detecting the flow on line in real time exists at present. Therefore, in the operation process, the problem that the cement paste density is difficult to accurately control due to insufficient ash supply and instability often occurs.
In addition, at present, operations such as inflation pressure holding, ash discharging, pipeline blowing and the like of an ash storage tank are also commonly controlled manually, an operator is required to watch the tank pressure on duty and adjust the ash discharging and blowing valve positions in the operation process, the problems of high labor cost, strong experience dependence, poor operation consistency and the like exist, and the improvement of the well cementation operation efficiency and quality is severely limited.
Therefore, the ash supply system in the related art has the defects of difficult accurate control of cement paste density, high labor cost, low automation degree, poor operation consistency, low fixing operation efficiency and low fixing quality, and needs to be improved.
Disclosure of Invention
In order to solve all or part of the problems, the invention aims to provide an ash supply system for fully automatic well cementation operation and a control method thereof, which can realize accurate control of cement paste density, reduce labor cost, improve automation degree, improve operation consistency and improve efficiency and quality of fixing operation.
In a first aspect, the present invention provides an ash supply system for a fully automatic cementing operation, comprising:
the ash storage tank is used for hermetically storing the dry cement ash;
the constant pressure tank is used for storing the dry cement ash in a constant pressure airtight manner;
the air source is used for providing power for conveying the dry cement ash;
the ash supply and air inlet pipeline is used for connecting the ash storage tank, the constant pressure tank, the air source and external slurry mixing equipment;
the monitoring system is arranged on the ash storage tank, the constant pressure tank and the ash supply and air inlet pipeline and is used for monitoring the pressure of the ash storage tank, the constant pressure tank and the ash supply and air inlet pipeline and the cement ash accumulation in real time;
The control valve group is arranged on the ash supply and air inlet pipeline and is used for controlling the fluid flow in the ash supply and air inlet pipeline;
the man-machine interaction interface is used for an operator to input an operation instruction;
the data acquisition system is respectively connected with the man-machine interaction interface and the monitoring system and is used for acquiring pressure signals and stock signals of the ash storage tank and the constant pressure tank in real time, acquiring pressure signals of the ash supply and air inlet pipelines, acquiring valve position signals of the control valve bank and receiving operation instructions from the man-machine interaction interface;
the automatic control system is respectively connected with the control valve group and the data acquisition system, is used for responding to the received operation instruction, and controls the opening and closing of the air source, the pipeline between the ash storage tank and the constant pressure tank, the pipeline between the discharge port of the ash storage tank and the feed port of the constant pressure tank, the pipeline between the discharge port of the constant pressure tank and external slurry mixing equipment, and the storage capacity and the pressure of the constant pressure tank;
the operation instructions of the man-machine interaction interface comprise, but are not limited to, an ash supply operation start/stop instruction, an ash storage tank pressure set value, an ash storage tank/constant pressure tank bottom air inlet pipeline pressure set value, a constant pressure tank pressure set value and a constant pressure tank cement ash storage set value.
Optionally, the ash supply and air intake line comprises:
the gas transmission pipe is connected with the gas source;
one end of the first air pipe is connected with the air pipe, and the other end of the first air pipe is connected to the bottom of the ash storage tank;
one end of the second air pipe is connected with the air pipe, and the other end of the second air pipe is connected to the bottom of the constant pressure tank;
one end of the discharging pipe is connected with the ash storage tank, and the other end of the discharging pipe is connected with the constant pressure tank;
one end of the air blowing pipe is connected with the air conveying pipe, and the other end of the air blowing pipe is connected with the discharging pipe so as to assist in conveying dry cement ash;
one end of the discharge pipe is connected to the constant pressure tank, and the other end of the discharge pipe is connected with external slurry mixing equipment;
one end of the standby pipe is connected with the discharging pipe, and the other end of the standby pipe is connected with external slurry mixing equipment;
the emptying pipe is connected to the constant pressure tank to realize the emptying of the constant pressure tank;
the two ends of the balance pipe are respectively connected with the emptying pipe;
one end of the adjusting pipe is connected with the gas pipe, and the other end of the adjusting pipe is connected with the balance pipe.
Optionally, the control valve group includes:
control valve V 1 Is connected to the first air pipe;
control valve V 2 Is connected to the air blowing pipe;
control valve V 3 Is connected to the second air pipe;
Control valve V 4 Is connected to the regulating pipe;
control valve V 5 The discharging pipe is connected with the upper end of the pipe body;
control valve V 6 Connected to the discharging pipe, and the port of the standby pipe is positioned at the control valve V 5 And a control valve V 6 Between them;
control valve V 7 Connected to the reserve tube;
control valve V 8 Connected to the discharge pipe;
control valve V 9 Is connected to the emptying pipe;
control valve V 10 Is connected to the balance pipe, and the regulating pipe and the control valve V 10 Connecting;
wherein the control valve V 1 -V 10 And the control system is respectively connected with the automatic control system.
Optionally, the monitoring system comprises:
pressure detector W 1 The ash storage tank is arranged at the bottom of the ash storage tank so as to monitor cement ash storage in the ash storage tank;
pressure detector W 2 The device is arranged at the bottom of the constant pressure tank to monitor the cement ash accumulation in the constant pressure tank;
pressure gauge P 1 Is connected to the first air pipe;
pressure gauge P 2 The ash storage tank is connected to the top of the ash storage tank;
pressure gauge P 3 Is connected to the second air pipe;
pressure gauge P 4 The top of the constant pressure tank is connected with the bottom of the constant pressure tank;
pressure gauge P 5 Is connected to the regulating pipe;
wherein the pressure gauge P 1 -P 5 Respectively with the data acquisition The collection system is connected.
Optionally, the bottoms of the ash storage tank and the constant pressure tank are respectively connected with an air distributor, and the first air pipe and the second air pipe are respectively connected with the corresponding air distributors.
In a second aspect, the present invention provides a control method of an ash supply system, including the steps of:
s1, inputting operation instructions on a human-computer interaction interface, wherein the operation instructions comprise a pressure set value p of an air inlet pipeline at the bottom of the ash storage tank 1,sp Set point p of top pressure of ash storage tank 2,sp Pressure set value p of air inlet pipeline at bottom of constant-pressure tank 3,sp Set point p of pressure at top of constant pressure tank 4,sp Constant pressure pot storage quantity set value w 2 , sp ；
S2, purging the ash supply and air inlet pipeline and the constant pressure tank, ensuring that the ash supply and air inlet pipeline are smooth, and blowing out the residual dry cement ash in the constant pressure tank;
s3, controlling the air inlet pressure of the ash storage tank, and when the top pressure of the ash storage tank reaches a set value p 2,sp The pipeline communication between the ash outlet of the ash storage tank and the feed inlet of the constant pressure tank is controlled;
s4, controlling the bottom air inlet pressure of the ash storage tank, the bottom air inlet pressure of the constant pressure tank, the cement ash storage capacity of the constant pressure tank and the pressure of the constant pressure tank so as to realize accurate control of ash supply quantity and air inflow.
Optionally, in S4, controlling the ash storage tank bottom intake pressure includes: collecting pressure gauge P in real time through data collecting system 1 Pressure signal p of (2) 1 Then the pressure of the air inlet line at the bottom of the ash storage tank is set to be p 1,sp Taking difference, obtaining pressure deviation signal, inputting into the first pressure control module of automatic control system, calculating to obtain control valve V 1 Is downloaded and executed;
by the formula:
calculating the pressure set value p at the kth sampling moment 1,sp Deviation from the kth sampling instant pressure measurement signal, wherein e 1 (k) For the pressure deviation signal, p, of the air inlet line at the bottom of the ash storage tank at the kth sampling moment 1,sp (k) For the pressure set value, p, of the air inlet pipeline at the bottom of the ash storage tank at the kth sampling moment 1 (k) For the kth sampling instant pressure gauge P 1 Is a measurement of (2);
by the formula:
calculating a k-th sampling time control valve V 1 Wherein Deltav is 1 (k) Control valve V for the kth sampling instant 1 K is the opening increment signal of (1) p,1 Is a proportionality coefficient in the first pressure control module, and K p,1 Taking 0.015, T i,1 Is an integral time coefficient in the first pressure control module, and T i,1 Taking 0.5, T as sampling step length, e 1 (k) For the pressure deviation value, e, at the kth sampling instant 1 (k-1) is the pressure deviation value at the (k-1) th sampling time, and when k=1, e is set 1 (0)=0，△v 1,max For controlling valve V 1 Upper limit of opening increment, deltav 1,min For controlling valve V 1 Opening increment lower limit value;
by the formula:
calculating a k-th sampling time control valve V 1 Wherein v is 1 (k) Control valve V for the kth sampling instant 1 Opening degree signal v of (v) 1 (k-1) is the (k-1) th sampling timing control valve V 1 When k=1, set v 1 (0)=0，v 1,max For controlling valve V 1 Upper limit value of opening degree v 1,min For controlling valve V 1 Lower limit value of the opening degree of (c).
Optionally, in S4, controlling the constant pressure tank cement ash inventory includes: pressure detector W is acquired in real time through data acquisition system 2 Is a measurement signal w of (2) 2 Then the stored constant pressure is used for storing the set value of the volumew 2 , sp Making a difference, obtaining a first stock deviation signal, inputting the first stock deviation signal into a first stock control module of an automatic control system, outputting the expected ash inlet amount of the constant pressure tank after calculation by the first stock control module, summing the expected ash inlet amount with the output value of an ash outlet amount calculation module of the automatic control system, subtracting the output value of an ash inlet amount calculation module of the automatic control system to obtain a second stock deviation signal, inputting the second stock deviation signal into a second stock control module of the automatic control system, and finally calculating by the second stock control module to obtain a control valve V 6 Is downloaded and executed;
by the formula:
calculating the deviation between the constant-pressure tank inventory set value at the kth sampling time and the inventory measurement signal at the kth sampling time, wherein e 2 (k) Is the constant-pressure tank stock deviation signal at the kth sampling moment, w 2 , sp (k) Setting value w for constant-pressure tank inventory at kth sampling time 2 (k) A constant-pressure canning measurement value at the kth sampling moment;
by the formula:
calculating an expected ash feed amount increment signal of the constant-pressure tank at the kth sampling time, wherein delta G 0 (k) Expected ash amount increment signal for constant pressure tank at kth sampling time, K p,2 Is the proportionality coefficient in the first stock control module, and K p,2 1.2, T i,2 Is an integral time coefficient in the first stock control module, and T i,2 Taking 2.0, T as sampling step length, e 2 (k) E is the reserve deviation value of the kth sampling moment 2 (k-1) is the pressure deviation value at the (k-1) th sampling time, and when k=1, e is set 2 (0)=0，△G 0,max The expected ash feeding amount increment upper limit value of the constant pressure tank is delta G 0,min A lower limit value of the expected ash feeding amount increment of the constant-pressure tank;
by the formula:
calculating the expected ash feeding amount of the constant-pressure tank at the kth sampling moment, G 0 (k) The expected ash feeding amount of the constant-pressure tank at the kth sampling time G 0 (k-1) the expected ash amount for the constant pressure tank at the (k-1) th sampling time, and when k=1, setting G 0 (0)=0，G 0,max An upper limit value of the expected ash feeding amount of the constant-pressure tank G 0,min The lower limit value of the expected ash feeding amount of the constant-pressure tank;
by the formula:
calculating ash output of a constant-pressure tank at the kth sampling moment, wherein G 1 (k) Calculating the ash output value k for the constant-pressure tank at the kth sampling moment 1 For controlling valve V 8 Dimensionless flow coefficient, v 8 (k) Control valve V for the kth sampling instant 8 Opening value of S 1 For cross-sectional area of discharge pipe, p 4 (k) Barometer P for the kth sampling instant 4 G=9.807 is the gravitational acceleration constant, w 2 (k) For the kth sampling instant pressure detector W 2 S, S Constant pressure tank Is the cross-sectional area of the constant pressure tank, ρ Air flow Is the density of air, n 1 Designing an ash-gas ratio for an ash outlet pipeline of the constant-pressure tank;
by the formula:
calculating the ash feeding amount of the constant-pressure tank at the kth sampling moment, wherein G 2 (k) The ash amount calculation value, k, is calculated for the constant pressure tank at the kth sampling time 2 For controlling valve V 6 Dimensionless flow coefficient, v 6 (k) Control valve V for the kth sampling instant 6 Opening value S 2 For the cross-sectional area of the tapping pipe, p 2 (k) Is thatBarometer P at the kth sampling instant 2 Measured value of p 4 (k) Barometer P for the kth sampling instant 4 G=9.807 is the gravitational acceleration constant, w 1 (k) For the kth sampling instant pressure detector W 1 S, S Ash storage tank For the cross-sectional area of the ash storage tank ρ Air flow Is the density of air, n 2 Designing an ash-gas ratio for an ash inlet pipeline between the ash storage tank and the constant pressure tank;
By the formula:
calculating an ash inlet amount deviation value of a constant-pressure tank at the kth sampling moment, wherein e 3 (k) Taking the ash inlet amount deviation value of the constant-pressure tank at the kth sampling moment as the input of the second stock control module;
by the formula:
control valve V for calculating the kth sampling instant 6 Wherein Deltav is 6 (k) Control valve V for the kth sampling instant 6 K is the opening increment signal of (1) p,3 Is the proportionality coefficient in the second stock control module, and K p,3 1.0, T i,3 Is an integral time coefficient in the second stock control module, and T i,3 Taking 100, T as sampling step length, e 3 (k) E is the deviation value of the ash feeding amount at the kth sampling time 3 (k-1) is an ash amount deviation value at the (k-1) th sampling timing, and when k=1, e is set 3 (0)=0，△v 6,max For controlling valve V 6 Upper limit of opening increment, deltav 6,min For controlling valve V 6 Opening increment lower limit value;
by the formula:
calculate the kth sampleTime control valve V 6 Wherein v is 6 (k) Control valve V for the kth sampling instant 6 Opening degree signal v of (v) 6 (k-1) is the (k-1) th sampling timing control valve V 6 When k=1, set v 6 (0)=0，v 6,max For controlling valve V 6 Upper limit value of opening degree v 6,min For controlling valve V 6 Lower limit value of the opening degree of (c).
Optionally, in S4, controlling the constant pressure tank bottom intake line pressure includes: collecting pressure gauge P in real time through data collecting system 3 Pressure signal p of (2) 3 Then the pressure of the air inlet line at the bottom of the constant pressure tank is set to be p 3,sp Performing difference, obtaining a pressure deviation signal, inputting the pressure deviation signal into a second pressure control module of the automatic control system, and calculating to obtain a control valve V 3 Is downloaded and executed;
by the formula:
calculating the deviation of the pressure set point of the inlet line of the constant pressure tank at the kth sampling time from the pressure measurement signal at the kth sampling time, wherein e 4 (k) The pressure deviation signal of the air inlet line at the bottom of the constant-pressure tank at the kth sampling moment, p 3,sp (k) The pressure of the bottom air inlet line of the constant-pressure tank at the kth sampling moment is set to be p 3 (k) For the kth sampling instant pressure gauge P 3 Is a measurement of (2);
by the formula:
calculating a k-th sampling time control valve V 3 Wherein Deltav is 3 (k) Control valve V for the kth sampling instant 3 K is the opening increment signal of (1) p,4 Is the proportionality coefficient in the second pressure control module and K p,4 Taking 0.010, T i,4 Is an integral time coefficient in the second pressure control module, and T i,4 Taking 2.0, T as sampling step length, e 4 (k) For the pressure deviation value, e, at the kth sampling instant 4 (k-1) is the pressure deviation value at the (k-1) th sampling time, and when k=1, e is set 4 (0)=0，△v 3,max For controlling valve V 3 Upper limit of opening increment of Deltav 3,min For controlling valve V 3 Lower limit value of opening increment of (2);
by the formula:
calculating a k-th sampling time control valve V 3 Wherein v is 3 (k) Control valve V for the kth sampling instant 3 An opening signal of (2); v 3 (k-1) is the (k-1) th sampling timing control valve V 3 When k=1, set v 3 (0)=0，v 3,max For controlling valve V 3 Upper limit value of opening degree v 3,min For controlling valve V 3 Lower limit value of the opening degree of (c).
Optionally, in S4, controlling the constant pressure tank pressure includes: collecting pressure gauge P in real time through data collecting system 4 Pressure signal p of (2) 4 Then with the constant pressure tank pressure set value p 4,sp The difference is made, a pressure deviation signal 1 is obtained and then is input into a third pressure control module of the automatic control system, and a control valve V is output after calculation by the third pressure control module 4 Desired intake pressure, and control valve V 4 The pressure deviation signal 2 is obtained by actually measuring the intake pressure difference and then is input into a fourth pressure control module of an automatic control system, and finally the control valve V is obtained by calculation of the fourth pressure control module 4 Opening degree signals are downloaded and executed;
by the formula:
calculating a desired intake pressure increase signal of the constant pressure valve at a kth sampling time, wherein ΔP 0 (k) Control valve V for the kth sampling instant 4 Desired intake pressure increaseQuantity signal, K p,5 Is a proportionality coefficient in the third pressure control module, and K p,5 Taking 15, T i,5 Is an integral time coefficient in the third pressure control module, and T i,5 Taking 0.1, T as sampling step length, e 5 (k) E is the constant pressure tank pressure deviation value at the kth sampling time 5 (k-1) is a constant pressure tank pressure deviation value at the (k-1) th sampling timing, and when k=1, e is set 5 (0)=0，△P 0,max For controlling valve V 4 Upper limit value of desired intake pressure increase, Δp 0,min For controlling valve V 4 A desired intake pressure lower limit value;
by the formula:
control valve V for calculating the kth sampling instant 4 Desired intake pressure, where P 0 (k) Control valve V for the kth sampling instant 4 Desired intake pressure, P 0 (k-1) control valve V at the (k-1) th sampling timing 4 Desired intake pressure, when k=1, P is set 0 (0)=0，P 0,max An expected ash feeding amount upper limit value P for the constant pressure tank 0,min The lower limit value of the expected ash feeding amount of the constant-pressure tank;
by the formula:
control valve V for calculating the kth sampling instant 4 A pressure deviation of the intake line, wherein e 6 (k) Control valve V for the kth sampling instant 4 As an input to a fourth pressure control module;
by the formula:
calculating a k-th sampling time control valve V 4 Delta v of opening increment signal 4 (k) For the kth sampling time control Valve V 4 K is the opening increment signal of (1) p,6 Is the proportionality coefficient in the fourth pressure control module, and K p,6 200.0, T i,6 Is an integral time coefficient in the fourth pressure control module, and T i,6 Taking 1000, T as sampling step length, e 6 (k) E is the pressure deviation value of the inlet line of the constant pressure tank at the kth sampling time 6 (k-1) is the pressure deviation value of the inlet line of the constant pressure tank at the (k-1) th sampling time, and when k=1, setting e 6 (0)=0，△v 4,max For controlling valve V 4 Upper limit of opening increment, deltav 4,min For controlling valve V 4 Opening increment lower limit value;
by the formula:
calculating a k-th sampling time control valve V 4 Wherein v is 4 (k) Control valve V for the kth sampling instant 4 Opening degree signal v of (v) 4 (k-1) is the (k-1) th sampling timing control valve V 4 When k=1, set v 4 (0)=0，v 4,max For controlling valve V 4 Upper limit value of opening degree v 4,min For controlling valve V 4 Lower limit value of the opening degree of (c).
According to the technical scheme, the ash supply system for the full-automatic well cementation operation and the control method thereof provided by the invention have the following advantages:
according to the ash supply system and the control method, valve position signals of the collection, pressure and control valve groups of the ash supply system are collected in real time through the data collection system, control instructions from a human-computer interaction interface are received, control signals of opening degrees of control valves on ash supply and air blowing pipelines are obtained after calculation through the automatic control system, stable control of ash supply quantity and air inflow is achieved, ash supply quantity is ensured to be matched with ash demand of subsequent well cementation and slurry mixing equipment, meanwhile labor intensity of operators is reduced, and errors caused by human factors are avoided. Meanwhile, the design can realize remote monitoring and full-automatic control of well cementation ash supply, on one hand, coordination and unified control among different ash supply devices such as an ash storage tank, a constant pressure tank, an air source, various control valves and the like can be realized, the functions of the devices are exerted to the greatest extent, stable ash supply is ensured, and the problem that the density of cement paste is difficult to control due to large fluctuation of the traditional ash supply amount is solved. On the other hand, the labor intensity of operators can be reduced, errors caused by human factors are reduced, and the method has very important significance for safe and efficient well cementation and ash supply operation.
Additional features and advantages of the invention will be set forth in the description which follows.
Drawings
The accompanying drawings are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate and do not limit the invention.
FIG. 1 is a schematic view showing the overall structure of an ash supply system according to embodiment 1 of the present invention;
FIG. 2 is a schematic view of the ash supply and air intake line in embodiment 1 of the present invention;
FIG. 3 is a flow chart of a method for controlling an ash supply system according to embodiment 2 of this invention;
FIG. 4 is a schematic view of the pressure control of the air inlet line at the bottom of the ash storage tank in example 2 of this invention;
FIG. 5 is a schematic diagram showing the constant pressure pot life control in example 2 of the present invention;
FIG. 6 is a schematic diagram of a calculation module for ash flow rate from a constant pressure tank in embodiment 2 of the present invention;
FIG. 7 is a schematic diagram of a calculation module for ash inlet flow rate of the constant pressure tank in embodiment 2 of the present invention;
FIG. 8 is a schematic diagram showing the pressure control of the inlet line at the bottom of the constant pressure tank in example 2 of the present invention;
FIG. 9 is a schematic diagram showing the pressure control of the constant pressure tank in example 2 of the present invention.
Reference numerals illustrate:
1. an ash storage tank; 2. a constant pressure tank; 3. a gas source; 4. ash supply and air intake lines; 401. a gas pipe; 402. a first air tube; 403. a second air pipe; 404. a discharge pipe; 405. an air blowing pipe; 406. a discharge pipe; 407. a reserve tube; 408. an evacuation tube; 409. a balance tube; 410. an adjusting tube; 5. a monitoring system 6 and a control valve group; 7. a human-computer interaction interface; 8. a data acquisition system; 9. an automatic control system; 10. an air distributor.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the present invention more apparent, embodiments of the present invention will be described in detail hereinafter with reference to the accompanying drawings. It should be noted that, without conflict, the embodiments of the present invention and features of the embodiments may be arbitrarily combined with each other.
Fig. 1 and 2 show an embodiment 1 of the present invention, in which an ash supply system for fully automatic cementing operation is disclosed, and the ash supply system comprises an ash storage tank 1, a constant pressure tank 2, an air source 3, an ash supply and air intake pipeline 4, a monitoring system 5, a control valve group 6, a man-machine interaction interface 7, a data acquisition system 8 and an automatic control system 9.
In one embodiment, as shown in fig. 1 and 2, the ash storage tank 1 is used for storing dry cement ash in a closed manner, is a transmitting device based on pneumatic conveying of the dry cement ash, and the constant pressure tank 2 is used for storing the dry cement ash in a constant pressure closed manner and plays roles in gas ash separation, pressure stabilizing buffering and emergency storage. The air source 3 provides power for the delivery of the dry cement ash for powering the fluidization, delivery of the dry cement ash and purging the lines.
In one embodiment, as shown in fig. 1 and 2, the ash supply and intake line 4 connects the ash storage tank 1, the constant pressure tank 2, the air source 3 and the external slurry mixing equipment, the monitoring system 5 is disposed on the ash storage tank 1, the constant pressure tank 2 and the ash supply and intake line 4, and the monitoring system 5 is used for monitoring the pressures of the ash storage tank 1, the constant pressure tank 2 and the ash supply and intake line 4 and the cement ash storage amount in real time.
In one embodiment, as shown in fig. 1 and 2, a control valve block 6 is disposed on the ash supply and intake line 4, and the control valve block 6 is used to control the flow rate of the fluid in the ash supply and intake line 4. The man-machine interface 7 is used for an operator to input operation instructions, and the operation instructions of the man-machine interface 7 include, but are not limited to, an ash supply operation start/stop instruction, an ash storage tank 1 pressure set value, an ash storage tank 1/constant pressure tank 2 bottom air inlet line pressure set value, a constant pressure tank 2 pressure set value, and a constant pressure tank 2 cement ash storage set value.
In one embodiment, as shown in fig. 1 and 2, the data acquisition system 8 is connected to the man-machine interface 7 and the monitoring system 5, respectively, and the data acquisition system 8 is configured to acquire pressure signals and stock signals of the ash storage tank 1 and the constant pressure tank 2, acquire pressure signals of the ash supply and air intake pipeline 4, acquire valve position signals of the control valve group 6, and receive operation instructions from the man-machine interface 7 in real time.
In one embodiment, as shown in fig. 1 and 2, the automatic control system 9 is connected to the control valve group 6 and the data acquisition system 8 respectively, and is used for responding to received operation instructions, controlling the opening and closing of the air source 3, the pipeline between the ash storage tank 1 and the constant pressure tank 2, the pipeline between the discharge port of the ash storage tank 1 and the feed port of the constant pressure tank 2, and the pipeline between the discharge port of the constant pressure tank 2 and the external slurry mixing equipment, and controlling the storage capacity and pressure of the constant pressure tank 2.
In the ash supply system in the embodiment, the data acquisition system 8 is used for acquiring the collection, pressure and valve position signals of the ash supply system and receiving the control instruction from the man-machine interaction interface 7 in real time, and the control signal of the opening degree of the control valve on the line of the ash supply and air blowing pipe 405 is obtained after calculation by the automatic control system 9, so that stable control of the ash supply amount and the air inflow is realized, the ash supply amount is ensured to be matched with the ash demand of the subsequent well cementation slurry mixing equipment, the labor intensity of operators is reduced, and errors caused by human factors are avoided.
In one embodiment, as shown in FIGS. 1 and 2, the ash supply and intake line 4 includes a gas pipe 401, a first gas pipe 402, a second gas pipe 403, a discharge pipe 404, a blow pipe 405, a discharge pipe 406, a reserve pipe 407, an evacuation pipe 408, a balance pipe 409, and a regulator pipe 410. The control valve group 6 comprises a control valve V 1 Control valve V 2 Control valve V 3 Control valve V 4 Control valve V 5 Control valve V 6 Control valve V 7 Control valve V 8 Control valve V 9 Control valve V 10 。
In one embodiment, as shown in FIGS. 1 and 2, a gas pipe 401 is connected to a gas source 3, and one end of a first gas pipe 402 is connected to the gas pipe 401,The other end is connected with the bottom of the ash storage tank 1 and is provided with a control valve V 1 Is connected to the first air tube 402. One end of the second air pipe 403 is connected with the air pipe 401, the other end is connected with the bottom of the constant pressure tank 2, and the valve V is controlled 3 Connected to the second air tube 403.
In one embodiment, as shown in fig. 1 and 2, one end of the discharging pipe 404 is connected with the ash storage tank 1, the other end is connected with the constant pressure tank 2, and the valve V is controlled 5 And a control valve V 6 Which in turn are connected to the tapping pipe 404. One end of the air blowing pipe 405 is connected with the air pipe 401, the other end is connected with the discharging pipe 404 to assist the conveying of the dry cement ash, and the valve V is controlled 2 Connected to the insufflation tube 405.
In one embodiment, as shown in fig. 1 and 2, one end of the discharge pipe 406 is connected to the constant pressure tank 2, the other end is connected to the external slurry mixing apparatus, and the valve V is controlled 8 Connected to the drain 406. One end of the standby pipe 407 is connected with the discharging pipe 404, the other end is connected with external slurry mixing equipment, and the port of the standby pipe 407 is positioned at the control valve V 5 And a control valve V 6 Between, at the same time, control valve V 7 Is connected to the reserve pipe 407 so that dry cement ash can be discharged through the reserve pipe 407 when the discharge pipe 406 or the constant pressure tank 2 fails, to improve the fault tolerance.
In one embodiment, as shown in fig. 1 and 2, an evacuation tube 408 is connected to the constant pressure tank 2 to effect evacuation of the constant pressure tank 2, and control valve V 9 Is connected to an evacuation tube 408. Two ends of the balance pipe 409 are respectively connected with the emptying pipe 408, and the valve V is controlled 10 Is connected to the balance pipe 409, one end of the adjusting pipe 410 is connected to the gas pipe 401, and the other end is connected to the control valve V 10 Connected, control valve V 10 Is one of the spring valves and is mainly used for balancing the pressure in the constant pressure tank 2.
In one embodiment, as shown in FIGS. 1 and 2, wherein the valve V is controlled 1 -V 10 Respectively connected with an automatic control system 9 and a control valve V 1 -V 10 Solenoid valves may be employed and the automatic control system 9 is capable of regulating the control valve V 1 -V 10 Opening degree and opening and closing control, thereby realizing remote control capabilityForce.
In one embodiment, as shown in FIGS. 1 and 2, the monitoring system 5 includes a pressure detector W 1 Pressure detector W 2 Pressure gauge P 1 Pressure gauge P 2 Pressure gauge P 3 Pressure gauge P 4 Pressure gauge P 5 . Pressure detector W 1 Is arranged at the bottom of the ash storage tank 1 to monitor the cement ash storage capacity in the ash storage tank 1 and a pressure detector W 2 Is arranged at the bottom of the constant pressure tank 2 to monitor the cement ash accumulation in the constant pressure tank 2.
In one embodiment, as shown in FIGS. 1 and 2, a pressure gauge P 1 Is connected to the first air pipe 402 to monitor the pressure of the air inlet line at the bottom of the ash storage tank 1, and is provided with a pressure gauge P 2 Is connected to the top of the ash storage tank 1 to realize the monitoring of the tank top pressure of the ash storage tank 1.
In one embodiment, as shown in FIGS. 1 and 2, a pressure gauge P 3 Is connected to a second air pipe 403 to realize the monitoring of the pressure of the air inlet line at the bottom of the constant pressure tank 2, and a pressure gauge P 4 Is connected to the top of the constant pressure tank 2 to realize the monitoring of the tank top pressure of the constant pressure tank 2.
In one embodiment, as shown in FIGS. 1 and 2, a pressure gauge P 5 Connected to the regulating tube 410, the pressure gauge P 1 -P 5 Respectively connected with the data acquisition system 8 to enable the pressure gauge P 1 -P 5 The acquired signals can be transmitted to a data collection system.
In one embodiment, as shown in fig. 1 and 2, the bottoms of the ash storage tank 1 and the constant pressure tank 2 are respectively connected with an air distributor 10, and the first air pipe 402 and the second air pipe 403 are respectively connected with the corresponding air distributors 10, so that the air entering the ash storage tank 1 and the constant pressure tank 2 can be dispersed, and the air can be blown more uniformly and in a large area.
According to the ash supply system, stable control of ash supply quantity and air inflow can be achieved, the ash supply quantity is ensured to be matched with ash demand of follow-up well cementation slurry mixing equipment, meanwhile, labor intensity of operators is reduced, and errors caused by human factors are avoided.
As shown in fig. 3 to 9, embodiment 2 of the present invention discloses a control method of the ash supply system in embodiment 1,
s1, inputting operation instructions on a human-computer interaction interface, wherein the operation instructions comprise a pressure set value p of an air inlet pipeline at the bottom of the ash storage tank 1,sp Set point p of top pressure of ash storage tank 2,sp Pressure set value p of air inlet pipeline at bottom of constant-pressure tank 3,sp Set point p of pressure at top of constant pressure tank 4,sp Constant pressure pot storage quantity set value w 2 , sp 。
S2, sequentially opening the control valve V 9 /V 6 /V 5 /V 2 The air blown by the air source sweeps the discharging pipe and the constant pressure tank, ensures that an ash supply pipeline (namely the discharging pipe) between an ash outlet of the ash storage tank and an ash inlet of the constant pressure tank is smooth, and sweeps the residual dry cement ash in the constant pressure tank for a period of time (such as 1 minute), and then sequentially closes the corresponding control valves V 2 /V 5 /V 6 /V 9 。
S3, opening the control valve V 1 The air inlet of the ash storage tank is suppressed, and when the pressure at the top of the ash storage tank reaches a set value p 2,sp Sequentially opening the control valve V 5 /V 6 So that the discharging pipe is communicated with the water storage tank and the constant pressure tank;
s4, controlling the bottom air inlet pressure of the ash storage tank, the bottom air inlet pressure of the constant pressure tank, the cement ash storage capacity of the constant pressure tank and the pressure of the constant pressure tank until the constant pressure storage capacity reaches w 2,sp Opening the control valve V 3 When the pressure at the top of the constant-pressure tank reaches a set value p 4,sp Opening the control valve V 8 So that the discharge pipe communicates the constant pressure tank with external slurry mixing equipment and realizes accurate control of ash supply quantity and air inflow.
In one embodiment, as shown in FIG. 4, controlling the ash storage tank bottom intake pressure in S4 includes: collecting pressure gauge P in real time through data collecting system 1 Pressure signal p of (2) 1 Then the pressure of the air inlet line at the bottom of the ash storage tank is set to be p 1,sp Taking difference, obtaining pressure deviation signal, inputting into the first pressure control module of automatic control system, calculating to obtain control valve V 1 Is downloaded and executed. The specific process is as follows:
by the formula:
calculating the pressure set value p at the kth sampling moment 1,sp Deviation from the kth sampling instant pressure measurement signal, wherein e 1 (k) For the pressure deviation signal, p, of the air inlet line at the bottom of the ash storage tank at the kth sampling moment 1,sp (k) For the pressure set value, p, of the air inlet pipeline at the bottom of the ash storage tank at the kth sampling moment 1 (k) For the kth sampling instant pressure gauge P 1 Is a measurement of (a).
By the formula:
calculating a k-th sampling time control valve V 1 Wherein Deltav is 1 (k) Control valve V for the kth sampling instant 1 K is the opening increment signal of (1) p,1 Is a proportionality coefficient in the first pressure control module, and K p,1 Taking 0.015, T i,1 Is an integral time coefficient in the first pressure control module, and T i,1 Taking 0.5, T as sampling step length, e 1 (k) For the pressure deviation value, e, at the kth sampling instant 1 (k-1) is the pressure deviation value at the (k-1) th sampling time, and when k=1, e is set 1 (0)=0，△v 1,max For controlling valve V 1 Upper limit of opening increment, deltav 1,min For controlling valve V 1 Opening increment lower limit.
By the formula:
calculating a k-th sampling time control valve V 1 Wherein v is 1 (k) Control valve V for the kth sampling instant 1 Opening degree signal v of (v) 1 (k-1) is the (k-1) th sampling timing control valve V 1 When k=1, set v 1 (0)=0，v 1,max For controlling valve V 1 Upper limit value of opening degree v 1,min For controlling valve V 1 Lower limit value of the opening degree of (c).
In one embodiment, as shown in fig. 5, 6 and 7, controlling the cement ash accumulation of the constant pressure tank in S4 includes: pressure detector W is acquired in real time through data acquisition system 2 Is a measurement signal w of (2) 2 Then the stored constant pressure tank storage quantity set value w 2,sp Making a difference, obtaining a first stock deviation signal, inputting the first stock deviation signal into a first stock control module of an automatic control system, outputting the expected ash inlet amount of the constant pressure tank after calculation by the first stock control module, summing the expected ash inlet amount with the output value of an ash outlet amount calculation module of the automatic control system, subtracting the output value of an ash inlet amount calculation module of the automatic control system to obtain a second stock deviation signal, inputting the second stock deviation signal into a second stock control module of the automatic control system, and finally calculating by the second stock control module to obtain a control valve V 6 Is downloaded and executed. The specific process is as follows:
by the formula:
calculating the deviation between the constant-pressure tank inventory set value at the kth sampling time and the inventory measurement signal at the kth sampling time, wherein e 2 (k) Is the constant-pressure tank stock deviation signal at the kth sampling moment, w 2 , sp (k) Setting value w for constant-pressure tank inventory at kth sampling time 2 (k) And measuring constant-pressure canning amount at the kth sampling time.
By the formula:
calculating an expected ash feed amount increment signal of the constant-pressure tank at the kth sampling time, wherein delta G 0 (k) Expected ash amount increment signal for constant pressure tank at kth sampling time, K p,2 Is the proportionality coefficient in the first stock control module, and K p,2 1.2, T i,2 Is an integral time coefficient in the first stock control module, and T i,2 Taking 2.0, T as sampling step length, e 2 (k) E is the reserve deviation value of the kth sampling moment 2 (k-1) is the pressure deviation value at the (k-1) th sampling time, and when k=1, e is set 2 (0)=0，△G 0,max The expected ash feeding amount increment upper limit value of the constant pressure tank is delta G 0,min The lower limit value of the ash inlet quantity increment is expected for the constant pressure tank.
By the formula:
calculating the expected ash feeding amount of the constant-pressure tank at the kth sampling moment, G 0 (k) The expected ash feeding amount of the constant-pressure tank at the kth sampling time G 0 (k-1) the expected ash amount for the constant pressure tank at the (k-1) th sampling time, and when k=1, setting G 0 (0)=0，G 0,max An upper limit value of the expected ash feeding amount of the constant-pressure tank G 0,min The lower limit value of the expected ash feeding amount of the constant-pressure tank;
by the formula:
calculating ash output of a constant-pressure tank at the kth sampling moment, wherein G 1 (k) Calculating the ash output value k for the constant-pressure tank at the kth sampling moment 1 For controlling valve V 8 Dimensionless flow coefficient, v 8 (k) Control valve V for the kth sampling instant 8 Opening value of S 1 For cross-sectional area of discharge pipe, p 4 (k) Barometer P for the kth sampling instant 4 G=9.807 is the gravitational acceleration constant, w 2 (k) For the kth sampling instant pressure detector W 2 S, S Constant pressure tank Is the cross-sectional area of the constant pressure tank, ρ Air flow Is the density of air, n 1 And designing an ash-gas ratio for an ash outlet pipeline of the constant-pressure tank.
By the formula:
calculating the ash feeding amount of the constant-pressure tank at the kth sampling moment, wherein G 2 (k) The ash amount calculation value, k, is calculated for the constant pressure tank at the kth sampling time 2 For controlling valve V 6 Dimensionless flow coefficient, v 6 (k) Control valve V for the kth sampling instant 6 Opening value S 2 For the cross-sectional area of the tapping pipe, p 2 (k) Barometer P for the kth sampling instant 2 Measured value of p 4 (k) Barometer P for the kth sampling instant 4 G=9.807 is the gravitational acceleration constant, w 1 (k) For the kth sampling instant pressure detector W 1 S, S Ash storage tank For the cross-sectional area of the ash storage tank ρ Air flow Is the density of air, n 2 The ash-gas ratio is designed for an ash inlet pipeline between the ash storage tank and the constant pressure tank.
By the formula:
calculating an ash inlet amount deviation value of a constant-pressure tank at the kth sampling moment, wherein e 3 (k) Taking the ash inlet amount deviation value of the constant-pressure tank at the kth sampling moment as the input of the second stock control module;
by the formula:
control valve V for calculating the kth sampling instant 6 Wherein Deltav is 6 (k) Control valve V for the kth sampling instant 6 K is the opening increment signal of (1) p,3 Is the proportionality coefficient in the second stock control module, and K p,3 1.0, T i,3 Is an integral time coefficient in the second stock control module, and T i,3 Taking 100, T as sampling step length, e 3 (k) E is the deviation value of the ash feeding amount at the kth sampling time 3 (k-1) is the gray scale deviation value at the (k-1) th sampling time, whenWhen k=1, set e 3 (0)=0，△v 6,max For controlling valve V 6 Upper limit of opening increment, deltav 6,min For controlling valve V 6 Opening increment lower limit.
By the formula:
calculating a k-th sampling time control valve V 6 Wherein v is 6 (k) Control valve V for the kth sampling instant 6 Opening degree signal v of (v) 6 (k-1) is the (k-1) th sampling timing control valve V 6 When k=1, set v 6 (0)=0，v 6,max For controlling valve V 6 Upper limit value of opening degree v 6,min For controlling valve V 6 Lower limit value of the opening degree of (c).
In one embodiment, as shown in fig. 8, controlling the constant pressure tank bottom intake line pressure in S4 includes: collecting pressure gauge P in real time through data collecting system 3 Pressure signal p of (2) 3 Then the pressure is matched with the pressure set value P of the air inlet line at the bottom of the constant pressure tank 3,sp Performing difference, obtaining a pressure deviation signal, inputting the pressure deviation signal into a second pressure control module of the automatic control system, and calculating to obtain a control valve V 3 Is downloaded and executed. The specific process is as follows:
by the formula:
calculating the deviation of the pressure set point of the inlet line of the constant pressure tank at the kth sampling time from the pressure measurement signal at the kth sampling time, wherein e 4 (k) The pressure deviation signal of the air inlet line at the bottom of the constant-pressure tank at the kth sampling moment, p 3,sp (k) The pressure of the bottom air inlet line of the constant-pressure tank at the kth sampling moment is set to be p 3 (k) For the kth sampling instant pressure gauge P 3 Is a measurement of (a).
By the formula:
calculating a k-th sampling time control valve V 3 Wherein Deltav is 3 (k) Control valve V for the kth sampling instant 3 K is the opening increment signal of (1) p,4 Is the proportionality coefficient in the second pressure control module, and K p,4 Taking 0.010, T i,4 Is an integral time coefficient in the second pressure control module, and T i,4 Taking 2.0, T as sampling step length, e 4 (k) For the pressure deviation value, e, at the kth sampling instant 4 (k-1) is the pressure deviation value at the (k-1) th sampling time, and when k=1, e is set 4 (0)=0，△v 3,max For controlling valve V 3 Upper limit of opening increment of Deltav 3,min For controlling valve V 3 Lower limit value of the opening increment of (c).
By the formula:
calculating a k-th sampling time control valve V 3 Wherein v is 3 (k) Control valve V for the kth sampling instant 3 An opening signal of (2); v 3 (k-1) is the (k-1) th sampling timing control valve V 3 When k=1, set v 3 (0)=0，v 3,max For controlling valve V 3 Upper limit value of opening degree v 3,min For controlling valve V 3 Lower limit value of the opening degree of (c).
In one embodiment, as shown in fig. 9, controlling the constant pressure tank pressure in S4 includes: collecting pressure gauge P in real time through data collecting system 4 Pressure signal p of (2) 4 Then with the constant pressure tank pressure set point P 4,sp The difference is made, a pressure deviation signal 1 is obtained and then is input into a third pressure control module of the automatic control system, and a control valve V is output after calculation by the third pressure control module 4 Desired intake pressure, and control valve V 4 The pressure difference is measured, a pressure deviation signal 2 is obtained and then is input into a fourth pressure control module of the automatic control system, and the most Finally, the fourth pressure control module calculates the control valve V 4 And opening degree signals are downloaded and executed. The specific process is as follows:
by the formula:
calculating a deviation of the constant pressure tank pressure set point at the kth sampling time from the pressure measurement signal at the kth sampling time, wherein e 5 (k) For the constant pressure tank pressure deviation signal, p at the kth sampling time 4,sp (k) For the constant pressure tank pressure set value, p, at the kth sampling time 4 (k) A constant-voltage canning measurement value at the kth sampling moment;
by the formula:
calculating a desired intake pressure increase signal of the constant pressure valve at a kth sampling time, wherein ΔP 0 (k) Control valve V for the kth sampling instant 4 Desired intake pressure delta signal, K p,5 Is a proportionality coefficient in the third pressure control module, and K p,5 Taking 15, T i,5 Is an integral time coefficient in the third pressure control module, and T i,5 Taking 0.1, T as sampling step length, e 5 (k) E is the constant pressure tank pressure deviation value at the kth sampling time 5 (k-1) is a constant pressure tank pressure deviation value at the (k-1) th sampling timing, and when k=1, e is set 5 (0)=0，△P 0,max For controlling valve V 4 Upper limit value of desired intake pressure increase, Δp 0,min For controlling valve V 4 A desired intake pressure lower limit value;
by the formula:
control valve V for calculating the kth sampling instant 4 Desired intake pressure, where P 0 (k) Control valve V for the kth sampling instant 4 Desired intake pressure, P 0 (k-1) control valve V at the (k-1) th sampling timing 4 Desired intake pressure, when k=1, P is set 0 (0)=0，P 0,max An expected ash feeding amount upper limit value P for the constant pressure tank 0,min The lower limit value of the expected ash feeding amount of the constant-pressure tank;
by the formula:
control valve V for calculating the kth sampling instant 4 A pressure deviation of the intake line, wherein e 6 (k) Control valve V for the kth sampling instant 4 As an input to a fourth pressure control module;
by the formula:
calculating a k-th sampling time control valve V 4 Delta v of opening increment signal 4 (k) Control valve V for the kth sampling instant 4 K is the opening increment signal of (1) p,6 Is the proportionality coefficient in the fourth pressure control module, and K p,6 200.0, T i,6 Is an integral time coefficient in the fourth pressure control module, and T i,6 Taking 1000, T as sampling step length, e 6 (k) E is the pressure deviation value of the inlet line of the constant pressure tank at the kth sampling time 6 (k-1) is the pressure deviation value of the inlet line of the constant pressure tank at the (k-1) th sampling time, and when k=1, setting e 6 (0)=0，△v 4,max For controlling valve V 4 Upper limit of opening increment, deltav 4,min For controlling valve V 4 Opening increment lower limit value;
by the formula:
calculating a k-th sampling time control valve V 4 Wherein v is 4 (k) Is thatControl valve V for kth sampling time 4 Opening degree signal v of (v) 4 (k-1) is the (k-1) th sampling timing control valve V 4 When k=1, set v 4 (0)=0，v 4,max For controlling valve V 4 Upper limit value of opening degree v 4,min For controlling valve V 4 Lower limit value of the opening degree of (c).
The invention can be realized by various modern industrial control systems, such as PLC, DCS or other industrial control computer systems and computers connected with the industrial control systems, and special equipment can also be designed according to the method of the invention. The implementation is various, and the same function can be realized in different ways even on the control systems with the same model.
According to the method and the device, remote monitoring and full-automatic control of well cementation ash supply can be realized, coordination and unified control among different ash supply devices such as an ash storage tank, a constant pressure tank, an air source and various control valves can be realized on the one hand, the effects of the devices are exerted to the greatest extent, stable ash supply is ensured, and the problem that cement slurry density is difficult to control due to large fluctuation of traditional ash supply is solved. On the other hand, the labor intensity of operators can be reduced, errors caused by human factors are reduced, and the method has very important significance for safe and efficient well cementation and ash supply operation.
It is noted that unless otherwise indicated, technical or scientific terms used herein should be given the ordinary meaning as understood by one of ordinary skill in the art to which this invention belongs.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. In the description of the present invention, the meaning of "plurality" is two or more unless specifically defined otherwise.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present invention, and not for limiting the same; although the invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the invention, and are intended to be included within the scope of the appended claims and description. In particular, the technical features mentioned in the respective embodiments may be combined in any manner as long as there is no structural conflict. The present invention is not limited to the specific embodiments disclosed herein, but encompasses all technical solutions falling within the scope of the claims.

Claims (10)

1. An ash supply system for fully automatic well cementation operation, comprising:
an ash storage tank (1) for hermetically storing the dry cement ash;
the constant pressure tank (2) is used for storing the dry cement ash in a constant pressure airtight manner;
the air source (3) is used for providing power for conveying the dry cement ash;
an ash supply and air inlet pipeline (4) for connecting the ash storage tank (1), the constant pressure tank (2), the air source (3) and external slurry mixing equipment;
the monitoring system (5) is arranged on the ash storage tank (1), the constant pressure tank (2) and the ash supply and air inlet pipeline (4) and is used for monitoring the pressure of the ash storage tank (1), the constant pressure tank (2) and the ash supply and air inlet pipeline (4) and the cement ash storage in real time;
the control valve group (6) is arranged on the ash supply and air inlet pipeline (4) and is used for controlling the flow of fluid in the ash supply and air inlet pipeline (4);
a man-machine interaction interface (7) for an operator to input an operation instruction;
the data acquisition system (8) is respectively connected with the man-machine interaction interface (7) and the monitoring system (5) and is used for acquiring pressure signals and stock signals of the ash storage tank (1) and the constant pressure tank (2), acquiring pressure signals of the ash supply and air inlet pipelines (4), acquiring valve position signals of the control valve group (6) and receiving operation instructions from the man-machine interaction interface (7);
The automatic control system (9) is respectively connected with the control valve group (6) and the data acquisition system (8) and is used for responding to the received operation instruction, controlling pipelines among the air source (3), the ash storage tank (1) and the constant pressure tank (2), pipelines among a discharge port of the ash storage tank (1) and a feed port of the constant pressure tank (2), opening and closing of the pipelines among the discharge port of the constant pressure tank (2) and external slurry mixing equipment, and controlling the stock and pressure of the constant pressure tank (2);
the operation instructions of the man-machine interaction interface (7) comprise, but are not limited to, an ash supply operation start/stop instruction, an ash storage tank (1) pressure set value, an ash storage tank (1)/constant pressure tank (2) bottom air inlet pipeline pressure set value, a constant pressure tank (2) pressure set value and a constant pressure tank (2) cement ash storage set value.
2. The ash supply system according to claim 1, characterized in that said ash supply and intake line (4) comprises:
a gas pipe (401) connected with the gas source (3);
a first air pipe (402), one end of which is connected with the air pipe (401) and the other end of which is connected with the bottom of the ash storage tank (1);
a second air pipe (403), one end of which is connected with the air pipe (401) and the other end of which is connected with the bottom of the constant pressure tank (2);
One end of the discharging pipe (404) is connected with the ash storage tank (1), and the other end of the discharging pipe is connected with the constant pressure tank (2);
one end of the air blowing pipe (405) is connected with the air conveying pipe (401), and the other end of the air blowing pipe is connected with the discharging pipe (404) so as to assist in conveying the dry cement ash;
a discharge pipe (406) with one end connected to the constant pressure tank (2) and the other end connected to an external slurry mixing device;
a standby pipe (407), one end of which is connected with the discharging pipe (404) and the other end of which is connected with external slurry mixing equipment;
an evacuation pipe (408) connected to the constant pressure tank (2) to effect evacuation of the constant pressure tank (2);
a balance pipe (409) with two ends respectively connected with the emptying pipe (408);
and one end of the adjusting pipe (410) is connected with the air conveying pipe (401), and the other end of the adjusting pipe is connected with the balance pipe (409).
3. An ash supply system according to claim 2, characterised in that said control valve group (6) comprises:
control valve V 1 Is connected to the first gas pipe (402);
control valve V 2 Is connected to the blowing pipe (405);
control valve V 3 Is connected to the second air pipe (403);
control valve V 4 Is connected to the adjusting tube (410);
control valve V 5 Is connected to the tapping pipe (404);
control valve V 6 Is connected to the discharging pipe (404), and the port of the standby pipe (407) is positioned at the control valve V 5 And a control valve V 6 Between them;
control valve V 7 Is connected to the reserve tube (407);
control valve V 8 Is connected to the discharge pipe (406);
control valve V 9 Is connected to the evacuation tube (408);
control valve V 10 Connected to the balancing pipe (409), and the regulating pipe (410) is connected to the control valve V10;
wherein the control valve V 1 -V 10 Are respectively connected with the automatic control system (9).
4. An ash supply system according to claim 2, characterised in that the monitoring system (5) comprises:
pressure detector W 1 The device is arranged at the bottom of the ash storage tank (1) to monitor the cement ash storage capacity in the ash storage tank (1);
pressure detector W 2 The device is arranged at the bottom of the constant pressure tank (2) to monitor the cement ash accumulation in the constant pressure tank (2);
pressure gauge P 1 Is connected to the first gas pipe (402);
pressure gauge P 2 Is connected with the ash storageA top of the tank (1);
pressure gauge P 3 Is connected to the second air pipe (403);
pressure gauge P 4 Is connected to the top of the constant pressure tank (2);
pressure gauge P 5 Is connected to the adjusting tube (410);
wherein the pressure gauge P 1 -P 5 Are respectively connected with the data acquisition system (8).
5. The ash supply system according to claim 2, characterized in that the bottoms of the ash storage tank (1) and the constant pressure tank (2) are respectively connected with an air distributor (10), and the first air pipe (402) and the second air pipe (403) are respectively connected with the corresponding air distributor (10).
6. A control method of an ash supply system according to any of claims 1-5, characterized by the steps of:
s1, inputting operation instructions on a human-computer interaction interface, wherein the operation instructions comprise a pressure set value p of an air inlet pipeline at the bottom of the ash storage tank 1,sp Set point p of top pressure of ash storage tank 2,sp Pressure set value p of air inlet pipeline at bottom of constant-pressure tank 3,sp Set point p of pressure at top of constant pressure tank 4,sp Constant pressure pot storage quantity set value w 2 , sp ；
S2, purging the ash supply and air inlet pipeline and the constant pressure tank, ensuring that the ash supply and air inlet pipeline are smooth, and blowing out the residual dry cement ash in the constant pressure tank;
s3, controlling the air inlet pressure of the ash storage tank, and when the top pressure of the ash storage tank reaches a set value p 2,sp The pipeline communication between the ash outlet of the ash storage tank and the feed inlet of the constant pressure tank is controlled;
s4, controlling the bottom air inlet pressure of the ash storage tank, the bottom air inlet pressure of the constant pressure tank, the cement ash storage capacity of the constant pressure tank and the pressure of the constant pressure tank so as to realize accurate control of ash supply quantity and air inflow.
7. The control method according to claim 6, characterized in that in S4, the control is performedThe bottom air inlet pressure of the ash storage tank comprises: collecting pressure gauge P in real time through data collecting system 1 Pressure signal p of (2) 1 Then the pressure of the air inlet line at the bottom of the ash storage tank is set to be p 1,sp Taking difference, obtaining pressure deviation signal, inputting into the first pressure control module of automatic control system, calculating to obtain control valve V 1 Is downloaded and executed;
by the formula:
calculating the pressure set value p at the kth sampling moment 1,sp Deviation from the kth sampling instant pressure measurement signal, wherein e 1 (k) For the pressure deviation signal, p, of the air inlet line at the bottom of the ash storage tank at the kth sampling moment 1,sp (k) For the pressure set value, p, of the air inlet pipeline at the bottom of the ash storage tank at the kth sampling moment 1 (k) For the kth sampling instant pressure gauge P 1 Is a measurement of (2);
by the formula:
calculating a k-th sampling time control valve V 1 Wherein Deltav is 1 (k) Control valve V for the kth sampling instant 1 K is the opening increment signal of (1) p,1 Is a proportionality coefficient in the first pressure control module, and K p,1 Taking 0.015, T i,1 Is an integral time coefficient in the first pressure control module, and T i,1 Taking 0.5, T as sampling step length, e 1 (k) For the pressure deviation value, e, at the kth sampling instant 1 (k-1) is the pressure deviation value at the (k-1) th sampling time, and when k=1, e is set 1 (0)=0，△v 1,max For controlling valve V 1 Upper limit of opening increment, deltav 1,min For controlling valve V 1 Opening increment lower limit value;
by the formula:
calculating a k-th sampling time control valve V 1 Wherein v is 1 (k) Control valve V for the kth sampling instant 1 Opening degree signal v of (v) 1 (k-1) is the (k-1) th sampling timing control valve V 1 When k=1, set v 1 (0)=0，v 1,max For controlling valve V 1 Upper limit value of opening degree v 1,min For controlling valve V 1 Lower limit value of the opening degree of (c).
8. The control method according to claim 7, wherein controlling the cement ash accumulation of the constant pressure tank in S4 includes: pressure detector W is acquired in real time through data acquisition system 2 Is a measurement signal w of (2) 2 Then the stored constant pressure tank storage quantity set value w 2 , sp Making a difference, obtaining a first stock deviation signal, inputting the first stock deviation signal into a first stock control module of an automatic control system, outputting the expected ash inlet amount of the constant pressure tank after calculation by the first stock control module, summing the expected ash inlet amount with the output value of an ash outlet amount calculation module of the automatic control system, subtracting the output value of an ash inlet amount calculation module of the automatic control system to obtain a second stock deviation signal, inputting the second stock deviation signal into a second stock control module of the automatic control system, and finally calculating by the second stock control module to obtain a control valve V 6 Is downloaded and executed;
by the formula:
calculating the deviation between the constant-pressure tank inventory set value at the kth sampling time and the inventory measurement signal at the kth sampling time, wherein e 2 (k) Is the constant-pressure tank stock deviation signal at the kth sampling moment, w 2 , sp (k) Setting value w for constant-pressure tank inventory at kth sampling time 2 (k) A constant-pressure canning measurement value at the kth sampling moment;
by the formula:
calculating an expected ash feed amount increment signal of the constant-pressure tank at the kth sampling time, wherein delta G 0 (k) Expected ash amount increment signal for constant pressure tank at kth sampling time, K p,2 Is the proportionality coefficient in the first stock control module, and K p,2 1.2, T i,2 Is an integral time coefficient in the first stock control module, and T i,2 Taking 2.0, T as sampling step length, e 2 (k) E is the reserve deviation value of the kth sampling moment 2 (k-1) is the pressure deviation value at the (k-1) th sampling time, and when k=1, e is set 2 (0)=0，△G 0,max The expected ash feeding amount increment upper limit value of the constant pressure tank is delta G 0,min A lower limit value of the expected ash feeding amount increment of the constant-pressure tank;
by the formula:
calculating the expected ash feeding amount of the constant-pressure tank at the kth sampling moment, G 0 (k) The expected ash feeding amount of the constant-pressure tank at the kth sampling time G 0 (k-1) the expected ash amount for the constant pressure tank at the (k-1) th sampling time, and when k=1, setting G 0 (0)=0，G 0,max An upper limit value of the expected ash feeding amount of the constant-pressure tank G 0,min The lower limit value of the expected ash feeding amount of the constant-pressure tank;
by the formula:
calculating ash output of a constant-pressure tank at the kth sampling moment, wherein G 1 (k) Calculating the ash output value k for the constant-pressure tank at the kth sampling moment 1 For controlling valve V 8 Dimensionless flow coefficient, v 8 (k) For the kth sampling instantControl valve V of (2) 8 Opening value of S 1 For cross-sectional area of discharge pipe, p 4 (k) Barometer P for the kth sampling instant 4 G=9.807 is the gravitational acceleration constant, w 2 (k) For the kth sampling instant pressure detector W 2 S, S Constant pressure tank Is the cross-sectional area of the constant pressure tank, ρ Air flow Is the density of air, n 1 Designing an ash-gas ratio for an ash outlet pipeline of the constant-pressure tank;
by the formula:
calculating the ash feeding amount of the constant-pressure tank at the kth sampling moment, wherein G 2 (k) The ash amount calculation value, k, is calculated for the constant pressure tank at the kth sampling time 2 For controlling valve V 6 Dimensionless flow coefficient, v 6 (k) Control valve V for the kth sampling instant 6 Opening value S 2 For the cross-sectional area of the tapping pipe, p 2 (k) Barometer P for the kth sampling instant 2 Measured value of p 4 (k) Barometer P for the kth sampling instant 4 G=9.807 is the gravitational acceleration constant, w 1 (k) For the kth sampling instant pressure detector W 1 S, S Ash storage tank For the cross-sectional area of the ash storage tank ρ Air flow Is the density of air, n 2 Designing an ash-gas ratio for an ash inlet pipeline between the ash storage tank and the constant pressure tank;
By the formula:
calculating an ash inlet amount deviation value of a constant-pressure tank at the kth sampling moment, wherein e 3 (k) Taking the ash inlet amount deviation value of the constant-pressure tank at the kth sampling moment as the input of the second stock control module;
by the formula:
control valve V for calculating the kth sampling instant 6 Wherein Deltav is 6 (k) Control valve V for the kth sampling instant 6 K is the opening increment signal of (1) p,3 Is the proportionality coefficient in the second stock control module, and K p,3 1.0, T i,3 Is an integral time coefficient in the second stock control module, and T i,3 Taking 100, T as sampling step length, e 3 (k) E is the deviation value of the ash feeding amount at the kth sampling time 3 (k-1) is an ash amount deviation value at the (k-1) th sampling timing, and when k=1, e is set 3 (0)=0，△v 6,max For controlling valve V 6 Upper limit of opening increment, deltav 6,min For controlling valve V 6 Opening increment lower limit value;
by the formula:
calculating a k-th sampling time control valve V 6 Wherein v is 6 (k) Control valve V for the kth sampling instant 6 Opening degree signal v of (v) 6 (k-1) is the (k-1) th sampling timing control valve V 6 When k=1, set v 6 (0)=0，v 6,max For controlling valve V 6 Upper limit value of opening degree v 6,min For controlling valve V 6 Lower limit value of the opening degree of (c).
9. The control method according to claim 6, wherein controlling the constant pressure tank bottom intake line pressure in S4 comprises: collecting pressure gauge P in real time through data collecting system 3 Pressure signal p of (2) 3 Then the pressure of the air inlet line at the bottom of the constant pressure tank is set to be p 3,sp The difference is made, a pressure deviation signal is obtained and then is input into a second pressure control module of the automatic control system, and a control valve V is obtained through calculation 3 Is downloaded and executed;
by the formula:
calculating the deviation of the pressure set point of the inlet line of the constant pressure tank at the kth sampling time from the pressure measurement signal at the kth sampling time, wherein e 4 (k) The pressure deviation signal of the air inlet line at the bottom of the constant-pressure tank at the kth sampling moment, p 3,sp (k) The pressure of the bottom air inlet line of the constant-pressure tank at the kth sampling moment is set to be p 3 (k) For the kth sampling instant pressure gauge P 3 Is a measurement of (2);
by the formula:
calculating a k-th sampling time control valve V 3 Wherein Deltav is 3 (k) Control valve V for the kth sampling instant 3 K is the opening increment signal of (1) p,4 Is the proportionality coefficient in the second pressure control module and K p,4 Taking 0.010, T i,4 Is an integral time coefficient in the second pressure control module, and T i,4 Taking 2.0, T as sampling step length, e 4 (k) For the pressure deviation value, e, at the kth sampling instant 4 (k-1) is the pressure deviation value at the (k-1) th sampling time, and when k=1, e is set 4 (0)=0，△v 3,max For controlling valve V 3 Upper limit of opening increment of Deltav 3,min For controlling valve V 3 Lower limit value of opening increment of (2);
by the formula:
calculating a k-th sampling time control valve V 3 Wherein v is 3 (k) Control valve V for the kth sampling instant 3 An opening signal of (2); v 3 (k-1) is the (k-1) th sampling timing control valve V 3 When k=1, set v 3 (0)=0，v 3,max For controlling valve V 3 Upper limit value of opening degree v 3,min For controlling valve V 3 Lower limit value of the opening degree of (c).
10. The control method according to claim 1, characterized in that in S4, controlling the constant pressure tank pressure includes: collecting pressure gauge P in real time through data collecting system 4 Pressure signal p of (2) 4 Then with the constant pressure tank pressure set value p 4,sp The difference is made, a pressure deviation signal 1 is obtained and then is input into a third pressure control module of the automatic control system, and a control valve V is output after calculation by the third pressure control module 4 Desired intake pressure, and control valve V 4 The pressure deviation signal 2 is obtained by actually measuring the intake pressure difference and then is input into a fourth pressure control module of an automatic control system, and finally the control valve V is obtained by calculation of the fourth pressure control module 4 Opening degree signals are downloaded and executed;
by the formula:
calculating a deviation of the constant pressure tank pressure set point at the kth sampling time from the pressure measurement signal at the kth sampling time, wherein e 5 (k) For the constant pressure tank pressure deviation signal, p at the kth sampling time 4,sp (k) For the constant pressure tank pressure set value, p, at the kth sampling time 4 (k) A constant-voltage canning measurement value at the kth sampling moment;
by the formula:
calculating a desired intake pressure increase signal of the constant pressure valve at a kth sampling time, wherein ΔP 0 (k) Control valve V for the kth sampling instant 4 Desired intake pressure delta signal, K p,5 Is a proportionality coefficient in the third pressure control module, and K p,5 Taking 15, T i,5 Is an integral time coefficient in the third pressure control module, and T i,5 Taking 0.1, T as sampling step length, e 5 (k) E is the constant pressure tank pressure deviation value at the kth sampling time 5 (k-1) is a constant pressure tank pressure deviation value at the (k-1) th sampling timing, and when k=1, e is set 5 (0)=0，△P 0,max For controlling valve V 4 Upper limit value of desired intake pressure increase, Δp 0,min For controlling valve V 4 A desired intake pressure lower limit value;
by the formula:
control valve V for calculating the kth sampling instant 4 Desired intake pressure, where P 0 (k) Control valve V for the kth sampling instant 4 Desired intake pressure, P 0 (k-1) control valve V at the (k-1) th sampling timing 4 Desired intake pressure, when k=1, P is set 0 (0)=0，P 0,max An expected ash feeding amount upper limit value P for the constant pressure tank 0,min The lower limit value of the expected ash feeding amount of the constant-pressure tank;
By the formula:
control valve V for calculating the kth sampling instant 4 A pressure deviation of the intake line, wherein e 6 (k) Control valve V for the kth sampling instant 4 As an input to a fourth pressure control module;
by the formula:
calculating a k-th sampling time control valve V 4 Delta v of opening increment signal 4 (k) Control valve V for the kth sampling instant 4 K is the opening increment signal of (1) p,6 Is the proportionality coefficient in the fourth pressure control module, and K p,6 200.0, T i,6 Is an integral time coefficient in the fourth pressure control module, and T i,6 Taking 1000, T as sampling step length, e 6 (k) E is the pressure deviation value of the inlet line of the constant pressure tank at the kth sampling time 6 (k-1) is the pressure deviation value of the inlet line of the constant pressure tank at the (k-1) th sampling time, and when k=1, setting e 6 (0)=0，△v 4,max For controlling valve V 4 Upper limit of opening increment, deltav 4,min For controlling valve V 4 Opening increment lower limit value;
by the formula:
calculating a k-th sampling time control valve V 4 Wherein v is 4 (k) Control valve V for the kth sampling instant 4 Opening degree signal v of (v) 4 (k-1) is the (k-1) th sampling timing control valve V 4 When k=1, set v 4 (0)=0，v 4,max For controlling valve V 4 Upper limit value of opening degree v 4,min For controlling valve V 4 Lower limit value of the opening degree of (c).
CN202410253554.6A 2024-03-06 2024-03-06 Ash supply system for full-automatic well cementation operation and control method thereof Active CN117819216B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202410253554.6A CN117819216B (en) 2024-03-06 2024-03-06 Ash supply system for full-automatic well cementation operation and control method thereof

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202410253554.6A CN117819216B (en) 2024-03-06 2024-03-06 Ash supply system for full-automatic well cementation operation and control method thereof

Publications (2)

Publication Number Publication Date
CN117819216A true CN117819216A (en) 2024-04-05
CN117819216B CN117819216B (en) 2024-06-11

Family

ID=90513894

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202410253554.6A Active CN117819216B (en) 2024-03-06 2024-03-06 Ash supply system for full-automatic well cementation operation and control method thereof

Country Status (1)

Country Link
CN (1) CN117819216B (en)

Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0526808A1 (en) * 1991-08-05 1993-02-10 Siemens Aktiengesellschaft Method and device for transporting of powder
JPH0711312A (en) * 1993-06-24 1995-01-13 Kawasaki Steel Corp Control method for blowing of pulverized coal
CN103261114A (en) * 2011-02-22 2013-08-21 电气化学工业株式会社 Pneumatic transport facility for chlorine bypass dust, and cement kiln exhaust gas treatment system equipped with the facility
CN206407631U (en) * 2016-12-19 2017-08-15 深圳市三鑫精美特玻璃有限公司 A kind of automatic feeding device for constant pressure feeding system
CN108894748A (en) * 2018-07-10 2018-11-27 中石化四机石油机械有限公司 A kind of well cementation equipment is with automatically for apparatus for ash and control method
CN114033332A (en) * 2021-10-25 2022-02-11 中石化四机石油机械有限公司 Continuous and stable ash supply device for well cementation equipment and control method thereof
WO2022194202A1 (en) * 2021-03-16 2022-09-22 烟台杰瑞石油装备技术有限公司 Full-electric drive cementing control system
CN116812561A (en) * 2023-05-25 2023-09-29 常州市昊达电力设备有限公司 Pneumatic conveying system based on PLC monitoring
CN117067396A (en) * 2023-08-30 2023-11-17 中海油田服务股份有限公司 Cement paste preparation device
CN117605954A (en) * 2023-11-27 2024-02-27 四机赛瓦石油钻采设备有限公司 Automatic ash supply gas circuit control system of constant-pressure tank and control method thereof

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0526808A1 (en) * 1991-08-05 1993-02-10 Siemens Aktiengesellschaft Method and device for transporting of powder
JPH0711312A (en) * 1993-06-24 1995-01-13 Kawasaki Steel Corp Control method for blowing of pulverized coal
CN103261114A (en) * 2011-02-22 2013-08-21 电气化学工业株式会社 Pneumatic transport facility for chlorine bypass dust, and cement kiln exhaust gas treatment system equipped with the facility
CN206407631U (en) * 2016-12-19 2017-08-15 深圳市三鑫精美特玻璃有限公司 A kind of automatic feeding device for constant pressure feeding system
CN108894748A (en) * 2018-07-10 2018-11-27 中石化四机石油机械有限公司 A kind of well cementation equipment is with automatically for apparatus for ash and control method
WO2022194202A1 (en) * 2021-03-16 2022-09-22 烟台杰瑞石油装备技术有限公司 Full-electric drive cementing control system
CN114033332A (en) * 2021-10-25 2022-02-11 中石化四机石油机械有限公司 Continuous and stable ash supply device for well cementation equipment and control method thereof
CN116812561A (en) * 2023-05-25 2023-09-29 常州市昊达电力设备有限公司 Pneumatic conveying system based on PLC monitoring
CN117067396A (en) * 2023-08-30 2023-11-17 中海油田服务股份有限公司 Cement paste preparation device
CN117605954A (en) * 2023-11-27 2024-02-27 四机赛瓦石油钻采设备有限公司 Automatic ash supply gas circuit control system of constant-pressure tank and control method thereof

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
孔祥伟;于祥春;刘志芳;宫俭纯;李良;: "钻井船灰罐物料监测系统设计", 工业仪表与自动化装置, no. 05, 5 October 2011 (2011-10-05), pages 59 - 61 *

Also Published As

Publication number Publication date
CN117819216B (en) 2024-06-11

Similar Documents

Publication Publication Date Title
CN104990669B (en) Surge pressure sensor field calibration device
CN101360975B (en) System for measurement of process control fluid consumption
CN102183284B (en) Liquid flow standard calibration device
CN102658975A (en) High-pressure conveyed continuous powder body quantitative feeding device
CN106523916A (en) High-flow liquid medium combined supply system
CN203191151U (en) Vacuum gauge automatic calibrating device
CN109250504A (en) A kind of coal dust two-phase transportation accurately controls and the system and method for flow Fast Calibration
CN117819216B (en) Ash supply system for full-automatic well cementation operation and control method thereof
CN202057396U (en) Standard liquid flow calibration device
CN112611540B (en) Pressure self-adaptive adjusting device and method for flexible inflation wind tunnel test model
CN116272588A (en) Automatic manufacturing system for trace dissolved ternary mixed gas standard solution
CN112444307A (en) Carbon dioxide pipeline flow regulation and differential pressure flowmeter precision testing and calibrating system
CN106153162A (en) Gas flowmeter detection equipment
CN108153342B (en) Hydrazine decomposition catalyst device of taking a trial run
CN214887619U (en) Water pump test system
CN215065156U (en) Pressure self-adaptive adjusting device for flexible inflation wind tunnel test model
CN111442876B (en) Intelligent transmitter checking system
CN213590410U (en) Solution positive pressure metering and conveying system
CN114082362A (en) Automatic gas distribution device and method for mixed gas
CN111122151B (en) Breather valve flow testing device and testing method thereof
CN210690061U (en) 1N single-component thruster test system
CN209783837U (en) multi-medium leakage rate adjustable leakage rate calibration system
CN108789777B (en) Pressure filling foam device and method for hollow material
RU2668628C1 (en) Method of consumption characteristics control for differential-safety devices and installation for method implementation
CN108152447B (en) Hydrazine decomposition catalyst test run device and method thereof

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant