CN203842339U - Automatic steam pressure stabilizing control device of methanol rectification system - Google Patents
Automatic steam pressure stabilizing control device of methanol rectification system Download PDFInfo
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- CN203842339U CN203842339U CN201420170719.5U CN201420170719U CN203842339U CN 203842339 U CN203842339 U CN 203842339U CN 201420170719 U CN201420170719 U CN 201420170719U CN 203842339 U CN203842339 U CN 203842339U
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Abstract
The utility model belongs to the technical field of automatic steam pressure stabilization, and particularly relates to an automatic steam pressure stabilizing control device of a methanol rectification system. The device comprises a methanol rectification pipeline, a steam working pipeline and a microcomputer control system, wherein the methanol rectification pipeline comprises a crude methanol pipeline which is connected with an inlet in the upper part of a pre-rectification tower through a crude methanol feeding regulating valve, an air phase outlet in the top of the pre-rectification tower is connected with a reflux tank of the pre-rectification tower through a pipeline, the reflux tank of the pre-rectification tower is connected with a pre-rectification tower reflux inlet in the upper part of the pre-rectification tower through a reflux pump, the steam working pipeline comprises a medium pressure steam pipeline and a low pressure steam pipeline, and the steam microcomputer control system comprises a model prediction controller which is connected with a data communication system (DCS) main control card. The automatic steam pressure stabilizing control device has the advantages that the low pressure steam is furthest utilized, the use level of medium pressure steam is saved, the load of the device can be timely adjusted, the steam is reasonably utilized, and the steam consumption is reduced.
Description
Technical field
The utility model belongs to steam automatic voltage regulation technical field, is specifically related to a kind of methanol fractionation system steam automatic voltage stabilization and control device.
Background technology
In nitrogenous fertilizer system, the production that utilizes the unnecessary heat of system to carry out byproduct is general.Methanol fractionation system is to utilize the low-quality steam that thermoelectric plant is come to carry out distillation process, but owing to being utilization to system waste heat, its low-pressure steam calorific value is inadequate, needs a certain amount of middle pressure steam of dispensing.But only using middle pressure steam is a kind of significant wastage to low-pressure steam.In steam use procedure, two-way steam can impact rectifier unit due to the load fluctuation of upper workshop section, causes each tower temperature sharply to change, and affects product quality simultaneously, and steam consumption also increases.
Summary of the invention
The purpose of this utility model is to overcome defect of the prior art, and provide a kind of middle pressure steam and low-pressure steam pressure of can automatically detecting to change, two bursts of steam sequencing valve apertures are controlled, use to greatest extent low-pressure steam, save middle pressure steam use amount, adjusting device load, reaches and rationally utilizes steam in good time, reduces the methanol fractionation system steam automatic voltage stabilization and control device of steam consumption.
The purpose of this utility model is achieved in that and comprises methanol rectification pipeline, steam working line and Control System of Microcomputer,
A, methanol rectification pipeline comprises that thick methyl alcohol pipeline is connected with the import on pre-rectifying tower top by thick alcohol charging control valve, the gaseous phase outlet at pre-rectifying tower top is connected with pre-rectifying tower backflash by pipeline, pre-rectifying tower backflash is connected with the pre-rectifying tower refluxing opening on pre-rectifying tower top by reflux pump, described pre-rectifying tower bottom is provided with pre-rectifying tower the first liquid-phase outlet and the outlet of pre-rectifying tower second liquid phase, pre-rectifying tower the first liquid-phase outlet is connected with the import at pre-rectifying tower middle part by the tube side of pre-rectifying tower reboiler, the outlet of pre-rectifying tower second liquid phase is connected with the import at pressurizing tower middle part by pipeline, the gaseous phase outlet at pressurizing tower top is connected with the import of pressurizing tower backflash by the shell side of atmospheric tower reboiler, pressurizing tower backflash is provided with the first outlet of pressurizing tower backflash and the second outlet of pressurizing tower backflash, the first outlet of pressurizing tower backflash is connected with the pressurizing tower refluxing opening on pressurizing tower top by pressurizing tower return flow meter, the second outlet of pressurizing tower backflash is connected with product storage tank with pressurizing tower extraction flowmeter by pressurizing tower extraction flow control valve, pressurizing tower bottom is provided with pressurizing tower the first liquid-phase outlet and the outlet of pressurizing tower second liquid phase, pressurizing tower the first liquid-phase outlet is connected with the import of pressurizing tower middle and lower part by the tube side of pressurizing tower reboiler, the outlet of pressurizing tower second liquid phase is connected with the import at atmospheric tower middle part by Liquid level adjusting valve at the bottom of pressurizing tower tower, the gaseous phase outlet at atmospheric tower top is connected with the import of atmospheric tower backflash by pipeline, atmospheric tower backflash is provided with the first outlet of atmospheric tower backflash and the second outlet of atmospheric tower backflash, the first outlet of atmospheric tower backflash is connected with the atmospheric tower refluxing opening on atmospheric tower top with atmospheric tower return flow meter by atmospheric tower return valve, the second outlet of atmospheric tower backflash is connected with product storage tank with atmospheric tower extraction flowmeter by atmospheric tower extraction flow control valve, atmospheric tower bottom is provided with atmospheric tower the first liquid-phase outlet and the outlet of atmospheric tower second liquid phase, atmospheric tower the first liquid-phase outlet is connected with the import of atmospheric tower middle and lower part by the tube side of atmospheric tower reboiler, the outlet of atmospheric tower second liquid phase is connected with thermoelectricity combustion pipe, the bottom of described pre-rectifying tower is provided with pre-rectifying tower column bottom temperature sensor, the bottom of pre-rectifying tower is provided with liquid level gauge at the bottom of pre-rectifying tower tower, the bottom of described pre-rectifying tower backflash is provided with pre-rectifying tower backflash liquid level gauge, the top of pressurizing tower is provided with pressurizing tower tower top temperature sensor, the bottom of pressurizing tower is provided with pressurizing tower column bottom temperature sensor, the top of atmospheric tower is provided with atmospheric tower tower top temperature sensor, and the bottom of atmospheric tower is provided with atmospheric tower column bottom temperature sensor,
B, steam working line comprises Medium Pressure Steam Pipeline and low-pressure steam pipeline, Medium Pressure Steam Pipeline is connected with steam buffer tank respectively with low-pressure steam pipeline, the steam (vapor) outlet of steam buffer tank top is connected with the shell side import of pre-rectifying tower reboiler by pipeline, between the shell side import of steam (vapor) outlet and pre-rectifying tower reboiler, be provided with threeway, threeway first end is connected with steam (vapor) outlet, threeway the second end is connected with the shell side import of pre-rectifying tower reboiler by pipeline, threeway the 3rd end is connected with the shell side import of pressurizing tower reboiler by pipeline, the shell side outlet of pre-rectifying tower reboiler and the shell side outlet of pressurizing tower reboiler are connected with condensate draining by pipeline respectively, between described Medium Pressure Steam Pipeline and steam buffer tank, be provided with middle pressure steam control valve, middle pressure steam pressure sensor and middle pressure steam temperature sensor, between described low-pressure steam pipeline and steam buffer tank, be provided with low-pressure steam control valve, low-pressure steam pressure sensor and low-pressure steam temperature sensor, pipeline between described threeway the second end and the shell side import of pre-rectifying tower reboiler is provided with pre-rectifying tower tower bottom steam control valve, pipeline between threeway the 3rd end and the shell side import of pressurizing tower reboiler is provided with pressurizing tower tower bottom steam control valve, described steam buffer tank top is provided with steam buffer pressure tank sensor and steam buffer tank temperature sensor,
C, Control System of Microcomputer comprises model predictive controller, model predictive controller and DCS main controller, described DCS main controller is connected with DCS database, described DCS database respectively with steam buffer pressure tank sensor, pre-rectifying tower backflash liquid level gauge, pre-rectifying tower column bottom temperature sensor, liquid level gauge at the bottom of pre-rectifying tower tower, atmospheric tower tower top temperature sensor, atmospheric tower column bottom temperature sensor, pressurizing tower tower top temperature sensor, pressurizing tower column bottom temperature sensor, pressurizing tower return flow meter, pressurizing tower extraction flowmeter, atmospheric tower return flow meter and atmospheric tower extraction flowmeter, described DCS main controller respectively with Liquid level adjusting valve and pressurizing tower tower bottom steam control valve, atmospheric tower extraction flow control valve and pressurizing tower extraction flow control valve at the bottom of middle pressure steam control valve, pre-rectifying tower tower bottom steam control valve, thick alcohol charging control valve, atmospheric tower return valve, pressurizing tower tower.
The utility model is by arranging steam buffer tank and various checkout gear, can either realize the pressure of stabilizing low voltage steam and middle pressure steam, fluctuation that again can look-ahead steam, make pre-rectifying tower reboiler and pressurizing tower reboiler steam regulation charging valve position in time, reach steam saving, the object of product quality is produced and guaranteed to stabilising arrangement, make smart alcohol per ton consume quantity of steam and be reduced to 0.72t by 0.75t, take that to produce 100000 tons of smart alcohol per year be example, every year can steam saving cost approximately 450,000 yuan, concrete computational process is: (smart alcohol originally per ton consumes the present smart alcohol per ton of quantity of steam 0.75t-and consumes quantity of steam 0.72t) * (produce 100000 tons of smart alcohol output 10 * 10 per year
4) * (steam average price 150t/ unit)=450,000 yuan, have and can automatically detect middle pressure steam and the variation of low-pressure steam pressure, low-pressure steam and middle pressure steam sequencing valve aperture are controlled, use to greatest extent low-pressure steam, save middle pressure steam use amount, adjusting device load, reaches and rationally utilizes steam in good time, reduces the advantage of steam consumption.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model;
Fig. 2 is the utility model Control System of Microcomputer frame principle figure.
The specific embodiment
As shown in Figure 1, 2, the utility model comprises methanol rectification pipeline, steam working line and Control System of Microcomputer,
A, methanol rectification pipeline comprises that thick methyl alcohol pipeline 1 is connected with the import on pre-rectifying tower 3 tops by thick alcohol charging control valve 2, the gaseous phase outlet at pre-rectifying tower 3 tops is connected with pre-rectifying tower backflash 4 by pipeline, pre-rectifying tower backflash 4 is connected with the pre-rectifying tower refluxing opening 6 on pre-rectifying tower 3 tops by reflux pump 5, described pre-rectifying tower 3 bottoms are provided with pre-rectifying tower the first liquid-phase outlet 7 and pre-rectifying tower second liquid phase outlet 8, pre-rectifying tower the first liquid-phase outlet 7 is connected with the import at pre-rectifying tower 3 middle parts by the tube side of pre-rectifying tower reboiler 15, pre-rectifying tower second liquid phase outlet 8 is connected with the import at pressurizing tower 9 middle parts by pipeline, the gaseous phase outlet at pressurizing tower 9 tops is connected with the import of pressurizing tower backflash 11 by the shell side of atmospheric tower reboiler 10, pressurizing tower backflash 11 is provided with the first outlet 12 of pressurizing tower backflash and the second outlet 13 of pressurizing tower backflash, the first outlet 12 of pressurizing tower backflash is connected with the pressurizing tower refluxing opening 21 on pressurizing tower top by pressurizing tower return flow meter 14, the second outlet 13 of pressurizing tower backflash is connected with product storage tank 44 with pressurizing tower extraction flowmeter 43 by pressurizing tower extraction flow control valve 25, pressurizing tower 9 bottoms are provided with pressurizing tower the first liquid-phase outlet 16 and pressurizing tower second liquid phase outlet 17, pressurizing tower the first liquid-phase outlet 16 is connected with the import of pressurizing tower 9 middle and lower parts by the tube side of pressurizing tower reboiler 18, the outlet 17 of pressurizing tower second liquid phase is connected with the import at atmospheric tower 19 middle parts by Liquid level adjusting valve 45 at the bottom of pressurizing tower tower, the gaseous phase outlet at atmospheric tower 19 tops is connected with the import of atmospheric tower backflash 20 by pipeline, atmospheric tower backflash 20 is provided with the first outlet of atmospheric tower backflash and the second outlet of atmospheric tower backflash, the first outlet of atmospheric tower backflash is connected with the atmospheric tower refluxing opening 22 on atmospheric tower 19 tops with atmospheric tower return flow meter 47 by atmospheric tower return valve 46, the second outlet of atmospheric tower backflash is connected with product storage tank 44 with atmospheric tower extraction flowmeter 49 by atmospheric tower extraction flow control valve 48, atmospheric tower 19 bottoms are provided with atmospheric tower the first liquid-phase outlet 23 and atmospheric tower second liquid phase outlet 24, atmospheric tower the first liquid-phase outlet 23 is connected with the import of atmospheric tower 19 middle and lower parts by the tube side of atmospheric tower reboiler 10, atmospheric tower second liquid phase outlet 24 is connected with thermoelectricity combustion pipe 26, the bottom of described pre-rectifying tower 3 is provided with pre-rectifying tower column bottom temperature sensor 50, the bottom of pre-rectifying tower 3 is provided with liquid level gauge 51 at the bottom of pre-rectifying tower tower, the bottom of described pre-rectifying tower backflash 4 is provided with pre-rectifying tower backflash liquid level gauge 52, the top of pressurizing tower 9 is provided with pressurizing tower tower top temperature sensor 53, the bottom of pressurizing tower 9 is provided with pressurizing tower column bottom temperature sensor 54, the top of atmospheric tower 19 is provided with atmospheric tower tower top temperature sensor 55, and the bottom of atmospheric tower 19 is provided with atmospheric tower column bottom temperature sensor 56,
B, steam working line comprises Medium Pressure Steam Pipeline 27 and low-pressure steam pipeline 28, Medium Pressure Steam Pipeline 27 is connected with steam buffer tank 29 respectively with low-pressure steam pipeline 28, the steam (vapor) outlet 30 at steam buffer tank 29 tops is connected with the shell side import of pre-rectifying tower reboiler 15 by pipeline, between the shell side import of steam (vapor) outlet 30 and pre-rectifying tower reboiler 15, be provided with threeway, threeway first end is connected with steam (vapor) outlet 30, threeway the second end is connected with the shell side import of pre-rectifying tower reboiler 15 by pipeline, threeway the 3rd end is connected with the shell side import of pressurizing tower reboiler 18 by pipeline, the shell side outlet of pre-rectifying tower reboiler 15 and the shell side outlet of pressurizing tower reboiler 18 are connected with condensate draining 31 by pipeline respectively, between described Medium Pressure Steam Pipeline 27 and steam buffer tank 29, be provided with middle pressure steam control valve 32, middle pressure steam pressure sensor 33 and middle pressure steam temperature sensor 34, between described low-pressure steam pipeline 28 and steam buffer tank 29, be provided with low-pressure steam control valve 35, low-pressure steam pressure sensor 36 and low-pressure steam temperature sensor 37, pipeline between described threeway the second end and the shell side import of pre-rectifying tower reboiler 15 is provided with pre-rectifying tower tower bottom steam control valve 38, pipeline between threeway the 3rd end and the shell side import of pressurizing tower reboiler 18 is provided with pressurizing tower tower bottom steam control valve 40, described steam buffer tank 29 tops are provided with steam buffer pressure tank sensor 41 and steam buffer tank temperature sensor 42,
C, Control System of Microcomputer comprises model predictive controller 57, model predictive controller 57 and DCS main controller 58, described DCS main controller 58 is connected with DCS database 39, described DCS database 39 respectively with steam buffer pressure tank sensor 41, pre-rectifying tower backflash liquid level gauge 52, pre-rectifying tower column bottom temperature sensor 50, at the bottom of pre-rectifying tower tower, liquid level gauge 51, atmospheric tower tower top temperature sensor 55, atmospheric tower column bottom temperature sensor 56, pressurizing tower tower top temperature sensor 53, pressurizing tower column bottom temperature sensor 54, pressurizing tower return flow meter 14, pressurizing tower extraction flowmeter 43, atmospheric tower return flow meter 47 and atmospheric tower extraction flowmeter 49, described DCS main controller 58 respectively with Liquid level adjusting valve 45 and pressurizing tower tower bottom steam control valve 40, atmospheric tower extraction flow control valve 48 and pressurizing tower extraction flow control valve 25 at the bottom of middle pressure steam control valve 32, pre-rectifying tower tower bottom steam control valve 38, thick alcohol charging control valve 2, atmospheric tower return valve 46, pressurizing tower tower.
A kind of control method of methanol fractionation system steam automatic voltage stabilization and control device, this control method comprises the control method of steam buffer pressure tank, the control method of pre-rectifying tower return tank liquid level, the control method of pre-rectifying tower column bottom temperature, the control method of liquid level at the bottom of pre-rectifying tower tower, the control method of atmospheric tower tower top temperature, the control method of atmospheric tower column bottom temperature, the control method of pressurizing tower tower top temperature and pressurization column bottom temperature, the control method of the control method of atmospheric tower reflux ratio and pressurizing tower reflux ratio;
A, steam buffer pressure tank control method comprise the steps:
One, steam buffer pressure tank sensor 41 detects the pressure of steam buffer tank, and the normally-pressured neighbor of steam buffer tank 29 is between 0.28～0.32MPa, and now low-pressure steam control valve 35 is in full-gear, and the aperture of middle pressure steam control valve 32 is 40%;
Two, steam buffer pressure tank sensor 41 detects the pressure of steam buffer tank, the pressure of steam buffer tank 29 is during lower than 0.28MPa, steam buffer pressure tank sensor 41 feeds back to DCS database 39 by the pressure data of steam buffer tank 29, DCS database 39 by DCS main controller 58 by data feedback to model predictive controller 57;
Three, will in step 2, feed back to after the data analysis of model predictive controller 57, model predictive controller 57 is controlled middle pressure steam control valve 32 by DCS main controller 58, by middle pressure steam control valve 32 aperture in step 1, be that 40% to adjust to aperture be 70%, make the pressure rise of steam buffer tank 29 to 0.28MPa; When the pressure rise of steam buffer tank 29 is during to 0.28MPa, model predictive controller 57 makes the aperture of middle pressure steam control valve 32 adjust to 40% by DCS main controller 58;
Four, steam buffer pressure tank sensor 41 detects the pressure of steam buffer tank, the pressure of steam buffer tank 29 is during higher than 0.32MPa, steam buffer pressure tank sensor 41 feeds back to DCS database 39 by the pressure data of steam buffer tank 29, DCS database 39 by DCS main controller 58 by data feedback to model predictive controller 57;
Five, will in step 4, feed back to after the data analysis of model predictive controller 57, model predictive controller 57 is controlled middle pressure steam control valve 32 by DCS main controller 58, by middle pressure steam control valve 32 aperture in step 1, be that 40% to adjust to aperture be 20%, make the pressure drop of steam buffer tank 29 to 0.32MPa; When the pressure drop of steam buffer tank 29 is during to 0.32MPa, model predictive controller 57 makes the aperture of middle pressure steam control valve 32 adjust to 40% by DCS main controller 58;
B, pre-rectifying tower return tank liquid level controlling method comprise the steps:
One, pre-rectifying tower backflash liquid level gauge 52 detects the liquid level of pre-rectifying tower backflash 4, and the liquid level normal range (NR) of pre-rectifying tower backflash 4 is between 100～120mm, and now the aperture of pre-rectifying tower tower bottom steam control valve 38 is 19%;
Two, pre-rectifying tower backflash liquid level gauge 52 detects the liquid level of pre-rectifying tower backflash 4, when the liquid level of pre-rectifying tower backflash 4 is during lower than 100mm, pre-rectifying tower backflash liquid level gauge 52 feeds back to DCS database 39 by the liquid level data in pre-rectifying tower backflash 4, DCS database 39 by DCS main controller 58 by data feedback to model predictive controller 57;
Three, will in step 2, feed back to after the data analysis of model predictive controller 57, model predictive controller 57 is controlled pre-rectifying tower tower bottom steam control valve 38 by DCS main controller 58, by pre-rectifying tower tower bottom steam control valve 38 aperture in above-mentioned steps one, be that 19% to adjust to aperture be 17%, the liquid level of pre-rectifying tower backflash 4 is risen to after 100mm, and model predictive controller 57 makes the aperture of pre-rectifying tower tower bottom steam control valve 38 adjust to 19% by DCS main controller 58;
Four, pre-rectifying tower backflash liquid level gauge 52 detects the liquid level of pre-rectifying tower backflash 4, when the liquid level of pre-rectifying tower backflash 4 is during higher than 120mm, pre-rectifying tower backflash liquid level gauge 52 feeds back to DCS database 39 by the liquid level data in pre-rectifying tower backflash 4, DCS database 39 by DCS main controller 58 by data feedback to model predictive controller 57;
Five, will in step 4, feed back to after the data analysis of model predictive controller 57, model predictive controller 57 is controlled pre-rectifying tower tower bottom steam control valve 38 by DCS main controller 58, by pre-rectifying tower tower bottom steam control valve 38 aperture in above-mentioned steps one, be that 19% to adjust to aperture be 23%, the liquid level of pre-rectifying tower backflash 4 is dropped to after 120mm, and model predictive controller 57 makes the aperture of pre-rectifying tower tower bottom steam control valve 38 adjust to 19% by DCS main controller 58;
C, pre-rectifying tower column bottom temperature control method comprise the steps:
One, the temperature at the bottom of pre-rectifying tower column bottom temperature sensor 50 detection pre-rectifying tower 3 towers, the temperature normal range (NR) at the bottom of pre-rectifying tower 3 towers is between 74～75 ℃, now the aperture of pre-rectifying tower tower bottom steam control valve 38 is 19%;
Two, the temperature at the bottom of pre-rectifying tower column bottom temperature sensor 50 detection pre-rectifying tower 3 towers, when the temperature at the bottom of pre-rectifying tower 3 towers is during lower than 74 ℃, the temperature data of pre-rectifying tower column bottom temperature sensor 50 at the bottom of by pre-rectifying tower 3 towers feeds back to DCS database 39, DCS database 39 by DCS main controller 58 by data feedback to model predictive controller 57;
Three, will in step 2, feed back to after the data analysis of model predictive controller 57, model predictive controller 57 is controlled pre-rectifying tower tower bottom steam control valve 38 by DCS main controller 58, by pre-rectifying tower tower bottom steam control valve 38 aperture in above-mentioned steps one, be that 19% to adjust to aperture be 19.8%, temperature at the bottom of pre-rectifying tower 3 towers is risen to after 74 ℃, and model predictive controller 57 makes the aperture of pre-rectifying tower tower bottom steam control valve 38 adjust to 19% by DCS main controller 58;
Four, the temperature at the bottom of pre-rectifying tower column bottom temperature sensor 50 detection pre-rectifying tower 3 towers, when the temperature at the bottom of pre-rectifying tower 3 towers is during higher than 75 ℃, the temperature data of pre-rectifying tower column bottom temperature sensor 50 at the bottom of by pre-rectifying tower 3 towers feeds back to DCS database 39, DCS database 39 by DCS main controller 58 by data feedback to model predictive controller 57;
Five, will in step 4, feed back to after the data analysis of model predictive controller 57, model predictive controller 57 is controlled pre-rectifying tower tower bottom steam control valve 38 by DCS main controller 58, by pre-rectifying tower tower bottom steam control valve 38 aperture in above-mentioned steps one, be that 19% to adjust to aperture be 18.5%, temperature at the bottom of pre-rectifying tower 3 towers is dropped to after 75 ℃, and model predictive controller 57 makes the aperture of pre-rectifying tower tower bottom steam control valve 38 adjust to 19% by DCS main controller 58;
At the bottom of d, pre-rectifying tower tower, liquid level controlling method comprises the steps:
One, the liquid level of liquid level gauge 51 detection pre-rectifying towers 3 at the bottom of pre-rectifying tower tower, the liquid level normal range (NR) of pre-rectifying tower 3 is between 100～120mm, now the aperture of thick alcohol charging control valve 2 is 58%;
Two, the liquid level of liquid level gauge 51 detection pre-rectifying towers 3 at the bottom of pre-rectifying tower tower, when the liquid level of pre-rectifying tower 3 is during lower than 100mm, at the bottom of pre-rectifying tower tower, liquid level gauge 51 feeds back to DCS database 39 by the liquid level data in pre-rectifying tower 3, DCS database 39 by DCS main controller 58 by data feedback to model predictive controller 57;
Three, will in step 2, feed back to after the data analysis of model predictive controller 57, model predictive controller 57 is controlled thick alcohol charging control valve 2 by DCS main controller 58, by thick alcohol charging control valve 2 aperture in above-mentioned steps one, be that 58% to adjust to aperture be 67%, the liquid level of pre-rectifying tower 3 is risen to after 100mm, and model predictive controller 57 makes the aperture of thick alcohol charging control valve 2 adjust to 58% by DCS main controller 58;
Four, the liquid level of liquid level gauge 51 detection pre-rectifying towers 3 at the bottom of pre-rectifying tower tower, when the liquid level of pre-rectifying tower 3 is during higher than 120mm, at the bottom of pre-rectifying tower tower, liquid level gauge 51 feeds back to DCS database 39 by the liquid level data in pre-rectifying tower 3, DCS database 39 by DCS main controller 58 by data feedback to model predictive controller 57;
Five, will in step 4, feed back to after the data analysis of model predictive controller 57, model predictive controller 57 is controlled thick alcohol charging control valve 2 by DCS main controller 58, by thick alcohol charging control valve 2 aperture in above-mentioned steps one, be that 58% to adjust to aperture be 55%, the liquid level of pre-rectifying tower backflash 4 is dropped to after 120mm, and model predictive controller 57 makes the aperture of thick alcohol charging control valve 2 adjust to 58% by DCS main controller 58;
E, atmospheric tower tower top temperature control method comprise the steps:
One, atmospheric tower tower top temperature sensor 55 detects the temperature of atmospheric tower 19 tower tops, and the temperature normal range (NR) of atmospheric tower 19 tower tops is between 67～70 ℃, and now the aperture of atmospheric tower return valve 46 is 53%;
Two, atmospheric tower tower top temperature sensor 55 detects the temperature of atmospheric tower 19 tower tops, when the temperature of atmospheric tower 19 tower tops is during lower than 67 ℃, atmospheric tower tower top temperature sensor 55 feeds back to DCS database 39 by the temperature data of atmospheric tower 19 tower tops, DCS database 39 by DCS main controller 58 by data feedback to model predictive controller 57;
Three, will in step 2, feed back to after the data analysis of model predictive controller 57, model predictive controller 57 is controlled atmospheric tower return valve 46 by DCS main controller 58, by atmospheric tower return valve 46 aperture in above-mentioned steps one, be that 53% to adjust to aperture be 50%, while making the temperature of atmospheric tower 19 tower tops rise to 67 ℃, model predictive controller 57 makes the aperture of atmospheric tower return valve 46 adjust to 53% by DCS main controller 58;
Four, atmospheric tower tower top temperature sensor 55 detects the temperature of atmospheric tower 19 tower tops, when the temperature of atmospheric tower 19 tower tops is during higher than 70 ℃, atmospheric tower tower top temperature sensor 55 feeds back to DCS database 39 by the temperature data of atmospheric tower 19 tower tops, DCS database 39 by DCS main controller 58 by data feedback to model predictive controller 57;
Five, will in step 4, feed back to after the data analysis of model predictive controller 57, model predictive controller 57 is controlled atmospheric tower return valve 46 by DCS main controller 58, by atmospheric tower return valve 46 aperture in above-mentioned steps one, be that 53% to adjust to aperture be 55%, the temperature of atmospheric tower 19 tower tops is dropped to after 70 ℃, and model predictive controller 57 makes the aperture of atmospheric tower return valve 46 adjust to 53% by DCS main controller 58;
F, atmospheric tower column bottom temperature control method comprise the steps:
One, the temperature at the bottom of atmospheric tower column bottom temperature sensor 56 detection atmospheric tower 19 towers, the temperature normal range (NR) at the bottom of atmospheric tower 19 towers is between 108～110 ℃, now at the bottom of pressurizing tower tower, the aperture of Liquid level adjusting valve 45 is 8%;
Two, the temperature at the bottom of atmospheric tower column bottom temperature sensor 56 detection atmospheric tower 19 towers, when the temperature at the bottom of atmospheric tower 19 towers is during lower than 108 ℃, the temperature data of atmospheric tower column bottom temperature sensor 56 at the bottom of by atmospheric tower 19 towers feeds back to DCS database 39, DCS database 39 by DCS main controller 58 by data feedback to model predictive controller 57;
Three, will in step 2, feed back to after the data analysis of model predictive controller 57, model predictive controller 57 is controlled Liquid level adjusting valve 45 at the bottom of pressurizing tower tower by DCS main controller 58, by the aperture in above-mentioned steps one of Liquid level adjusting valve 45 at the bottom of pressurizing tower tower, be that 8% to adjust to aperture be 2%, while making the temperature of atmospheric tower 19 tower tops rise to 108 ℃, model predictive controller 57 makes the aperture of Liquid level adjusting valve 45 at the bottom of pressurizing tower tower adjust to 8% by DCS main controller 58;
Four, the temperature at the bottom of atmospheric tower column bottom temperature sensor 56 detection atmospheric tower 19 towers, when the temperature at the bottom of atmospheric tower 19 towers is during higher than 110 ℃, the temperature data of atmospheric tower column bottom temperature sensor 56 at the bottom of by atmospheric tower 19 towers feeds back to DCS database 39, DCS database 39 by DCS main controller 58 by data feedback to model predictive controller 57;
Five, will in step 4, feed back to after the data analysis of model predictive controller 57, model predictive controller 57 is controlled Liquid level adjusting valve 45 at the bottom of pressurizing tower tower by DCS main controller 58, by the aperture in above-mentioned steps one of Liquid level adjusting valve 45 at the bottom of pressurizing tower tower, be that 8% to adjust to aperture be 10%, temperature at the bottom of atmospheric tower 19 towers is dropped to after 110 ℃, and model predictive controller 57 makes the aperture of Liquid level adjusting valve 45 at the bottom of pressurizing tower tower adjust to 8% by DCS main controller 58;
The control method of g, pressurizing tower tower top temperature and pressurization column bottom temperature comprises the steps:
One, pressurizing tower tower top temperature sensor 53 detects the temperature of pressurizing tower 9 tower tops, the temperature normal range (NR) of pressurizing tower 9 tower tops is between 118～121 ℃, pressurizing tower column bottom temperature sensor 54 detects the temperature at the bottom of pressurizing tower 9 towers, temperature normal range (NR) at the bottom of pressurizing tower 9 towers is between 126～130 ℃, wherein, when the temperature at the bottom of pressurizing tower 9 towers reduces, the temperature of pressurizing tower 9 tower tops is also along with reduction, when the temperature at the bottom of pressurizing tower 9 towers raises, the temperature of pressurizing tower 9 tower tops is also along with rising, and now the aperture of pressurizing tower tower bottom steam control valve 40 is 46%;
Two, pressurizing tower tower top temperature sensor 53 detects the temperature of pressurizing tower 9 tower tops, pressurizing tower column bottom temperature sensor 54 detects the temperature at the bottom of pressurizing tower 9 towers, when the temperature at the bottom of pressurizing tower 9 towers is during lower than 126 ℃, the temperature data of pressurizing tower column bottom temperature sensor 54 at the bottom of by pressurizing tower 9 towers feeds back to DCS database 39, DCS database 39 by DCS main controller 58 by data feedback to model predictive controller 57;
Three, will in step 2, feed back to after the data analysis of model predictive controller 57, model predictive controller 57 is controlled pressurizing tower tower bottom steam control valve 40 by DCS main controller 58, by pressurizing tower tower bottom steam control valve 40 aperture in above-mentioned steps one, be that 46% to adjust to aperture be 50%, while making temperature at the bottom of pressurizing tower 9 towers rise to 126 ℃, model predictive controller 57 makes the aperture of pressurizing tower tower bottom steam control valve 40 adjust to 46% by DCS main controller 58;
Four, pressurizing tower tower top temperature sensor 53 detects the temperature of pressurizing tower 9 tower tops, pressurizing tower column bottom temperature sensor 54 detects the temperature at the bottom of pressurizing tower 9 towers, when the temperature at the bottom of pressurizing tower tower is during higher than 130 ℃, the temperature data of pressurizing tower column bottom temperature sensor 54 at the bottom of by pressurizing tower 9 towers feeds back to DCS database 39, DCS database 39 by DCS main controller 58 by data feedback to model predictive controller 57;
Five, will in step 4, feed back to after the data analysis of model predictive controller 57, model predictive controller 57 is controlled pressurizing tower tower bottom steam control valve 40 by DCS main controller 58, by pressurizing tower tower bottom steam control valve 40 aperture in above-mentioned steps one, be that 46% to adjust to aperture be 40%, temperature at the bottom of pressurizing tower 9 towers is dropped to after 130 ℃, and model predictive controller 57 makes the aperture of Liquid level adjusting valve 45 at the bottom of pressurizing tower tower adjust to 46% by DCS main controller 58;
The control method of h, atmospheric tower reflux ratio comprises the steps:
One, the return flow of 47 pairs of atmospheric towers 19 of atmospheric tower return flow meter detects, the extraction flow of 49 pairs of atmospheric towers 19 of atmospheric tower extraction flowmeter detects, the normal ratio of the extraction flow of the return flow of above-mentioned atmospheric tower 19 and atmospheric tower 19 is between 1.0～1.3, and the aperture of now atmospheric tower extraction flow control valve 48 is 13.5%;
Two, the return flow of 47 pairs of atmospheric towers 19 of atmospheric tower return flow meter detects, the extraction flow of 49 pairs of atmospheric towers 19 of atmospheric tower extraction flowmeter detects, the return flow of atmospheric tower 19 with the ratio of the extraction flow of atmospheric tower 19 lower than 1.0 o'clock, the extraction data on flows of the return flow data of 47 pairs of atmospheric towers 19 of atmospheric tower return flow meter and 49 pairs of atmospheric towers 19 of atmospheric tower extraction flowmeter feeds back to respectively DCS database 39, DCS database 39 by DCS main controller 58 by data feedback to model predictive controller 57;
Three, will in step 2, feed back to after the data analysis of model predictive controller 57, model predictive controller 57 is controlled atmospheric tower extraction flow control valve 48 by DCS main controller 58, by atmospheric tower extraction flow control valve 48 aperture in above-mentioned steps one, be that 13.5% to adjust to aperture be 13%, the return flow of atmospheric tower 19 rises at 1.0 o'clock with the ratio of the extraction flow of atmospheric tower 19, and model predictive controller 57 makes the aperture of atmospheric tower extraction flow control valve 48 adjust to 13.5% by DCS main controller 58;
Four, the return flow of 47 pairs of atmospheric towers 19 of atmospheric tower return flow meter detects, the extraction flow of 49 pairs of atmospheric towers 19 of atmospheric tower extraction flowmeter detects, the return flow of atmospheric tower 19 with the ratio of the extraction flow of atmospheric tower 19 higher than 1.3 o'clock, the extraction data on flows of the return flow data of 47 pairs of atmospheric towers 19 of atmospheric tower return flow meter and 49 pairs of atmospheric towers 19 of atmospheric tower extraction flowmeter feeds back to respectively DCS database 39, DCS database 39 by DCS main controller 58 by data feedback to model predictive controller 57;
Five, will in step 4, feed back to after the data analysis of model predictive controller 57, model predictive controller 57 is controlled atmospheric tower extraction flow control valve 48 by DCS main controller 58, by atmospheric tower extraction flow control valve 48 aperture in above-mentioned steps one, be that 13.5% to adjust to aperture be 14%, the return flow of atmospheric tower 19 drops at 1.3 o'clock with the ratio of the extraction flow of atmospheric tower 19, and model predictive controller 57 makes the aperture of atmospheric tower extraction flow control valve 48 adjust to 13.5% by DCS main controller 58;
The control method of i, pressurizing tower reflux ratio comprises the steps:
One, the return flow of 14 pairs of pressurizing tower 9 of pressurizing tower return flow meter detects, the extraction flow of 43 pairs of pressurizing tower 9 of pressurizing tower extraction flowmeter detects, the normal ratio of the extraction flow of the return flow of above-mentioned pressurizing tower 9 and pressurizing tower 9 is between 2.6～2.8, and the aperture of now atmospheric tower extraction flow control valve 48 is 34%;
Two, the return flow of 14 pairs of pressurizing tower 9 of pressurizing tower return flow meter detects, the extraction flow of 43 pairs of pressurizing tower 9 of pressurizing tower extraction flowmeter detects, the return flow of pressurizing tower 9 with the ratio of the extraction flow of pressurizing tower 9 lower than 2.6 o'clock, the extraction data on flows of the return flow data of 14 pairs of pressurizing tower 9 of pressurizing tower return flow meter and 43 pairs of pressurizing tower 9 of pressurizing tower extraction flowmeter feeds back to respectively DCS database 39, DCS database 39 by DCS main controller 58 by data feedback to model predictive controller 57;
Three, will in step 2, feed back to after the data analysis of model predictive controller 57, model predictive controller 57 is controlled pressurizing tower extraction flow control valve 25 by DCS main controller 58, by pressurizing tower extraction flow control valve 25 aperture in above-mentioned steps one, be that 34% to adjust to aperture be 30%, the return flow of pressurizing tower 9 rises at 2.6 o'clock with the ratio of the extraction flow of pressurizing tower 9, and model predictive controller 57 makes the aperture of pressurizing tower extraction flow control valve 25 adjust to 34% by DCS main controller 58;
Four, the return flow of 14 pairs of pressurizing tower 9 of pressurizing tower return flow meter detects, the extraction flow of 43 pairs of pressurizing tower 9 of pressurizing tower extraction flowmeter detects, the return flow of pressurizing tower 9 with the ratio of the extraction flow of pressurizing tower 9 higher than 2.8 o'clock, the extraction data on flows of the return flow data of 14 pairs of pressurizing tower 9 of pressurizing tower return flow meter and 43 pairs of pressurizing tower 9 of pressurizing tower extraction flowmeter feeds back to respectively DCS database 39, DCS database 39 by DCS main controller 58 by data feedback to model predictive controller 57;
Five, will in step 4, feed back to after the data analysis of model predictive controller 57, model predictive controller 57 is controlled pressurizing tower extraction flowmeter 43 by DCS main controller 58, by pressurizing tower extraction flowmeter 43 aperture in above-mentioned steps one, be that 34% to adjust to aperture be 40%, the return flow of pressurizing tower 9 drops at 2.8 o'clock with the ratio of the extraction flow of pressurizing tower 9, and model predictive controller 57 makes the aperture of pressurizing tower extraction flow control valve 25 adjust to 3496 by DCS main controller 58.
Claims (1)
1. a methanol fractionation system steam automatic voltage stabilization and control device, this control device comprises methanol rectification pipeline, steam working line and Control System of Microcomputer, it is characterized in that:
A, methanol rectification pipeline comprises that thick methyl alcohol pipeline (1) is connected with the import on pre-rectifying tower (3) top by thick alcohol charging control valve (2), the gaseous phase outlet at pre-rectifying tower (3) top is connected with pre-rectifying tower backflash (4) by pipeline, pre-rectifying tower backflash (4) is connected with the pre-rectifying tower refluxing opening (6) on pre-rectifying tower (3) top by reflux pump (5), described pre-rectifying tower (3) bottom is provided with pre-rectifying tower the first liquid-phase outlet (7) and pre-rectifying tower second liquid phase outlet (8), pre-rectifying tower the first liquid-phase outlet (7) is connected with the import at pre-rectifying tower (3) middle part by the tube side of pre-rectifying tower reboiler (15), pre-rectifying tower second liquid phase outlet (8) is connected with the import at pressurizing tower (9) middle part by pipeline, the gaseous phase outlet at pressurizing tower (9) top is connected with the import of pressurizing tower backflash (11) by the shell side of atmospheric tower reboiler (10), pressurizing tower backflash (11) is provided with the first outlet (12) of pressurizing tower backflash and the second outlet (13) of pressurizing tower backflash, the first outlet (12) of pressurizing tower backflash is connected with the pressurizing tower refluxing opening (21) on pressurizing tower top by pressurizing tower return flow meter (14), the second outlet (13) of pressurizing tower backflash is connected with product storage tank (44) with pressurizing tower extraction flowmeter (43) by pressurizing tower extraction flow control valve (25), pressurizing tower (9) bottom is provided with pressurizing tower the first liquid-phase outlet (16) and pressurizing tower second liquid phase outlet (17), pressurizing tower the first liquid-phase outlet (16) is connected with the import of pressurizing tower (9) middle and lower part by the tube side of pressurizing tower reboiler (18), pressurizing tower second liquid phase outlet (17) is connected with the import at atmospheric tower (19) middle part by Liquid level adjusting valve (45) at the bottom of pressurizing tower tower, the gaseous phase outlet at atmospheric tower (19) top is connected with the import of atmospheric tower backflash (20) by pipeline, atmospheric tower backflash (20) is provided with the first outlet of atmospheric tower backflash and the second outlet of atmospheric tower backflash, the first outlet of atmospheric tower backflash is connected with the atmospheric tower refluxing opening (22) on atmospheric tower (19) top with atmospheric tower return flow meter (47) by atmospheric tower return valve (46), the second outlet of atmospheric tower backflash is connected with product storage tank (44) with atmospheric tower extraction flowmeter (49) by atmospheric tower extraction flow control valve (48), atmospheric tower (19) bottom is provided with atmospheric tower the first liquid-phase outlet (23) and atmospheric tower second liquid phase outlet (24), atmospheric tower the first liquid-phase outlet (23) is connected with the import of atmospheric tower (19) middle and lower part by the tube side of atmospheric tower reboiler (10), atmospheric tower second liquid phase outlet (24) is connected with thermoelectricity combustion pipe (26), the bottom of described pre-rectifying tower (3) is provided with pre-rectifying tower column bottom temperature sensor (50), the bottom of pre-rectifying tower (3) is provided with liquid level gauge (51) at the bottom of pre-rectifying tower tower, the bottom of described pre-rectifying tower backflash (4) is provided with pre-rectifying tower backflash liquid level gauge (52), the top of pressurizing tower (9) is provided with pressurizing tower tower top temperature sensor (53), the bottom of pressurizing tower (9) is provided with pressurizing tower column bottom temperature sensor (54), the top of atmospheric tower (19) is provided with atmospheric tower tower top temperature sensor (55), the bottom of atmospheric tower (19) is provided with atmospheric tower column bottom temperature sensor (56),
B, steam working line comprises Medium Pressure Steam Pipeline (27) and low-pressure steam pipeline (28), Medium Pressure Steam Pipeline (27) is connected with steam buffer tank (29) respectively with low-pressure steam pipeline (28), the steam (vapor) outlet (30) at steam buffer tank (29) top is connected with the shell side import of pre-rectifying tower reboiler (15) by pipeline, between the shell side import of steam (vapor) outlet (30) and pre-rectifying tower reboiler (15), be provided with threeway, threeway first end is connected with steam (vapor) outlet (30), threeway the second end is connected with the shell side import of pre-rectifying tower reboiler (15) by pipeline, threeway the 3rd end is connected with the shell side import of pressurizing tower reboiler (18) by pipeline, the shell side outlet of pre-rectifying tower reboiler (15) and the shell side outlet of pressurizing tower reboiler (18) are connected with condensate draining (31) by pipeline respectively, between described Medium Pressure Steam Pipeline (27) and steam buffer tank (29), be provided with middle pressure steam control valve (32), middle pressure steam pressure sensor (33) and middle pressure steam temperature sensor (34), between described low-pressure steam pipeline (28) and steam buffer tank (29), be provided with low-pressure steam control valve (35), low-pressure steam pressure sensor (36) and low-pressure steam temperature sensor (37), pipeline between described threeway the second end and the shell side import of pre-rectifying tower reboiler (15) is provided with pre-rectifying tower tower bottom steam control valve (38), pipeline between threeway the 3rd end and the shell side import of pressurizing tower reboiler (18) is provided with pressurizing tower tower bottom steam control valve (40), described steam buffer tank (29) top is provided with steam buffer pressure tank sensor (41) and steam buffer tank temperature sensor (42),
C, Control System of Microcomputer comprises model predictive controller (57), model predictive controller (57) and DCS main controller (58), described DCS main controller (58) is connected with DCS database (39), described DCS database (39) respectively with steam buffer pressure tank sensor (41), pre-rectifying tower backflash liquid level gauge (52), pre-rectifying tower column bottom temperature sensor (50), liquid level gauge at the bottom of pre-rectifying tower tower (51), atmospheric tower tower top temperature sensor (55), atmospheric tower column bottom temperature sensor (56), pressurizing tower tower top temperature sensor (53), pressurizing tower column bottom temperature sensor (54), pressurizing tower return flow meter (14), pressurizing tower extraction flowmeter (43), atmospheric tower return flow meter (47) and atmospheric tower extraction flowmeter (49), described DCS main controller (58) respectively with Liquid level adjusting valve (45) and pressurizing tower tower bottom steam control valve (40), atmospheric tower extraction flow control valve (48) and pressurizing tower extraction flow control valve (25) at the bottom of middle pressure steam control valve (32), pre-rectifying tower tower bottom steam control valve (38), thick alcohol charging control valve (2), atmospheric tower return valve (46), pressurizing tower tower.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420170719.5U CN203842339U (en) | 2014-04-10 | 2014-04-10 | Automatic steam pressure stabilizing control device of methanol rectification system |
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| CN201420170719.5U CN203842339U (en) | 2014-04-10 | 2014-04-10 | Automatic steam pressure stabilizing control device of methanol rectification system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103893988A (en) * | 2014-04-10 | 2014-07-02 | 河南心连心化肥有限公司 | Automatic pressure stabilizing control device for steam of methanol distillation system and control method of control device |
| CN114367118A (en) * | 2021-12-22 | 2022-04-19 | 泰兴金江化学工业有限公司 | Zirconium material reboiler for ethyl acetate production |
-
2014
- 2014-04-10 CN CN201420170719.5U patent/CN203842339U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103893988A (en) * | 2014-04-10 | 2014-07-02 | 河南心连心化肥有限公司 | Automatic pressure stabilizing control device for steam of methanol distillation system and control method of control device |
| CN103893988B (en) * | 2014-04-10 | 2015-09-23 | 河南心连心化肥有限公司 | Methanol fractionation system steam automatic voltage stabilization and control device and control method thereof |
| CN114367118A (en) * | 2021-12-22 | 2022-04-19 | 泰兴金江化学工业有限公司 | Zirconium material reboiler for ethyl acetate production |
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