CN103592930A - Energy-saving production method based on sugar factory refining system - Google Patents
Energy-saving production method based on sugar factory refining system Download PDFInfo
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Abstract
The invention discloses an energy-saving production method based on a sugar factory refining system. The energy-saving production method based on the sugar factory refining system comprises the steps of collecting the steam consuming parameters, material data and production state parameters of all steam consuming equipment in the sugar factory refining system, establishing steam consuming relevance mathematic expressions of all the steam consuming equipment, carrying out analysis and classification on the correlation of all production state variables, equipment state variables and process state variables and influential effects on the system, determining reigning strategic variables, establishing a mathematic model for system steam consumption and useful energy losses, searching a strategy meeting constraint conditions in the feasible domain of the mathematic model for the system steam consumption and the useful energy losses to enable the system steam consumption and the useful energy losses to acquire a minimum value, establishing a basic algorithm, carrying out programming based on the basic algorithm, completing strategic software, operating the strategic software to obtain an operation running scheme enabling the system steam consumption and the useful energy losses to acquire the minimum value, establishing a control network, and carrying out control over all the steam consuming equipment according to the operation running scheme enabling the system steam consumption and the useful energy losses to acquire the minimum value.
Description
Technical field
The present invention relates to energy-saving production method, especially a kind of energy-saving production method based on sugar refinery system refining system, belongs to sugar refinery system refining production field.
Background technology
The sugar of China is the necessity of people's lives, is also the important raw materials such as food industry, beverage, pharmacy.The growth of population and living standard improve, to there is the trend of rising appreciably in sugar consumption, sugar industry is China's waste water and the larger food industries of waste discharge amount, every ten thousand yuan of industrial outpuut energy consumptions of sugaring industry Ye Shi China, water consume one of the highest industry, the energy-saving horizontal in current domestic sugar refinery has been compared larger gap with Foreign Advanced Lerel, 6 tons/100 tons of average coal consumptions are more than sugarcane, are 2 times of the international advanced enterprises of 1.5Bei，Shi of international average level; Ton sugarcane power consumption 31.5 kilowatt hours are 1.6 times of international average level; According to the national Eleventh Five-Year Development Plan object of planning, require the Energy Intensity Reduction of CHINESE INDUSTRIES 20%, wherein require cane suger standard coal consumption lower than 5 tons/100 tons sugarcanes, beet sugar standard coal consumption is lower than 6 tons/100 tons beets.Although go into overdrive year by year in China's power consumption blowdown measure aspect, effect is also not obvious, and along with the increase of output, the energy consumption blowdown flow rate of China's sugaring industry constantly increases.The energy-saving and emission-reduction level of China has been compared larger gap with Foreign Advanced Lerel at present, China's sugaring industry is in the urgent need to carrying out energy-saving and emission-reduction in sugaring process, this is not only an urgent demand of sugar enterprise's self-growth, is also to realize industrial technology and integral level is in line with international standards and the needs of China's sustained economic development general requirement.
At present, domestic sugar refinery is all located in former revolutionary bases, minority-inhabited areas, frontier areas and poverty-stricken areas, and production scale is little, and technical equipment does not match, Automation of Manufacturing Process, information system management degree are low etc. be all cause energy consumption high, pollute heavy major reason.Within nearly 10 years, follow the significantly raising of domestic candy output, sugar industry technology also has large development, and the technical equipment sequential use of some energy-saving and emission-reduction, in production, has been brought into play positive role to reducing industry energy consumption.Sugaring is a longer production run of technological process, there is certain influence each unit to energy consumption, because front and back operation mutually restricts and affects at aspects such as material, energy, sugar refinery is energy-conservation is actually a systems engineering, and the low energy consumption of unit is not exclusively equal to the low energy consumption of whole production.Therefore,, how from system refining production angle unified planning energy, the device systems that makes sugar refinery system refine each link all completes production task with minimum energy consumption, thereby guarantees that whole production run runs on low energy consumption state, is the important topic of current research.
Summary of the invention
The object of the invention is in order to solve the defect of above-mentioned prior art, a kind of energy-saving production method based on sugar refinery system refining system is provided, the method is by the various parameter collection of each gas utilization unit in sugar refinery system refining production, analyze contrast, utilize computer networking technology operation to control, each gas utilization unit in sugar refinery system refining production is regulated and controled, can produce good energy-saving effect.
Object of the present invention can be by taking following technical scheme to reach:
An energy-saving production method based on sugar refinery system refining system, is characterized in that comprising the following steps:.
1) gather use vapour parameter, material data and the production status parameter of each gas utilization unit in the refining system processed of sugar refinery, and store;
2) according to sugar refinery system refining production process, to step 1) parameter that gathers analyzes, set up the associated mathematical expression of vapour for each gas utilization unit, to describe exergy loss related physical quantity transitivity parameter, the impact by vapour and exergy loss relation on system according to the physical parameter value under different conditions and related physical quantity, carries out related data analysis and judgement;
3) according to related data in associated mathematical expression, to the correlationship of various production status variablees, equipment state variable and process status variable and influence that system rises is analyzed and sorted out;
4) determine reigning decision variable, utilize the associated mathematical expression of exergy loss related physical quantity transitivity parameter, set up corresponding mathematical model equation, the operation operating scheme that arbitrary group of decision variable determined, set up the mathematical model of vapour and the available energy loss of energy for system, from this model, obtain a total exergy loss value of system corresponding with it;
5) by system, use the mathematical model of vapour and exergy loss to find a decision-making that meets constraint condition in the decision-making feasible zone of all set, make system obtain minimum value with vapour and exergy loss;
6) set up basic algorithm, to analyzing and contrast by vapour parameter, material data and production status parameter, decision variable is chosen certain value under constraint condition, carry out computing, basic algorithm is being determined the rational direction of search of next round after repeatedly relatively judging, to the rational direction of search, constantly carry out computing judgement, obtain compared with Rational Decision scheme;
7) according to basic algorithm, programme, complete decision-making software;
8) decision-making software operation, an aritrary decision of input gas utilization unit parameter, production status parameter and production, operation basic algorithm, obtains a system and obtains minimum value operation operating scheme with vapour and exergy loss;
9) set up and control network, according to system, with vapour and exergy loss, obtain minimum value operation operating scheme each gas utilization unit is carried out and controlled.
As a kind of preferred version, step 2) vapour and exergy loss relation for described system, comprise that exergy loss and vapour that the exergy loss on evaporator heat-transfer area, ducted exergy loss, condensation cause coagulate the exergy loss that water causes.The total exergy loss E of vapo(u)rization system
xcalculating can be expressed as:
E
x＝E
t+E
p+E
c+E
s
In formula, E
xfor vapo(u)rization system total exergy loss in the unit interval, kj/h; E
tfor system unit evaporator heat transfer exergy loss in the time, unit is kj/h; E
pfor the pipeline exergy loss of system unit time, unit is kj/h; E
cfor system unit total condensation exergy loss in the time, unit is kj/h; E
sfor the exergy loss that system condensing water causes, unit is kJ/h.
As a kind of preferred version, step 3) described production status variable comprises clearly juice flow, clear juice concentration, syrup flow, syrup concentration, sugar products quality and sugar products quantity; Described equipment state variable comprises well heater, evaporator and boiling pan heat transfer area; Described process status variable comprises saturated vapor temperature, the temperature of the solidifying water of vapour, each well heater heating-up temperature, each evaporator syrup hammer degree, each evaporator heating steam temperature, each evaporator heating steam flow, the solidifying discharge of each evaporator vapour, each boiling pan heating steam temperature, each boiling pan heating steam flow and the solidifying discharge of each boiling pan vapour.
4, a kind of energy-saving production method based on sugar refinery system refining system according to claim 2, is characterized in that: step 4) describedly with vapour and exergy loss mathematical model equation, be shown below:
In formula, Q
ibe i effect evaporator unit interval heat transfer capacity, kJ/h; T
dibe i effect evaporator heating stripping temperature, unit is ℃; T
gibe i effect evaporator juice stripping temperature, unit is ℃; W
ibe the evaporated water of unit interval in i evaporator, unit is kg/h; q
e, 5for the Zhi Qiliang， unit of extracting out from the 5th effect evaporator in the unit interval is kg/h; q
d, 1for the water yield of melting down in the unit interval, unit is kg/h; q
d, 5for the vapour condensate flow of discharging in the unit interval, unit is kg/h; h
5be the specific enthalpy of the 5th effect evaporator juice vapour, unit is kj/kg; s
5be the specific entropy of the 5th effect evaporator juice vapour, unit is kj/kg.k; h
5' be the specific enthalpy of the solidifying water of the 5th effect evaporator heating vapour vapour, unit is kj/kg; s
5' be the specific entropy of the solidifying water of the 5th effect evaporator heating vapour vapour, unit is kj/kg.k; T
0for environment temperature, unit is K; H0 is the specific enthalpy of water under ground state, and unit is kj/kg; s
0for the specific entropy of water under ground state, unit is kj/kgk.
As a kind of preferred version, described T
0value is 298K; Described h
0value is 104.77kjkg; Described s
0value is 0.367kj/kgk.
As a kind of preferred version, step 4) described decision variable is q
e, 1, q
e, 2, q
e, 3, q
e, 4and q
e, 5, its constraint condition comprises manufacturing condition, productive capacity and control index; q
e, 1, q
e, 2, q
e, 3, q
e, 4and q
e, 5be respectively the juice vapour amount of extracting out to the 5th effect evaporator from the 1st effect in the unit interval.
As a kind of preferred version, step 6) described by vapour and exergy loss mathematical model, the existing equality constraint of its constraint condition, has again inequation constraint, punishes function former problem is converted into a series of unconstrained problems separates by structure.
The present invention has following beneficial effect with respect to prior art:
1, energy-saving production method of the present invention adopts automatic control technology and computer networking technology, makes sugar refinery break away from the limitation of single equipment, to realizing concentrating by vapour situation in sugar refinery system refining production process, optimizes and controls, and saves the steam consumption of system refining production run.
2, energy-saving production method of the present invention is advanced by vapour analysis and judgment method, employing exergy loss is minimum, be that available energy utilization ratio is analyzed sugar refinery system refining vapour situation, grade with vapour thermal source and quantity are passed judgment on, compared with conventional energy conservation, only by number of heat source, how much passed judgment on accurately;
3, energy-saving production method of the present invention is by foundation system refining production run consumption vapour mathematical model, can construct available energy and concentrate optimal control program, can be according to producing real time status, obtain fast system refining vapour Optimal Parameters, instruct process steam operation, thereby realize the energy-saving and cost-reducing object in sugar refinery.
Accompanying drawing explanation
Fig. 1 is the structure principle chart of sugar refinery system refining system.
Fig. 2 is energy-saving production method schematic flow sheet of the present invention.
Fig. 3 is material of the present invention, vapour and condensate water process chart.
Embodiment
Embodiment 1:
As shown in Figure 1, sugar refinery refining system processed of the present embodiment comprises that central server, remote control module, system refining administration module, available energy optimum management module, communicator A, communicator B, controller A, controller B, system refining evaporation substation, system refiningly cook sugared substation, described controller A is connected with central server, system refining administration module, available energy optimum management module respectively by communicator A, controls system refining evaporation substation work; Described controller B is connected with central server, system refining administration module, available energy optimum management module by communicator B, and the system of control refiningly cooks the work of sugared substation.
As shown in Figure 1-Figure 3, the energy-saving production method of the present embodiment comprises the following steps:
1) gather system refining evaporation substation and system refiningly cook each gas utilization unit in sugared substation by vapour parameter, material data and production status parameter, and store;
2) according to sugar refinery system refining production process, to step 1) parameter that gathers analyzes, setting up each gas utilization unit uses the associated mathematical expression of vapour to describe exergy loss related physical quantity transitivity parameter, the impact by vapour and exergy loss relation on system according to the physical parameter value under different conditions and related physical quantity, carries out related data analysis and judgement; Vapour and exergy loss relation for described system, comprise that exergy loss and vapour that the exergy loss on evaporator heat-transfer area, ducted exergy loss, condensation cause coagulate the exergy loss that water causes.The total exergy loss E of vapo(u)rization system
xcalculating can be expressed as:
E
x＝E
t+E
p+E
c+E
s
In formula, E
xfor vapo(u)rization system total exergy loss in the unit interval, kJ/h; E
tfor system unit evaporator heat transfer exergy loss in the time, unit is kj/h; E
pfor the pipeline exergy loss of system unit time, unit is kj/h; E
cfor system unit total condensation exergy loss in the time, unit is kj/h; E
sfor the exergy loss that system condensing water causes, unit is kj/h;
3) according to related data in associated mathematical expression, to the correlationship of various production status variablees, equipment state variable and process status variable and influence that system rises is analyzed and sorted out, described production status variable comprises juice flow, clear juice concentration, syrup flow, syrup concentration clearly, sugar products quality and sugar products quantity; Described equipment state variable comprises well heater, evaporator and boiling pan heat transfer area; Described process status variable comprises saturated vapor temperature, the temperature of the solidifying water of vapour, each well heater heating-up temperature, each evaporator syrup hammer degree, each evaporator heating steam temperature, each evaporator heating steam flow, the solidifying discharge of each evaporator vapour, each boiling pan heating steam temperature, each boiling pan heating steam flow and the solidifying discharge of each boiling pan vapour;
4) in the refining of sugar refinery system, use in vapour and the closely-related variable of production operation, reigning is decision variable, once decision variable is definite, process status variable is also determined thereupon; Determine decision variable, utilize the associated mathematical expression of exergy loss related physical quantity transitivity parameter, set up corresponding mathematical model equation, the operation operating scheme that arbitrary group of decision variable determined, set up the mathematical model of vapour and exergy loss for system, from this model, obtain a total exergy loss value of system corresponding with value; Describedly with vapour and exergy loss mathematical model equation, be shown below:
In formula, Q
ibe i effect evaporator unit interval heat transfer capacity, kJ/h; T
dibe i effect evaporator heating stripping temperature, unit is ℃; T
gibe i effect evaporator juice stripping temperature, unit is ℃; W
ibe the evaporated water of unit interval in i evaporator, unit is kg/h; q
e, 5for the Zhi Qiliang， unit of extracting out from the 5th effect evaporator in the unit interval is kg/h; q
d, 1for the water yield of melting down in the unit interval, unit is kg/h; q
d, 5for the vapour condensate flow of discharging in the unit interval, unit is kg/h; h
5be the specific enthalpy of the 5th effect evaporator juice vapour, unit is kj/kg; s
5be the specific entropy of the 5th effect evaporator juice vapour, unit is kj/kg.k; h
5' be the specific enthalpy of the solidifying water of the 5th effect evaporator heating vapour vapour, unit is kj/kg; s
5' be the specific entropy of the solidifying water of the 5th effect evaporator heating vapour vapour, unit is kj/kg.k; T
0for environment temperature, unit is K, and value is 298K; h
0for the specific enthalpy of water under ground state, unit is kj/kg, and value is 104.77kj/kg; s
0for the specific entropy of water under ground state, unit is kj/kgk, and value is 0.367kj/kgk;
5) reigning decision variable must meet the technological requirement of sugar refinery system refining, it is restricted by the constraint condition of manufacturing condition, productive capacity and control index, decision variable changes between certain limit, they will meet the decision-making of constraint condition, are the decision-making feasible zones of all set; By system, use the mathematical model of vapour and exergy loss in feasible zone, to find a decision-making that meets constraint condition, make system obtain minimum value with vapour and exergy loss; Described decision variable is q
e, 1, q
e, 2, q
e, 3, q
e, 4and q
e, 5, q
e, 1, q
e, 2, q
e, 3, q
e, 4and q
e, 5be respectively the juice vapour amount of extracting out to the 5th effect evaporator from the 1st effect in the unit interval;
6) set up basic algorithm, to analyzing and contrast by vapour parameter, material data and production status parameter, decision variable is chosen certain value under the constraint condition of manufacturing condition, productive capacity and control index, carry out computing, basic algorithm is being determined the rational direction of search of next round after repeatedly relatively judging, to the rational direction of search, constantly carry out computing judgement, obtain compared with Rational Decision scheme; The existing equality constraint of described constraint condition, has again inequation constraint, punishes function former problem is converted into a series of unconstrained problems separates by structure;
7) according to basic algorithm, programme, complete decision-making software;
8) decision-making software operation, an aritrary decision of input gas utilization unit parameter, production status parameter and production, operation basic algorithm, obtains a system and obtains minimum value operation operating scheme, i.e. Optimization of Energy Saving scheme with vapour and exergy loss;
9) set up and control network, according to system, with vapour and exergy loss, obtain minimum value operation operating scheme each gas utilization unit is carried out and controlled, reach further energy-conservation object of sugar refinery system refining.
By material and energy balance are carried out in sugar refinery cane sugar factory system refining workshop, obtain basic system refining and use vapour scheme, result is as shown in table 1 below.
| Project | The 1st effect | The 2nd effect | The 3rd effect | The 4th effect | The 5th effect |
| Steam drum temperature/℃ | 129 | 120 | 111 | 100 | 84 |
| Steam chest temperature/℃ | 121 | 112 | 101 | 85 | 65 |
| Syrup hammer degree/° Bx | 25.36 | 40.33 | 51.14 | 61.46 | 65.00 |
| Effective temperature difference/℃ | 6.48 | 5.50 | 6.15 | 8.69 | 9.96 |
| Take out juice vapour amount/%C to sugarcane ratio | 14.41 | 15.71 | 3.27 | 4.00 | 1.48 (entering condenser) |
Table 1 cane sugar factory refining system vapour work sheet for distribution processed
Wherein, the clear juice hammer degree in calculating is 16 ° of Bx, and its temperature is 120 ℃; 65 ° of Bx of syrup hammer degree, its temperature is 65 ℃, 1 effect throttle flow is 38.87%C.
By system vapour and exergy loss relationship analysis, comprise that exergy loss and vapour that the exergy loss on evaporator heat-transfer area, ducted exergy loss, condensation cause coagulate the exergy loss that water causes.
To squeeze 3000 tons of cane sugar factory system refining workshops day, with vapour situation analysis and optimization method, be described further:
By above-mentioned formula and decision variable q
e, 1, q
e, 2, q
e, 3, q
e, 4, q
e, 5programme, the basic algorithm of the present embodiment adopts powell algorithm, and the available energy filtering out is by analysis allocated as follows shown in table 2.
Prioritization scheme table is controlled in the operation of table 2 evaporation section
From upper table 1 and table 2 result, can find out, through available energy, concentrate and optimize and adopt after powell algorithm, 5 effect vapo(u)rization system throttle (steam) temperatures are reduced to 127 ℃ by 129 ℃, the total throttle flow of system is reduced to 37.21%C by 38.87%C, final-effect juice steam temperature enters condenser juice stripping temperature is 71.4 ℃ by 65 ℃ of risings, it is 2.64%C that juice vapour amount is raise by 1.48%C, it is 18882524 kj/h that total exergy loss is raise by 16277108.53kj/h, but in available energy, transfer efficient brings up to 80.83% by 80.69%.Wherein exergy loss raise with actual evaporation tank heat transfer coefficient, pipeline heat radiation, enter condenser available energy etc. loss increase relevant, but for whole multi-effect evaporation system, the middle transfer efficient of available energy improves, total throttle flow is decreased, approximately reduce 1.66%C, amount to and save 132.8 tons of mark coal consumptions every day.
The energy-saving production method of the present embodiment adopts automatic control technology and computer networking technology, make sugar refinery break away from the limitation of single equipment, from sugar refinery system refining production system, consider energy distribution and the energy consumption possibility that becomes, sugar refinery system is refined main heating power workshop section and is linked together by Industrial Ethernet, realizes the networking of each main heating power workshop section and controls; Each workshop section's energy consumption related data is shared, by foundation system refining therrmodynamic system model, heating power scheme is carried out to tuning, network control system is carried out optimal control according to the heating power scheme of tuning to each unit, thereby sugar refinery system refining of assurance completes under the prerequisite of production task at existing equipment, run on minimum energy consumption state, make the operation of system refining therrmodynamic system efficient stable, reach further energy-conservation object.
The above; it is only patent preferred embodiment of the present invention; but the protection domain of patent of the present invention is not limited to this; anyly be familiar with those skilled in the art in the disclosed scope of patent of the present invention; according to the present invention, the technical scheme of patent and inventive concept thereof are equal to replacement or are changed, and all belong to the protection domain of patent of the present invention.
Claims (7)
1. based on sugar refinery system, refine an energy-saving production method for system, it is characterized in that comprising the following steps:
1) gather use vapour parameter, material data and the production status parameter of each gas utilization unit in the refining system processed of sugar refinery, and store;
2) according to sugar refinery system refining production process, to step 1) parameter that gathers analyzes, set up the associated mathematical expression of vapour for each gas utilization unit, to describe exergy loss related physical quantity transitivity parameter, the impact by vapour and exergy loss relation on system according to the physical parameter value under different conditions and related physical quantity, carries out related data analysis and judgement;
3) according to related data in associated mathematical expression, to the correlationship of various production status variablees, equipment state variable and process status variable and influence that system rises is analyzed and sorted out;
4) determine reigning decision variable, utilize the associated mathematical expression of exergy loss related physical quantity transitivity parameter, set up corresponding mathematical model equation, the operation operating scheme that arbitrary group of decision variable determined, set up the mathematical model of vapour and the available energy loss of energy for system, from this model, obtain a total exergy loss value of system corresponding with it;
5) by system, use the mathematical model of vapour and exergy loss to find a decision-making that meets constraint condition in the decision-making feasible zone of all set, make system obtain minimum value with vapour and exergy loss;
6) set up basic algorithm, to analyzing and contrast by vapour parameter, material data and production status parameter, decision variable is chosen certain value under constraint condition, carry out computing, basic algorithm is being determined the rational direction of search of next round after repeatedly relatively judging, to the rational direction of search, constantly carry out computing judgement, obtain compared with Rational Decision scheme;
7) according to basic algorithm, programme, complete decision-making software;
8) decision-making software operation, an aritrary decision of input gas utilization unit parameter, production status parameter and production, operation basic algorithm, obtains a system and obtains minimum value operation operating scheme with vapour and exergy loss;
9) set up and control network, according to system, with vapour and exergy loss, obtain minimum value operation operating scheme each gas utilization unit is carried out and controlled.
2. a kind of energy-saving production method based on sugar refinery system refining system according to claim 1, it is characterized in that: step 2) vapour and exergy loss relation for described system, comprise that exergy loss and vapour that the exergy loss on evaporator heat-transfer area, ducted exergy loss, condensation cause coagulate the exergy loss that water causes.The total exergy loss E of vapo(u)rization system
xcalculating can be expressed as:
E
x＝E
t+E
p+E
c+E
s
In formula, E
xfor vapo(u)rization system total exergy loss in the unit interval, kj/h; E
tfor system unit evaporator heat transfer exergy loss in the time, unit is kj/h; E
pfor the pipeline exergy loss of system unit time, unit is kj/h; E
cfor system unit total condensation exergy loss in the time, unit is kg/h; E
sfor the exergy loss that system condensing water causes, unit is kJ/h.
3. a kind of energy-saving production method based on sugar refinery system refining system according to claim 1, is characterized in that: step 3) described production status variable comprises juice flow, clear juice concentration, syrup flow, syrup concentration clearly, sugar products quality and sugar products quantity; Described equipment state variable comprises well heater, evaporator and boiling pan heat transfer area; Described process status variable comprises saturated vapor temperature, the temperature of the solidifying water of vapour, each well heater heating-up temperature, each evaporator syrup hammer degree, each evaporator heating steam temperature, each evaporator heating steam flow, the solidifying discharge of each evaporator vapour, each boiling pan heating steam temperature, each boiling pan heating steam flow and the solidifying discharge of each boiling pan vapour.
4. a kind of energy-saving production method based on sugar refinery system refining system according to claim 2, is characterized in that: step 4) describedly with vapour and exergy loss mathematical model equation, be shown below:
In formula, Q
ibe i effect evaporator unit interval heat transfer capacity, kJ/h; T
dibe i effect evaporator heating stripping temperature, unit is ℃; T
gibe i effect evaporator juice stripping temperature, unit is ℃; W
ibe the evaporated water of unit interval in i evaporator, unit is kg/h; q
e, 5for the Zhi Qiliang， unit of extracting out from the 5th effect evaporator in the unit interval is kg/h; q
d, 1for the water yield of melting down in the unit interval, unit is kg/h; q
d, 5for the vapour condensate flow of discharging in the unit interval, unit is kg/h; h
5be the specific enthalpy of the 5th effect evaporator juice vapour, unit is kj/kg; s
5be the specific entropy of the 5th effect evaporator juice vapour, unit is kj/kg.k; h
5' be the specific enthalpy of the solidifying water of the 5th effect evaporator heating vapour vapour, unit is kj/kg; s
5' be the specific entropy of the solidifying water of the 5th effect evaporator heating vapour vapour, unit is kj/kg.k; T
0for environment temperature, unit is K; h
0for the specific enthalpy of water under ground state, unit is kj/kg; s
0for the specific entropy of water under ground state, unit is kj/kgk.
5. a kind of energy-saving production method based on sugar refinery system refining system according to claim 4, is characterized in that: described T
0value is 298K; Described h
0value is 104.77kj/kg; Described s
0value is 0.367kj/kgk.
6. a kind of energy-saving production method based on sugar refinery system refining system according to claim 4, is characterized in that: step 4) described decision variable is q
e, 1, q
e, 2, q
e, 3, q
e, 4and q
e, 5, its constraint condition comprises manufacturing condition, productive capacity and control index; q
e, 1, q
e, 2, q
e, 3, q
e, 4and q
e, 5be respectively the juice vapour amount of extracting out to the 5th effect evaporator from the 1st effect in the unit interval.
7. a kind of energy-saving production method based on sugar refinery system refining system according to claim 1, it is characterized in that: step 6) described by vapour and exergy loss mathematical model, the existing equality constraint of its constraint condition, there is again inequation constraint, by structure, punish function and former problem is converted into a series of unconstrained problems separates.
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| CN110412960A (en) * | 2019-08-22 | 2019-11-05 | 广东省生物工程研究所（广州甘蔗糖业研究所） | Into squeezing and wisdom production management method and system are squeezed based on the sugar refinery of cloud computing |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110412960A (en) * | 2019-08-22 | 2019-11-05 | 广东省生物工程研究所（广州甘蔗糖业研究所） | Into squeezing and wisdom production management method and system are squeezed based on the sugar refinery of cloud computing |
| CN110412960B (en) * | 2019-08-22 | 2021-07-06 | 广东省生物工程研究所（广州甘蔗糖业研究所） | Intelligent squeezing and squeezing production management method and system for sugar refinery based on cloud computing |
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