CN105962005A - Energy-saving control method of twin-stage compression type heat pump vacuum freeze drying combined device - Google Patents
Energy-saving control method of twin-stage compression type heat pump vacuum freeze drying combined device Download PDFInfo
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- CN105962005A CN105962005A CN201610299893.3A CN201610299893A CN105962005A CN 105962005 A CN105962005 A CN 105962005A CN 201610299893 A CN201610299893 A CN 201610299893A CN 105962005 A CN105962005 A CN 105962005A
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- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
- A23L3/00—Preservation of foods or foodstuffs, in general, e.g. pasteurising, sterilising, specially adapted for foods or foodstuffs
- A23L3/40—Preservation of foods or foodstuffs, in general, e.g. pasteurising, sterilising, specially adapted for foods or foodstuffs by drying or kilning; Subsequent reconstitution
- A23L3/44—Freeze-drying
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B30/00—Heat pumps
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B5/00—Drying solid materials or objects by processes not involving the application of heat
- F26B5/04—Drying solid materials or objects by processes not involving the application of heat by evaporation or sublimation of moisture under reduced pressure, e.g. in a vacuum
- F26B5/06—Drying solid materials or objects by processes not involving the application of heat by evaporation or sublimation of moisture under reduced pressure, e.g. in a vacuum the process involving freezing
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P60/00—Technologies relating to agriculture, livestock or agroalimentary industries
- Y02P60/80—Food processing, e.g. use of renewable energies or variable speed drives in handling, conveying or stacking
- Y02P60/85—Food storage or conservation, e.g. cooling or drying
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- General Engineering & Computer Science (AREA)
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- Mechanical Engineering (AREA)
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- Polymers & Plastics (AREA)
- Thermal Sciences (AREA)
- Physics & Mathematics (AREA)
- Molecular Biology (AREA)
- Drying Of Solid Materials (AREA)
Abstract
The present invention relates to an energy-saving control method of a twin-stage compression type heat pump vacuum freeze drying combined device. The energy-saving control method of a control system is characterized by comprising the steps that according to the requirements of the food drying processes, temperature T1 of a heating medium entering drying chamber heating division plates is determined; according to the vacuum degree requirements of the combined device and the changes of the thickness of a frost layer on the surface of a water catcher in the operation process of the combined device, a functional expression of the change of an evaporation temperature T4 of the water catcher with an operation time t during the operation process of the combined device is determined; according to the evaporation temperature T4 of the water catcher in a low-pressure stage refrigeration system and a condensing temperature T2 of a high-pressure stage condenser, an optimum intermediate temperature T3 of an intercooler is determined; according to the functional expression of the change of the evaporator temperature T4 of the water catcher with the operation time t, the temperature is realized by adjusting the opening degree of a low-pressure stage throttle valve and the rotation speed of a low-pressure stage compressor; and according to the calculation of a functional expression, the optimal intermediate temperature T3 of the intercooler is determined and realized by adjusting the opening degree of a high-pressure stage throttle valve and the rotation speed of a high-pressure compressor. The advantages are as follows: the heat supply temperature and heat of the drying chamber can be adjusted, the optimum evaporation temperature of the water catcher can be determined, and the optimum intermediate temperature of the intercooler can be determined, and the combined device is energy-saving in operation.
Description
Technical field
The present invention relates to a kind of two-stage compression heat pump vacuum lyophilization unit equipment energy-saving control method.
Background technology
The food that vacuum freeze is dried is good relative to the food quality that other drying meanss are dried, but the course of processing
Middle energy consumption is big.During vacuum freeze runs, the water sublimed being on the one hand dried in food needs substantial amounts of heat, separately
On the one hand, moisture is sublimated in water vessel needs substantial amounts of cold.Owing to providing the refrigeration of cold for vacuum freeze
System is during refrigeration, and substantial amounts of heat released by its condenser, and this heat is more than food drying institute calorific requirement, because of
This, have researcher to propose to utilize refrigerant system condenser heat as food drying thermal source, thereby produce heat pump vacuum freezing
It is dried unit equipment.Unit equipment energy consumption in running is mainly refrigeration system energy consumption, the joint of unit equipment to be realized
Can, it is important under meeting the requirements such as food processing technology parameter such as hothouse heating-up temperature, vacuum, improve refrigeration as far as possible
The evaporating temperature of system.Due within a dry process-cycle food drying technique be change, its required refrigerating capacity and
Evaporating temperature is change, and institute's calorific requirement and heating-up temperature are also changes, and it is energy-conservation how Collaborative Control becomes unit equipment
Crucial.Simultaneously as hothouse heating needed for temperature typically at about 60 DEG C, refrigeration system evaporating temperature at about-40 DEG C,
Refrigeration system must use cascade refrigeration, two-stage compression refrigeration or air injection enthalpy-increasing refrigeration could meet requirement, but this also increases
The control difficulty of unit equipment.
Summary of the invention
It is an object of the invention to overcome the deficiencies in the prior art to provide a kind of two-stage compression heat pump vacuum lyophilization
Unit equipment energy-saving control method, it can be according to food drying technological parameter requirement, regulation hothouse heat supply temperature and heat,
And then determine the optimal condensation temperature of hiigh pressure stage condenser, according to vacuum level requirements and water vessel frosting thickness, determine that water vessel is (also
I.e. low-pressure stage vaporizer) optimal evaporation temperature, according to hiigh pressure stage condenser condensation temperature and water vessel evaporating temperature, in determining
Between the optimal medium temperature of cooler, and realized by corresponding control system, it is achieved unit equipment energy saving in running.
In order to achieve the above object, the present invention is achieved in that it is that a kind of two-stage compression heat pump vacuum freezing is done
Dry unit equipment energy-saving control method, it is characterised in that unit equipment includes that vacuum system, low-pressure stage compressor, hiigh pressure stage are compressed
Machine, cooling water flow regulation valve, bypass heat exchanger, heating medium circulation pump, hiigh pressure stage condenser, hothouse heated barrier, height
Arbitrarily downgrade choke valve, intercooler, low-pressure stage choke valve, water vessel, control system, heating medium inlet temperature sensor, height
Condensation temperature of arbitrarily downgrading sensor, medium temperature sensor and water vessel evaporating temperature sensor；Wherein said heating medium inlet
Temperature sensor senses enters temperature T1 adding thermal medium of hothouse heated barrier porch, hiigh pressure stage condensation temperature sensor
Condensation temperature T2 of sensing hiigh pressure stage condenser, medium temperature sensor sensing enters the medium temperature of the coolant of intercooler
T3, evaporating temperature T4 of water vessel evaporating temperature sensor sensing water vessel；The energy-saving control method of described control system includes
Step is as follows:
(1) temperature T1 adding thermal medium of entrance hothouse heated barrier is determined according to food drying technological requirement, as control
Object processed is realized by the aperture of regulation cooling water flow regulation valve, when actual temperature is more than setting value, and cooling water flow
The aperture of regulation valve strengthens, otherwise reduces；
(2) according to the change of water vessel surface frost thickness in unit equipment vacuum level requirements and unit equipment running,
Determine that in unit equipment running, evaporating temperature T4 of water vessel is with the functional expression running time t change；The following is a kind of letter
The computational methods changed:
A (), according to determining the vacuum of hothouse, obtains the corresponding steam de-sublimation temperature of water vessel, namely water vessel frost layer table
Evaporating temperature T4 in face have to be lower than this temperature, the highest initial evaporation of water vessel when this temperature namely unit equipment bring into operation
Temperature T41；
B () always catches the water yield and surface area according to water vessel, frosting thickness in water vessel surface when determining whole service end cycle
D, obtains end evaporating temperature T42 of required water vessel at the end of cycle of operation, therefore catches water in the S time in whole service cycle
The initial vaporization temperature T41 of device and the poor Δ T=T41-T42 terminating evaporating temperature T42；
C () because of in the S time in whole service cycle, the unit interval distillation water yield is different, according to actual motion rule, and its running
Substantially can be divided into two stages, the first stage is 0～0.5S within the operation time of half, and the distillation water yield is about total Water
70% ± 10%, and unit interval distillation amount is essentially identical；Within the second stage remaining operation time namely 0.5S～S, distillation
The water yield is about the 30% ± 10% of total Water, and unit interval distillation amount is the most essentially identical；As calculated with plate water vessel, then
Evaporating temperature T4 of first stage water vessel (12) is T4=T41-1.4*(t/s with the function formula I of operation time t change) * Δ
T, in formula I,, the function formula II changed at the evaporating temperature T4 t in time of second stage water vessel is T4=T41-
0.4 Δ T-0.6*(t/s) * Δ T, in formula II,, it is contemplated that to the certain safe clearance of evaporating temperature, actual evaporation temperature
Degree T4 can reduce by 2～3 DEG C on the basis of above-mentioned value of calculation；
(3) in determining according to evaporating temperature T4 of low-pressure stage refrigeration system water vessel and condensation temperature T2 of hiigh pressure stage condenser
Between optimal medium temperature T3 of cooler, optimal medium temperature T3 of intercooler with water vessel evaporating temperature T4 and
The function formula III of the condensation temperature T2 change of hiigh pressure stage condenser is: P3=(P2*P4)0.5, in formula III, P2 is hiigh pressure stage condenser
The saturation pressure corresponding to condensation temperature T2, P4 is the saturation pressure corresponding to evaporating temperature T4 of water vessel, according to function
The calculated P3 of formula III can directly obtain the optimal middle temperature of the saturation temperature of correspondence, this temperature namely intercooler
Degree T3；
(4) the function formula I changed with operation time t according to evaporating temperature T4 of water vessel and function formula II, saved by low-pressure stage
The aperture regulation of stream valve and the rotational speed regulation of low-pressure stage compressor realize；When the actual value of evaporating temperature T4 of water vessel is higher than
During value of calculation, the rotating speed of low-pressure stage compressor improves, and the aperture of low-pressure stage choke valve reduces accordingly, when actual value is less than value of calculation
Time, the rotating speed of low-pressure stage compressor reduces, and the aperture of low-pressure stage choke valve strengthens accordingly；
(5) optimal medium temperature T3 of the intercooler determined is calculated according to function formula III, by hiigh pressure stage choke valve
The rotational speed regulation of aperture regulation and high pressure stage compressor realizes；Actual value when optimal medium temperature T3 of intercooler
During higher than value of calculation, the rotating speed of high pressure stage compressor improves, and the aperture of hiigh pressure stage choke valve reduces accordingly, when actual value is less than meter
During calculation value, high pressure stage compressor rotating speed reduces, and the aperture of hiigh pressure stage choke valve strengthens accordingly.
Present invention advantage compared with prior art is: it can regulate be dried according to food drying technological parameter requirement
Room heat supply temperature and heat, and then determine hiigh pressure stage condenser condensation temperature, according to vacuum level requirements and water vessel frosting thickness,
Determine the optimal evaporating temperature of water vessel, according to hiigh pressure stage condenser condensation temperature and water vessel evaporating temperature, determine centre
The medium temperature that cooler is optimal, and realized by corresponding control system, it is achieved unit equipment energy saving in running.
Accompanying drawing explanation
Fig. 1 is the two-stage compression heat pump vacuum lyophilization combined equipment system schematic diagram that the present invention implements.
Detailed description of the invention
Embodiments of the invention are described below in detail, and the example of described embodiment is shown in the drawings.Below with reference to
The embodiment that accompanying drawing describes is exemplary, is only used for explaining the present invention, and is not considered as limiting the invention.
As it is shown in figure 1, it is a kind of two-stage compression heat pump vacuum lyophilization unit equipment energy-saving control method, combination
Equipment include vacuum system 1, low-pressure stage compressor 2, high pressure stage compressor 3, cooling water flow regulation valve 4, bypass heat exchanger 5,
Heating medium circulation pump 6, hiigh pressure stage condenser 7, hothouse heated barrier 8, hiigh pressure stage choke valve 9, intercooler 10, low pressure
Level choke valve 11, water vessel 12, control system 13, heating medium inlet temperature sensor 14, hiigh pressure stage condensation temperature sensor
15, medium temperature sensor 16 and water vessel evaporating temperature sensor 17；Wherein
The refrigerant exit of described high pressure stage compressor 3 connects with the refrigerant inlet of bypass heat exchanger 5, described bypass heat exchanger 5
Refrigerant exit connects with the refrigerant inlet of hiigh pressure stage condenser 7, and the refrigerant exit of described hiigh pressure stage condenser 7 is saved by hiigh pressure stage
Stream valve 9 connects with a refrigerant inlet of intercooler 10, and a refrigerant exit of described intercooler 10 is saved by low-pressure stage
Stream valve 11 connects with the refrigerant inlet of water vessel 11, and the refrigerant exit of described water vessel 11 returns with the coolant of low-pressure stage compressor 2
QI KOU connects, and the refrigerant exit of described low-pressure stage compressor 2 leads to another refrigerant inlet of intercooler 10, intercooling
Another refrigerant exit of device 10 connects with the coolant gas returning port of high pressure stage compressor 3；Described heating medium circulation pump 7 and hothouse
Heated barrier 8 is connected, and hiigh pressure stage condenser 7 is to adding thermal medium heating, and the thermal medium that adds after being heated is flowed into hothouse heating
Hothouse material is heated by dividing plate 8；The temperature of described cooling water flow regulation valve 4 scalable bypass heat exchanger 5, described
Vacuum system 1 carries out evacuation to hothouse, and water vessel 12 traps the moisture content from hothouse；
Described heating medium inlet temperature sensor 14 sensing enters the temperature adding thermal medium of hothouse heated barrier 8 entrance also
I.e. temperature T1 of hothouse heated barrier 8, hiigh pressure stage condensation temperature sensor 15 senses the condensation temperature of hiigh pressure stage condenser 7
T2, medium temperature sensor 16 sensing enters medium temperature T3 of the coolant of intercooler 10, and water vessel evaporating temperature senses
Device 17 senses low-pressure stage evaporator evaporation temperature namely evaporating temperature T4 of water vessel 12；The energy-saving control method of control system 13
Comprise the following steps that
(1) temperature T1 adding thermal medium of entrance hothouse heated barrier 8 entrance is determined according to food drying technological requirement, with
This is realized by the aperture of regulation cooling water flow regulation valve 4 for control object, when actual temperature is more than setting value, and cooling
The aperture of Water flow adjusting valve 4 strengthens, otherwise reduces；
(2) according to the change of water vessel 12 surface frost thickness in unit equipment vacuum level requirements and unit equipment running
Change, determine that in unit equipment running, evaporating temperature T4 of water vessel 12 is with the functional expression running time t change；Because combination sets
Standby in a cycle of operation, in the unit interval, the water yield of distillation is different, carries out calculating complex according to heat transfer theory, with
Under be the computational methods of a kind of simplification:
A (), according to the vacuum of the hothouse determined, obtains the corresponding steam de-sublimation temperature of water vessel 12, namely water vessel 12
Evaporating temperature T4 on frost layer surface have to be lower than this temperature, and when this temperature namely unit equipment bring into operation, water vessel 12 is the highest
Initial vaporization temperature T41；
B () always catches the water yield and surface area according to water vessel 12, water vessel 12 surface frosting when determining whole service end cycle
Thickness d, obtains end evaporating temperature T42 of required water vessel 12 at the end of cycle of operation, therefore S time in whole service cycle
The initial vaporization temperature T41 of interior the water vessel 12 and poor Δ T=T41-T42 terminating evaporating temperature T42；
C () because of in the S time in whole service cycle, the unit interval distillation water yield is different, according to actual motion rule, and its running
Substantially can be divided into two stages, the first stage is 0～0.5S within the operation time of half, and the distillation water yield is about total Water
70% ± 10%, and unit interval distillation amount is essentially identical；Within the second stage remaining operation time namely 0.5S～S, distillation
The water yield is about the 30% ± 10% of total Water, and unit interval distillation amount is the most essentially identical；As calculated with plate water vessel, then
Evaporating temperature T4 of first stage water vessel 12 is T4=T41-1.4*(t/s with the function formula I of operation time t change) * Δ T,
In formula I,, the function formula II changed at the evaporating temperature T4 t in time of second stage water vessel 12 is T4=T41-
0.4 Δ T-0.6*(t/s) * Δ T, in formula II,, it is contemplated that to the certain safe clearance of evaporating temperature, actual evaporation temperature
Degree T4 can reduce by 2～3 DEG C on the basis of above-mentioned value of calculation；
(3) determine according to evaporating temperature T4 of low-pressure stage refrigeration system water vessel 12 and condensation temperature T2 of hiigh pressure stage condenser 7
Optimal medium temperature T3 of intercooler 10, optimal medium temperature T3 of intercooler 10 is with the evaporation of water vessel 12
The function formula III of the condensation temperature T2 change of temperature T4 and hiigh pressure stage condenser 7 is: P3=(P2*P4)0.5, in formula III, P2 is high
Arbitrarily downgrading the saturation pressure corresponding to condensation temperature T2 of condenser 7, P4 is saturated corresponding to evaporating temperature T4 of water vessel 12
Pressure, can directly obtain the saturation temperature of correspondence, this temperature namely intercooler according to the calculated P3 of function formula III
Optimal medium temperature T3 of 10；
(4) the function formula I changed with operation time t according to evaporating temperature T4 of water vessel 12 and function formula II, pass through low-pressure stage
The aperture regulation of choke valve 11 and the rotational speed regulation of low-pressure stage compressor 2 realize；Reality when evaporating temperature T4 of water vessel 12
When actual value is higher than value of calculation, the rotating speed of low-pressure stage compressor 2 improves, and the aperture of low-pressure stage choke valve 11 reduces accordingly, works as reality
When value is less than value of calculation, the rotating speed of low-pressure stage compressor 2 reduces, and the aperture of low-pressure stage choke valve 11 strengthens accordingly；
(5) optimal medium temperature T3 of the intercooler 10 determined is calculated according to function formula III, by hiigh pressure stage choke valve
The aperture regulation of 9 and the rotational speed regulation of high pressure stage compressor 3 realize；Optimal medium temperature T3 when intercooler 10
When actual value is higher than value of calculation, the rotating speed of high pressure stage compressor 3 improves, and the aperture of hiigh pressure stage choke valve 9 reduces accordingly, works as reality
When value is less than value of calculation, high pressure stage compressor 3 rotating speed reduces, and the aperture of hiigh pressure stage choke valve 9 strengthens accordingly.
Although an embodiment of the present invention has been shown and described, it will be understood by those skilled in the art that: not
These embodiments can be carried out multiple change in the case of the principle of the disengaging present invention and objective, revise, replace and deform, this
The scope of invention is limited by claim and equivalent thereof.
Claims (1)
1. a two-stage compression heat pump vacuum lyophilization unit equipment energy-saving control method, it is characterised in that unit equipment bag
Include vacuum system (1), low-pressure stage compressor (2), high pressure stage compressor (3), cooling water flow regulation valve (4), bypass heat exchanger
(5), heating medium circulation pump (6), hiigh pressure stage condenser (7), hothouse heated barrier (8), hiigh pressure stage choke valve (9), centre
Cooler (10), low-pressure stage choke valve (11), water vessel (12), control system (13), heating medium inlet temperature sensor
(14), hiigh pressure stage condensation temperature sensor (15), medium temperature sensor (16) and water vessel evaporating temperature sensor (17)；Its
Described in heating medium inlet temperature sensor (14) sensing enter hothouse heated barrier (8) porch the temperature adding thermal medium
Degree T1, condensation temperature T2 of the coolant of hiigh pressure stage condensation temperature sensor (15) sensing hiigh pressure stage condenser (7), medium temperature passes
Sensor (16) sensing enters medium temperature T3 of the coolant of intercooler (10), and water vessel evaporating temperature sensor (17) senses
Evaporating temperature T4 of the coolant of water vessel (12)；The energy-saving control method of described control system (13) comprises the following steps that
(1) temperature T1 adding thermal medium of entrance hothouse heated barrier (8) is determined according to food drying technological requirement, with this
Realized by the aperture of regulation cooling water flow regulation valve (4) for control object, when actual temperature is more than setting value, cooling
The aperture of Water flow adjusting valve (4) strengthens, otherwise reduces；
(2) according to water vessel (12) surface frost thickness in unit equipment vacuum level requirements and unit equipment running
Change, determines that in unit equipment running, evaporating temperature T4 of water vessel (12) is with the functional expression running time t change；Below
It is the computational methods of a kind of simplification:
A (), according to the vacuum of the hothouse determined, obtains the corresponding steam de-sublimation temperature of water vessel (12), namely water vessel
(12) evaporating temperature T4 on frost layer surface have to be lower than this temperature, water vessel (12) when this temperature namely unit equipment bring into operation
The highest initial vaporization temperature T41；
B () always catches the water yield and surface area according to water vessel (12), water vessel (12) surface when determining whole service end cycle
Frosting thickness d, obtains end evaporating temperature T42 of required water vessel (12) at the end of cycle of operation, therefore whole service week
The initial vaporization temperature T41 of water vessel (12) and the poor Δ T=T41-T42 terminating evaporating temperature T42 in time phase S；
C () because of in the S time in whole service cycle, the unit interval distillation water yield is different, according to actual motion rule, and its running
Substantially can be divided into two stages, the first stage is 0～0.5S within the operation time of half, and the distillation water yield is about total Water
70% ± 10%, and unit interval distillation amount is essentially identical；Within the second stage remaining operation time namely 0.5S～S, distillation
The water yield is about the 30% ± 10% of total Water, and unit interval distillation amount is the most essentially identical；As calculated with plate water vessel, then
Evaporating temperature T4 of first stage water vessel (12) is T4=T41-1.4*(t/s with the function formula I of operation time t change) * Δ
T, in formula I,, the function formula II changed at the evaporating temperature T4 t in time of second stage water vessel (12) is T4=
T41-0.4 Δ T-0.6*(t/s) * Δ T, in formula II,, it is contemplated that to the certain safe clearance of evaporating temperature, actual steaming
Send out temperature T4 and can reduce by 2～3 DEG C on the basis of above-mentioned value of calculation；
(3) according to evaporating temperature T4 and condensation temperature T2 of hiigh pressure stage condenser (7) of low-pressure stage refrigeration system water vessel (12)
Determining optimal medium temperature T3 of intercooler (10), optimal medium temperature T3 of intercooler (10) is with water vessel
(12) the function formula III of the condensation temperature T2 change of evaporating temperature T4 and hiigh pressure stage condenser (7) is: P3=(P2*P4)0.5, letter
In numerical expression III, P2 is the saturation pressure corresponding to condensation temperature T2 of hiigh pressure stage condenser (7), and P4 is the evaporation of water vessel (12)
Saturation pressure corresponding to temperature T4, can directly obtain the saturation temperature of correspondence according to the calculated P3 of function formula III, this
Temperature namely optimal medium temperature T3 of intercooler (10)；
(4) the function formula I changed with operation time t according to evaporating temperature T4 of water vessel (12) and function formula II, pass through low pressure
The aperture regulation of level choke valve (11) and the rotational speed regulation of low-pressure stage compressor (2) realize；Evaporation temperature when water vessel (12)
When the actual value of degree T4 is higher than value of calculation, the rotating speed of low-pressure stage compressor (2) improves, and the aperture of low-pressure stage choke valve (11) is corresponding
Reducing, when actual value is less than value of calculation, the rotating speed of low-pressure stage compressor (2) reduces, the aperture phase of low-pressure stage choke valve (11)
Should strengthen；
(5) calculate optimal medium temperature T3 of the intercooler (10) determined according to function formula III, throttled by hiigh pressure stage
The aperture regulation of valve (9) and the rotational speed regulation of high pressure stage compressor (3) realize；Optimal centre when intercooler (10)
When the actual value of temperature T3 is higher than value of calculation, the rotating speed of high pressure stage compressor (3) improves, the aperture phase of hiigh pressure stage choke valve (9)
Should reduce, when actual value is less than value of calculation, high pressure stage compressor (3) rotating speed reduces, and the aperture of hiigh pressure stage choke valve (9) is corresponding
Strengthen.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610299893.3A CN105962005B (en) | 2016-05-09 | 2016-05-09 | Energy-saving control method for two-stage compression type heat pump vacuum freeze drying combined equipment |
| PCT/CN2016/092839 WO2017193490A1 (en) | 2016-05-09 | 2016-08-02 | Energy-saving control method for vacuum freezing and drying combined device for double-stage compression heat pump |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610299893.3A CN105962005B (en) | 2016-05-09 | 2016-05-09 | Energy-saving control method for two-stage compression type heat pump vacuum freeze drying combined equipment |
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| CN105962005A true CN105962005A (en) | 2016-09-28 |
| CN105962005B CN105962005B (en) | 2019-12-27 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107676973A (en) * | 2017-10-27 | 2018-02-09 | 顺德职业技术学院 | Frequency conversion two-stage compression heat pump water heater dynamic heat frequency optimization and control method |
| CN107906752A (en) * | 2017-10-27 | 2018-04-13 | 顺德职业技术学院 | Twin-stage frequency conversion two-stage compression heat pump water heater frequency dynamic optimizes and control method |
| CN112815560A (en) * | 2021-01-18 | 2021-05-18 | 珠海格力电器股份有限公司 | Two-stage compression system and control method thereof |
| CN114413497A (en) * | 2022-01-06 | 2022-04-29 | 珠海格力电器股份有限公司 | Two-stage compressor, control method and device, control equipment and refrigeration equipment |
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| CN111006413B (en) * | 2019-12-30 | 2023-09-19 | 冰山冷热科技股份有限公司 | Wide ring temperature range CO for low pressure exhaust heat recovery 2 Air source heat pump system |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107676973A (en) * | 2017-10-27 | 2018-02-09 | 顺德职业技术学院 | Frequency conversion two-stage compression heat pump water heater dynamic heat frequency optimization and control method |
| CN107906752A (en) * | 2017-10-27 | 2018-04-13 | 顺德职业技术学院 | Twin-stage frequency conversion two-stage compression heat pump water heater frequency dynamic optimizes and control method |
| WO2019080278A1 (en) * | 2017-10-27 | 2019-05-02 | 顺德职业技术学院 | Method for dynamically optimizing and controlling frequency two-stage variable frequency two-stage compression heat pump water heater |
| CN107906752B (en) * | 2017-10-27 | 2019-06-14 | 顺德职业技术学院 | The optimization of twin-stage frequency conversion two-stage compression heat pump water heater frequency dynamic and control method |
| CN112815560A (en) * | 2021-01-18 | 2021-05-18 | 珠海格力电器股份有限公司 | Two-stage compression system and control method thereof |
| CN112815560B (en) * | 2021-01-18 | 2022-06-17 | 珠海格力电器股份有限公司 | Two-stage compression system and control method thereof |
| CN114413497A (en) * | 2022-01-06 | 2022-04-29 | 珠海格力电器股份有限公司 | Two-stage compressor, control method and device, control equipment and refrigeration equipment |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105962005B (en) | 2019-12-27 |
| WO2017193490A1 (en) | 2017-11-16 |
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