CN101886861A - Refrigerant pneumatic conveyor and heat pump air conditioner using same - Google Patents

Abstract

The invention discloses a refrigerant pneumatic conveyor which consists of a two-stage integrated spray pipe and a CO2 supercritical heat pump air conditioner using the same. The refrigerant pneumatic conveyor consists of a micro quantitative positive displacement pump (4), a vapor-liquid boost nozzle (5), a vapor-liquid precompression spray pipe (6), a gas-liquid separator (7), an automatic exhaust steam valve (8) and a synchronous differential pressure control valve (9); and the CO2 supercritical heat pump air conditioner consists of the refrigerant pneumatic conveyor, an evaporator (1), a gas cooler (2), a compressor (3), a four-way valve (4), an internal gas heat exchanger (11), a steam superheater (12), a check valve (13) and a capillary tube (14). CO2 is taken as a working medium (ODP is equal to 0), therefore the refrigerant pneumatic conveyor and the CO2 supercritical heat pump air conditioner using the same better accord with the modern, energy-saving and environmental-friendly new concept; and the energy efficiency ratio is greatly increased from 2.73 in the old system shown as a figure 2 to 3.67 in the new system shown as a figure 4, and is higher than that of the Freon refrigerant circulating system which is used widely at present. The system opens up an efficient and feasible new approach for the natural working medium which is applied to the heat pump air conditioner, and can obtain excellent social effect and fruitful economic effect.

Description

A kind of refrigerant pneumatic conveyor and use the heat-pump air-conditioner of this device

Technical field

The present invention relates to a kind of refrigerant pneumatic conveyor and use the heat-pump air-conditioner of this device, particularly relate to a kind of refrigerant pneumatic conveyor that constitutes by the integrated jet pipe of two-stage and the CO2 supercritical heat pump air conditioner of using this device thereof.

Background technology

Present heat-pump air-conditioner generally adopts restricting element to regulate evaporation capacity.In Fig. 1, evaporimeter (1), condenser (2), compressor (3), cross valve (4), capillary (5), capillary plays throttling.Fig. 2 builds the CO that the strong people of grade researchs and proposes by Deng of Tsing-Hua University ₂Supercritical refrigeration cycle figure, it is by evaporimeter (1), gas cooler (2), compressor (3), expansion valve (4), injector (5) is formed, and this system is subjected to the emitter construction performance impact, can only move under the situation of firm demand.Fig. 3 is compressed the system diagram of high-efficient compressor by the up-to-date proposition of Samsung " air injection enthalpy-increasing " secondary: evaporimeter (1), gas cooler (2), compressor (3), middle pressure steam generator (4), expansion valve (5), injector (6), pressure regulation expansion valve (7).This system is subjected to the emitter construction performance impact, jet pipe when the sub-load effect of boosting is very limited, and even the working flow that can drop into injection is less than condensation number, so the full-power situation, the fractional energy savings of obtaining is also below 20%, and just more weaker during sub-load.

Other relevant technical elements comprises: people such as Italian G.Cattadori, the tight person of outstanding talent of Xi'an Communications University propose, the steam injection-water increasing apparatus of research, and the coefficient that boosts that is obtained is up to 1.54.

Summary of the invention

Among Fig. 4, by miniature quantitative displacement pump (4), solution-air boost jet pipe (5), liquid-gas precommpression jet pipe (6), gas-liquid separator (7), automatic exhaust steam valve (8), the refrigerant pneumatic conveyor that constituted of differential pressure control valve (9) synchronously; This conveying device and evaporimeter (1), gas cooler (2), compressor (3), cross valve (10), internal gas heat exchanger (11), steam superheater (12), check-valves (13), the CO2 supercritical heat pump air conditioner that capillary (14) is constituted.

Among Fig. 4, the high steam that compressor (3) outlet is 2 enters the solution-air jet pipe (5) that boosts through 3, the low temperature liquid that provides with miniature quantitative displacement pump (4) mixes, the mixed flow that forms slows down in contraction mouth and boosts, time liquid that this high-speed jet injection enters through synchronous differential pressure control valve (9) enters liquid-gas precommpression jet pipe (6) inlet 14 points after two fluid streams are mixed.

Miniature quantitative displacement pump (4) provides quantitative low temperature liquid, and when load reduced, compressor (3) frequency conversion reduced rotating speed, and differential pressure control valve (9) is pressed synchronization parameter and regulated pressure reduction synchronously simultaneously, makes the stream condition satisfy the dynamically working characteristic of jet pipe (6).

The boost coefficient that boosts of jet pipe (5) of solution-air is defined by following formula:

$\mathrm{\&Gamma;}=\frac{P_x-{\mathrm{<figure-callout\; id="0"\; label="P"\; filenames="HSA00000199080800022.png"\; state="\{\{state\}\}">P</figure-callout>}}_{0.s}}{P_{o.s}}$

In the formula, P _O.s--the steam stagnation pressure

P _x--collapsible tube outlet total head

When system's cooling load changes between 21.75～100%, this pressure coefficient can be between 0.15～0.5 value.

Differential pressure control valve (9) is according to the regulated quantity of compressor (3) synchronously, and the mode of taking default definite value self adaptation to regulate is carried out the adjusting program.

(9) the valve decompression of pressure reduction control synchronously amount is determined by following formula:

${\mathrm{\&Delta;P}}_x=\mathrm{\&zeta;}.\&times;{\left(\frac{G_0}{G_x}\right)}^2\&times;{\mathrm{\&Delta;P}}_0$

In the formula: 0～X---represents the process of standard-sized sheet to complete shut-down

The working solution flow of liquid-gas precommpression jet pipe (6) equals 0.59～1.0G ₀, jetting steam caused flow equals 0.2175～1.0m ₀

G ₀--full-load operation liquid measure, m ₀--full load evaporation liquid measure

There is following coupled relation between the displacement of liquid-gas precommpression jet pipe (6) and the injection volume:

Mass ratio of induced-to-inducing air: μ

Work liquid measure G ₀: 4,3,2,1.5,1,0.5

Exhaust steam amount m ₁₈: 1.1925 1.236 1.303,1.351,1.414,1.5

During 21.75% load: m ₁₈=0.348, mass ratio of induced-to-inducing air: μ=0.1577

During 100% load: m ₁₈=1.414, mass ratio of induced-to-inducing air: μ=0.414

The work liquid measure can be decided according to different pressure ratio demands, if system has chosen a certain setting value, also just equals to have chosen the COP value of a correspondence.

Through the steam that gas-liquid separator (7) steam (vapor) outlet 18 is discharged, enter the motor internal cooling inlet 19 of compressor (3) after in internal gas heat exchanger (12), once heating; After motor internal is by post bake to air entry 1.

Cross valve (10) can be done the pattern conversion, and when adopting refrigeration mode, 5-6 and 4-5 ' become communication channel; When adopting heating mode, 4-5 and 5 '-6 one-tenth communication channel.

Among the present invention, described CO2 supercritical heat pump air conditioner is characterized in that: the working solution flow of liquid-gas precommpression jet pipe (6) equals 0.59～1.0G ₀, jetting steam caused flow equals 0.2175～1.0m ₀When system's cooling load changes between 21.75～100%, solution-air boost the pressure coefficient of jet pipe (5) can be between 0.15～0.5 value, flow can be chosen arbitrarily between 0.5～4, but just keeps quantitatively constant after selected; Compressor (3) can adopt the various types that can adapt to the high-voltage operation operating mode such as vortex, rolling-rotor, piston.

Among the present invention, described air-cooled CO2 supercritical heat pump air conditioner is characterized in that precommpression realizes possessing using names by the liquid injection " CO ₂Liquid spray air conditioner " popular feature.

Among Fig. 5,2-11 is meant system's rated load graph, 2 "-11 " graph is the situation during less than rated load.

Description of drawings

Fig. 1 regulates the air-cooled heat-pump air-conditioner schematic diagram of evaporation capacity for adopting restricting element.

Fig. 2 is the strong CO that waits the people to research and propose for Deng of Tsing-Hua University builds ₂Overcritical refrigeration system schematic diagram.

Fig. 3 is the system diagram of the up-to-date proposition of Samsung " air injection enthalpy-increasing " secondary compression high-efficient compressor.

Refrigerant pneumatic conveyor that constitutes by the integrated jet pipe of two-stage that Fig. 4 proposes for the present invention and the CO2 supercritical heat pump air conditioner schematic diagram that uses this device thereof.

Fig. 5 schemes for the P-h of the circulatory system that the present invention proposes.

Specific embodiments

Embodiment working condition: set evaporator refrigerant flux unit 1.0,7.2 ℃ of evaporating temperatures, 35 ℃ of air themperatures, working medium R744, load 100%.Adopt R744 as the jet working solution, compressor adopts screw compressor, and each flow process is disregarded resistance.

1, the operating mode of embodiment 1:(load 100%)

Evaporimeter (1): t ₅=7.2 ℃, P ₅=4.197MPa

S′ ₅＝1.063kj/kg h′ ₅＝218.2kj/kg ρ′ ₅＝881kg/m ³

h″ ₅＝425.6kj/kg v″ ₅＝0.00812m ³/kg S ₅″＝1.8028.kj/kg

The state of cooling: t _{5 '}=86.3～41.3 ℃, 11MPa

A, the solution-air jet pipe (5) that boosts: contraction-diffused

Working steam amount: G ₃=0.08 (steam parameter is seen the compressor outlet parameter), injection flow G ₁₂=0.92.Suppose: the flow type pump with injection temperature t ₁₂=16.8 ℃, saturation pressure P ₁₂=5.8MPa, h ' ₁₂=255kj/kg sets P ₁₄=11MPa

Outlet liquid enthalpy:

The outlet parameter of synchronous differential pressure control valve (9):

t ₁₁＝28℃，ρ′ ₁₁＝790kg/m ³，P ₁₁＝11MPa

Outflow: G ₁₁=1.334.

Parameter after confluxing: pressure 11MPa, h ' 275.5kj/kg

Outflow: G ₁₄=2.334.

B, evaporimeter steam: heat exchange in steam superheater (12), be superheated to 12 ℃ by 7.2 ℃,

Outlet parameter is as follows:

P ₇＝4.197MPa，h′ _7′″＝435.5kj/kg，v″ _7′＝0.009068kg/m ³，

The inlet liquid enthalpy of liquid-gas precommpression jet pipe (6):

${h^{\&prime;}}_{14+11}=\frac{1\&times;273.4+1.334\&times;277}{2.334}=275.5\mathrm{kj}/\mathrm{kg}$

Can draw as calculated: P ₁₇=5.8MPa.

Check in: t ₁₇=16.8 ℃.

C, gas-liquid separator (7) steam exhaust-gas once is superheated to 29.5 ℃ through the 18-19-1 process in internal gas heat exchanger (11), and secondary is superheated to 32.4 ℃ in compressor electric motor, the air-breathing parameter of compressor (3):

P ₁＝5.8MPa t ₁＝33.5℃

S ₁″＝1.8223kj/kg h″ _1′＝443kj/kg

D, the interior thermal balance of gas-liquid separator (7):

Check in t ₁₇=20.5 ℃, h ' ₁₇=257.6kj/kg h " ₁₇=406.7kj/kg

Go out the coupled relation between quantity of steam and the jetting steam caused amount:

Mass ratio of induced-to-inducing air: μ=0.414

Input enthalpy 2.334 * 275.5+1.0 * 435.5=1078kj/kg

Output enthalpy 1.92 * 257.6+1.414 * 406.7=1070kj/kg

E, compressor (3) outlet:

S _2′″＝1.8223kj/kg， h″ _2′＝469.4kj/kg

P ₂＝1.9×5.8＝11.MPa， t ₂＝85℃

Compressor (3) isentropic efficiency empirical equation:

${\mathrm{\&eta;}}_3\&ap;1.0-{\mathrm{\&eta;}}_v\&times;\frac{P_2}{{\mathrm{<figure-callout\; id="1"\; label="P"\; filenames="HSA00000199080800011.png,HSA00000199080800012.png"\; state="\{\{state\}\}">P</figure-callout>}}_1}=0.77$

Compressor (3) power consumption: w=(h ₂" h ₁") * (1+a)

＝(469.4-443)×1.414＝37.33 kj/kg

F, gas cooler (2) heat dissipation capacity: q ₂=(469.4-308) * 1.334=215.3 kj/kg

G, evaporimeter (1) unit working medium refrigerating capacity:

Behind Low Temperature Steam superheater (11) the outlet liquid enthalpy heat regenerator:

257.6-(435.5-425.6)＝247.6 kj/kg

q ₁＝(h ₅″-h ₂₁′)

＝425.6-247.7＝178 kj/kg

System's thermal balance:

H, Energy Efficiency Ratio: COP=3.67

1, the operating mode of embodiment 2:(load 21.75%)

Evaporimeter (1): t ₅=7.2 ℃, P ₅=4.197MPa

S′ ₅＝1.063kj/kg h′ ₅＝218.2kj/kg ρ′ ₅＝881kg/m ³

h″ ₅＝425.6kj/kg v″ ₅＝0.00812m ³/kg S ₅″＝1.8028.kj/kg

The state of cooling: t _{5 '}=79.5～36.8 ℃, 9.538MPa

A: solution-air jet pipe (5) contraction-diffused that boosts

Working steam amount: G ₃=0.08 (steam parameter is seen the compressor outlet parameter), injection flow G ₁₂=0.92.Suppose: the flow type pump with injection temperature t ₁₂=14 ℃, saturation pressure P ₁₂=5MPa, h ' ₁₂=238kj/kg sets P ₁₄=9.538MPa

Outlet liquid enthalpy:

The decompression amount of synchronous differential pressure control valve (9):

ΔP ₀₂₁＝ζ.×22.67×ΔP ₀

Outflow: G ₁₁=0.295.

Parameter after confluxing: pressure 9.538MPa, h '=265.9kj/kg

B, evaporimeter (1) low temperature is jetting steam caused: heat exchange in steam superheater (12) is superheated to 8 ℃ by 7.2 ℃.Disregard the process resistance, outlet parameter is as follows:

P ₇＝4.197MPa，h′ _7′″＝435.5kj/kg， v″ _7′＝0.00823kg/m ³，

The inlet liquid enthalpy of liquid-gas precommpression jet pipe (6):

${h^{\&prime;}}_{14+11}=\frac{1\&times;257+0.295\&times;265.9}{1.295}259j/\mathrm{kg}$

Can draw as calculated: P ₁₇=5.02MPa.

Check in: t ₁₇=14.45 ℃.

C, the steam exhaust-gas of gas-liquid separator (7) once are superheated to 29.5 ℃ through the 18-19-1 process in internal gas heat exchanger (11), secondary is superheated to 32.4 ℃ in compressor electric motor, the compressor air suction parameter:

P ₁＝5.02MPa t ₁＝28℃

S ₁″＝1.8256kj/kg h″ _1′＝447.7kj/kg

Thermal balance in the d, gas-liquid separator (7):

Check in t ₁₇=14.45 ℃, h ' ₁₇=238.35kj/kg, h " ₁₇=417.4kj/kg

Coupled relation between liquid-gas precommpression jet pipe (6) exhaust steam amount and the jetting steam caused amount:

Coupling between liquid-gas precommpression jet pipe (6) exhaust steam amount and the jetting steam caused amount:

m ₁₈=0.375, mass ratio of induced-to-inducing air: μ=0.1577

Input enthalpy 1.295 * 259+0.2175 * 427.5=428.5kj/kg

Output enthalpy 1.1375 * 238.35+0.375 * 417.4=427.6kj/kg

Error is less than 1%, and is qualified.

E, compressor (3) outlet parameter:

S _2′″＝1.8562kj/kg h″ _2′＝475kj/kg

P ₂＝1.9×5.02＝9.538.MPa， t ₂＝79.5.℃

Compressor (3) isentropic efficiency empirical equation:

${\mathrm{\&eta;}}_3\&ap;1.0-{\mathrm{\&eta;}}_v\&times;\frac{P_2}{{\mathrm{<figure-callout\; id="1"\; label="P"\; filenames="HSA00000199080800011.png,HSA00000199080800012.png"\; state="\{\{state\}\}">P</figure-callout>}}_1}=0.77$

The power consumption of compressor (3): w=(h ₂" h ₁") * (1+a)

＝(475-447.7)×0.375＝10.23 kj/kg

F, gas cooler (2) heat dissipation capacity:

q ₂＝(475-301.5)×0.295＝51.2 kj/kg

G, evaporimeter (1) unit working medium refrigerating capacity:

Low Temperature Steam superheater (11) outlet liquid enthalpy: 238.35-(1)=237.4 kj/kg

q ₁＝(h ₃″-h ₅′′)

＝0.2175×(425.6-237.4)＝40.93 kj/kg

System's thermal balance:

H, Energy Efficiency Ratio: COP=3.08

Among the present invention, internal gas heat exchanger (10) is provided with at R744 working medium specially.Because the CO2 working medium in the evaporimeter (1) is evaporated under liquefaction condition, so can no longer establish gas-liquid separator before the inlet of compressor (3) in the native system.

When using as heat pump, evaporating temperature is higher than-5 ℃ all can reach 100% load; System still can move when evaporating temperature was lower than-5 ℃, but need take to accompany hot measure could keep whole heating capacities.For by the efficient under the worst cold case, can adopt the method for regulator solution-gas precommpression jet pipe (6) pressure ratio.

Because the present invention adopts CO2 to do working medium (ODP=0), it meets modern environmental protection and energy saving new concept more.Its obtained Energy Efficiency Ratio is significantly brought up to 3.67 of new system shown in Figure 4 by 2.73 of old system shown in Figure 2, is higher than the efficiency ratio that the present freon refrigeration circulatory system of generally using is reached.This system is the application of natural medium on heat pump type air conditioner, has split an efficient feasible new way, will obtain very good social effect and plentiful and substantial economic benefits.

Claims (3)

1. by miniature quantitative displacement pump (4), vapour-liquid boost nozzle (5), liquid-gas precommpression jet pipe (6), gas-liquid separator (7), automatic exhaust steam valve (8), the refrigerant pneumatic conveyor that constituted of differential pressure control valve (9) synchronously; This conveying device and evaporimeter (1), gas cooler (2), compressor (3), cross valve (10), internal gas heat exchanger (11), steam superheater (12), check-valves (13), the CO2 supercritical heat pump air conditioner that capillary (14) is constituted.

2. according to right 1, described CO2 supercritical heat pump air conditioner is characterized in that: the working solution flow of liquid-gas precommpression jet pipe (6) equals 0.59～1.0G ₀, jetting steam caused flow equals 0.2175～1.0m ₀When system's cooling load changes between 21.75～100%, vapour-liquid boost the pressure coefficient of nozzle (5) can be between 0.15～0.5 value, steam and fluid flow can be set value arbitrarily between 0.5～4, promptly remains unchanged after setting; Compressor (3) can adopt the various types that can adapt to the high-voltage operation operating mode such as vortex, rolling-rotor, piston.

3. according to right 1, described air-cooled CO2 supercritical heat pump air conditioner is characterized in that precommpression is sprayed by liquid and realizes possessing using names " CO2 liquid spray air conditioner " popular feature.

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