TREA

Heat transfer method

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Information

  • Patent Grant
  • 10858561
  • Patent Number
    10,858,561
  • Date Filed
    Thursday, July 5, 2018
    6 years ago
  • Date Issued
    Tuesday, December 8, 2020
    4 years ago
Information
Abstract
A method of heat transfer by means of a composition containing hydrochlorofluoroolefins. A heat transfer method including, successively, a step of evaporation of a coolant fluid, a compression step, a step of condensation of said fluid at a temperature of greater than or equal to 70° C. and a step of expansion of said fluid, characterized in that that coolant fluid includes at least one hydrochlorofluoroolefin.
Description
TECHNICAL FIELD

The present invention relates to a heat transfer process using a composition containing hydrochlorofluoroolefins. It relates more particularly to the use of a composition containing hydrochlorofluoroolefins in heat pumps.


BACKGROUND

The problems posed by substances which deplete the atmospheric ozone layer (ODP: ozone depletion potential) were tackled at Montreal, where the protocol imposing a reduction in the production and use of chlorofluorocarbons (CFCs) was signed. This protocol has been the subject of amendments which have required that CFCs be withdrawn and have extended regulatory control to other products.


The refrigeration industry and the air conditioning industry have invested a great deal in the replacement of these refrigerant fluids.


In the automotive industry, the air conditioning systems for vehicles sold in many countries have changed from a chlorofluorocarbon (CFC-12) refrigerant fluid to a hydrofluorocarbon (1,1,1,2-tetrafluoroethane: HFC-134a) refrigerant fluid which is less harmful to the ozone layer. However, from the viewpoint of the objectives set by the Kyoto protocol, HFC-134a (GWP=1300) is regarded as having a high warming potential. The contribution to the greenhouse effect of a fluid is quantified by a criterion, the GWP (Global Warming Potential), which indexes the warming potential by taking a reference value of 1 for carbon dioxide.


As carbon dioxide is non-toxic and non-flammable and has a very low GWP, it has been proposed as a refrigerant fluid for air conditioning systems as a replacement for HFC-134a. However, there are several disadvantages to the use of carbon dioxide, related in particular to the very high pressure of the use thereof as a refrigerant fluid in existing devices and technologies.


Document JP 4110388 describes the use of hydro-fluoropropenes of formula C.sub.3H.sub.mF.sub.n with m and n representing an integer between 1 and 5 inclusive and m+n=6, as heat transfer fluids, in particular tetrafluoropropene and trifluoropropene.


Document WO 2004/037913 discloses the use of compositions comprising at least one fluoroalkene having three or four carbon atoms, in particular pentafluoropropene and tetrafluoropropene, preferably having a GWP at most of 150, as heat transfer fluids.


In document WO 2007/002625, fluorohaloalkenes having from to 6 carbon atoms, in particular tetrafluoropropenes, pentafluoropropenes and chlorotrifluoropropenes, have been described as capable of being used as a heat transfer fluid.


In the field of heat pumps, substitutes for dichlorotetrafluoroethane (HCFC-114), used under conditions of high condensing temperature, have been proposed. Thus, document U.S. Pat. No. 6,814,884 describes a composition comprising 1,1,1,3,3-pentafluorobutane (HFC-365mfc) and at least one compound chosen from 1,1,1,2-tetrafluoroethane, pentafluoroethane (HFC-125), 1,1,1,3,3-pentafluoropropane (HFC-245fa) and 1,1,1,2,3,3,3-heptafluoropropane (HFC-227ea). However, these compounds have a high GWP.







DETAILED DESCRIPTION

The applicant has now discovered that compositions containing hydrochlorofluoroolefins are very particularly suitable as heat transfer fluid in heat pumps, in particular heat pumps that operate at a high condensing temperature. Moreover, these compositions have a negligible ODP and a GWP below that of existing heat transfer fluids.


The term “hydrochlorofluoroolefins” is understood to mean olefins having from 3 to 4 carbon atoms that comprise one chlorine atom and at least one fluorine atom. Preferably, the chlorine atom is borne by the unsaturated carbon.


A heat pump is a thermodynamic device allowing the transfer of heat from the coldest medium to the hottest medium. The heat pumps used for heating are referred to as compression heat pumps and the operation is based on the principle of the compression cycle of fluids, referred to as refrigerant fluids. These heat pumps operate with compression systems comprising a single or several stage(s). At a given stage, when the refrigerant fluid is compressed and passes from the gaseous state to the liquid state, an exothermic reaction (condensation) takes place that produces heat. Conversely, if the fluid is expanded by passing it from the liquid state to the gaseous state, an endothermic reaction (evaporation) takes place, which produces a cold sensation. Everything therefore relies on the change of state of a fluid used in a closed circuit.


Each stage of a compression system comprises (i) a step of evaporation during which, in contact with heat drawn from the surroundings, the refrigerant fluid, by virtue of its low boiling point, changes from the liquid state to the gaseous state, (ii) a step of compression during which the gas from the preceding step is brought to high pressure, (iii) a step of condensation during which the gas will transmit its heat to the heating circuit; the refrigerant, still compressed, becomes liquid again and (iv) a step of expansion during which the pressure of the fluid is reduced. The fluid is ready for a new absorption of heat from the cold environment.


One subject of the present invention is a heat transfer process using a compression system having at least one stage successively comprising a step of evaporation of a refrigerant fluid, a step of compression, a step of condensation of said fluid at a temperature greater than or equal to 70° C. and a step of expansion of said fluid characterized in that the refrigerant fluid comprises at least one hydrochlorofluoroolefin.


Preferably, the condensing temperature of the refrigerant fluid is between 70 and 140° C., and advantageously between 95 and 125° C.


Preferably, the hydrochlorofluoroolefins comprise at least three fluorine atoms.


Particularly advantageous hydrochlorofluoroolefins are chlorotrifluoropropenes (HCFO-1233), in particular 1-chloro-3,3,3-trifluoropropene (HCFO-1233zd) and 2-chloro-3,3,3-trifluoropropene (HCFO-1233xf). The 1-chloro-3,3,3-trifluoropropene may be in either cis form or trans form.


Besides the hydrochlorofluoroolefin(s), the refrigerant fluid may comprise at least one hydrofluorocarbon.


As hydrofluorocarbons, mention may especially be made of 1,1,1,3,3-pentafluorobutane, 1,1,1,2-tetrafluoroethane, pentafluoroethane, 1,1,1,3,3-pentafluoropropane, 1,1,1,2,3-pentafluoropropane, 1,1,1,2,2-penta-fluoropropane and 1,1,1,2,3,3,3-heptafluoropropane.


The refrigerant fluid may also comprise at least one fluoroether, preferably at least one hydrofluoroether and advantageously at least one hydrofluoroether having from three to six carbon atoms.


As hydrofluoroethers, mention may especially be made of heptafluoromethoxypropane, nonafluoromethoxybutane and nonafluoroethoxybutane.


The hydrofluoroether is available in several isomeric forms such as 1,1,1,2,2,3,3,4,4-nonafluoroethoxybutane, 1,1,1,2,3,3-hexafluoro-2-(trifluoromethyl)-3-ethoxybutane, 1,1,1,2,2,3,3,4,4-nonafluoromethoxybutane and 1,1,1,2,3,3-hexafluoro-2-(trifluoromethyl)-3-methoxybutane.


The refrigerant fluid may also comprise at least one fluoroalkene having from 3 to 6 carbon atoms. Preferably, the fluoroalkene is chosen from fluoropropenes, in particular trifluoropropenes such as 1,1,1-trifluoropropene, tetrafluoropropenes such as 2,3,3,3-tetrafluoropropene (HFO-1234yf), 1,3,3,3-tetrafluoropropene and fluorobutenes. Fluoromethylpropenes may be suitable.


Preferably, the refrigerant fluid comprises at least 10% by weight of hydrochlorofluoroolefins.


The refrigerant fluid used in the present invention may comprise a stabilizer of the hydrochlorofluoroolefin. The stabilizer represents at most 5% by weight relative to the total composition of the fluid.


As stabilizers, mention may especially be made of nitromethane, ascorbic acid, terephthalic acid, azoles such as tolutriazole or benzotriazole, phenolic compounds such as tocopherol, hydroquinone, t-butylhydroguinone, 2,6-di-cert-butyl-4-methylphenol, epoxides (alkyl, optionally fluorinated or perfluorinated, or alkenyl or aromatic epoxides) such as n-butyl glycidyl ether, hexanediol diglycidyl ether, allyl glycidyl ether or butylphenyl glycidyl ether, phosphites, phosphates, phosphonates, thiols and lactones.


The refrigerant used in the process according to the present invention may comprise lubricants such as mineral oil, alkylbenzene, polyalkylene glycol and polyvinyl ether.


EXPERIMENTAL SECTION

In what follows:


Evap P is the pressure at the evaporator


Cond P is the pressure at the condenser


T cond is the condensing temperature


Te comp is the compressor inlet temperature


Ratio: the compression ratio


T outlet comp is the compressor outlet temperature


COP: coefficient of performance and is defined, where a heat pump is concerned, as being the useful heat power provided the system over the power taken in or consumed by the system


CAP: volumetric capacity, heat capacity per unit volume (kJ/m.sup.3)


% CAP or COP is the ratio of the value of the CAP or COP of the fluid relative to that obtained with HCFC-114.


Example 1

The performances of the refrigerant fluid under the heat pump operating conditions and by setting the temperature at the evaporator to 10° C. and that at the condenser to 100° C. are given below.


For HCFC-114, the nominal operating pressure is 14.19 bar, the volumetric capacity is 785 kJ/m.sup.3 and the COP is 2.07 under the following operating conditions:


Isentropic efficiency of the compressor: 80%




















HCFO-
HFC-365mfc/



HCFC-114
HFC-365mfc
1233zd
HFC-227ea




















Temp evap (° C.)
10
10
10
10


T e comp
15
15
15
15


Evap P (kPa)
129
30
76


Cond P (kPa)
1419
590
1048


Ratio (p/p)
11.04
19.81
13.72
27.1


T cond (° C.)
100
100
100
100


T outlet comp
100
100
103


(° C.)


CAP (kJ/m3)
785
260
630
374


COP
2.07
2.30
2.42
2.40


% CAP
100
33
80
48


% COP
100
111
117
116









Example 2

The performances of the refrigerant fluid under the heat pump operating conditions and by setting the temperature at the evaporator to 50° C. and that at the condenser to 80° C. are given below.


For HCFC-114, the nominal operating pressure is 9.3 bar, the volumetric capacity is 3321 kJ/m.sup.3 and the COP is 8.19 under the following operating conditions:


Isentropic efficiency of the compressor: 80%

















HCFC-114
HFC-365mfc
HCFO-1233zd



















Temp outlet evap (° C.)
50
50
50


T e comp (° C.)
65
65
65


Evap P (kPa)
447
142
298


Cond P (kPa)
930
352
663


Ratio (p/p)
2.08
2.48
2.22


T cond (° C.)
80
80
80


T outlet comp (° C.)
90
87
94


CAP (kJ/m3)
3321
1394
2554


COP
8.19
8.60
8.53


% CAP
100
42
77


% COP
100
105
104









Example 3

The performances of the refrigerant fluid under the heat pump operating conditions and by setting the temperature at the evaporator to 50° C. and the temperature at the condenser to 95° C. are given below.


For HCFC-114, the nominal operating pressure is 12.82 bar, the volumetric capacity is 2976 kJ/m.sup.3 and the COP is 5.19 under the following operating conditions:


Isentropic efficiency of the compressor: 80%




















HCFO-




HCFC-114
HFC-365mfc
1233zd
HFO-1234yf




















Temp evap (° C.)
50
50
50
50


T e comp (° C.)
65
65
65
65


Evap P (kPa)
447
142
298
1283


Cond P (kPa)
1282
522
939
3345


Ratio (p/p)
2.87
3.67
3.15
2.61


T cond (° C.)
95
95
95
95


T outlet comp (° C.)
103
98
107
113


CAP (kJ/m3)
2976
1284
2379
4065


COP
5.19
5.56
5.56
2.80


% CAP
100
43
80
137


% COP
100
107
107
54









Example 4

The performances of the refrigerant fluid under the heat pump operating conditions and by setting the temperature at the evaporator to 50° C. and that at the condenser to 110° C. are given below.


For HCFC-114, the nominal operating pressure is 17.26 bar, the volumetric capacity is 2573 kJ/m.sup.3 and the COP is 3.56 under the following operating conditions:


Isentropic efficiency of the compressor: 80%

















HCFC-114
HFC-365mfc
HCFO-1233zd



















Temp evap (° C.)
50
50
50


T e comp (° C.)
65
65
65


Evap P (kPa)
447
142
298


Cond P (kPa)
1726
748
1294


Ratio (p/p)
3.86
5.26
4.34


T cond (° C.)
110
110
110


T outlet comp (° C.)
116
110
121


CAP (kJ/m3)
2573
1157
2172


COP
3.56
3.97
4.00


% CAP
100
45
84


% COP
100
111
112









Example 5

The performances of the refrigerant fluid under the heat pump operating conditions and by setting the temperature at the evaporator to 50° C. and that at the condenser to 120° C. are given below.


For HCFC-114, the nominal operating pressure is 20.82 bar, the volumetric capacity is 2257 kJ/m.sup.3 and the COP is 2.79 under the following operating conditions:


Isentropic efficiency of the compressor: 80%

















HCFC-114
HFC-365mfc
HCFO-1233zd



















Temp evap (° C.)
50
50
50


T e comp
65
65
65


Evap P (kPa)
447
142
298


Cond P (kPa)
2082
936
1581


Ratio (p/p)
4.66
6.58
5.30


T cond (° C.)
120
120
120


T outlet comp (° C.)
125
120
130


CAP (kJ/m3)
2257
1063
2015


COP
2.79
3.25
3.29


% CAP
100
47
89


% COP
100
116
118









Example 6

The performances of the refrigerant fluid under the heat pump operating conditions and by setting the temperature at the evaporator to 80° C. and that at the condenser to 110° C. are given below.


For HCFC-114, the nominal operating pressure is 17.26 bar, the volumetric capacity is 5475 kJ/m.sup.3 and the COP is 7.94 under the following operating conditions:


Isentropic efficiency of the compressor: 80%

















HCFC-114
HFC-365mfc
HCFO-1233zd



















Temp evap (° C.)
80
80
80


T e comp (° C.)
90
90
90


Evap P (kPa)
930
352
663


Cond P (kPa)
1726
748
1294


Ratio (p/p)
1.86
2.12
1.95


T cond (° C.)
110
110
110


T outlet comp (° C.)
116
111
117


CAP (kJ/m3)
5475
2872
4705


COP
7.94
8.83
8.72


% CAP
100
52
86


% COP
100
111
110









Example 7

The performances of the refrigerant fluid under the heat pump operating conditions and by setting the temperature at the evaporator to 80° C. and that at the condenser to 120° C. are given below.


For HCFC-114, the nominal operating pressure is 20.82 bar, the volumetric capacity is 4810 kJ/m.sup.3 and the COP is 5.45 under the following operating conditions:


Isentropic efficiency of the compressor: 80%

















HCFC-114
HFC-365mfc
HCFO-1233zd



















Temp evap (° C.)
80
80
80


T e comp (° C.)
90
90
90


Evap P (kPa)
930
352
663


Cond P (kPa)
2082
936
1581


Ratio (p/p)
2.24
2.66
2.38


T cond (° C.)
120
120
120


T outlet comp (° C.)
126
120
127


CAP (kJ/m3)
4810
2648
4360


COP
5.45
6.36
6.24


% CAP
100
55
91


% COP
100
117
114









Example 8

The performances of the refrigerant fluid under the heat pump operating conditions and by setting the temperature at the evaporator to 80° C. and that at the condenser to 130° C. are given below.


For HCFC-114, the nominal operating pressure is 24.92 bar, the volumetric capacity is 4027 kJ/m.sup.3 and the COP is 3.79 under the following operating conditions:


Isentropic efficiency of the compressor: 80%

















HCFC-114
HFC-365mfc
HCFO-1233zd



















Temp evap (° C.)
80
80
80


T e comp (° C.)
90
90
90


Evap P (kPa)
930
352
663


Cond P (kPa)
2492
1157
1913


Ratio (p/p)
2.68
3.28
2.88


T cond (° C.)
130
130
130


T outlet comp (° C.)
136
130
136


CAP (kJ/m3)
4027
2403
3967


COP
3.79
4.81
4.71


% CAP
100
60
99


% COP
100
127
124









Example 9

The performances of the refrigerant fluid under the heat pump operating conditions and by setting the temperature at the evaporator to 80° C. and that at the condenser to 140° C. are given below.


For HCFC-114, the nominal operating pressure is 29.61 bar, the volumetric capacity is 2971 kJ/m.sup.3 and the COP is 2.46 under the following operating conditions:


Isentropic efficiency of the compressor: 80%

















HCFC-114
HFC-365mfc
HCFO-1233zd



















Temp evap (° C.)
80
80
80


T e comp (° C.)
90
90
90


Evap P (kPa)
930
352
663


Cond P (kPa)
2961
1417
2295


Ratio (p/p)
3.19
4.02
3.46


T cond (° C.)
140
140
140


T outlet comp (° C.)
147
140
147


CAP (kJ/m3)
2971
2134
3520


COP
2.46
3.73
3.62


% CAP
100
72
118


% COP
100
152
147








Claims
  • 1. A heat transfer process using a compression system comprising successively a step of evaporation of a refrigerant fluid, a step of compression of said refrigerant fluid, a step of condensation of said refrigerant fluid at a temperature greater than or equal to 110° C. and a step of expansion of said refrigerant fluid, wherein the refrigerant comprises at least 10% by weight of trans-1-chloro-3,3,3-trifluoropropene and at least 10% by weight a fluoroalkene.
  • 2. The process as claimed in claim 1, wherein the temperature is between 110 and 140° C.
  • 3. The process as claimed in claim 1, wherein the refrigerant fluid comprises at least one hydrofluoroether.
  • 4. The process as claimed in claim 1, wherein the temperature is between 110 and 125° C.
  • 5. The process as claimed in claim 1, wherein the refrigerant fluid comprises at least 10% by weight a hydrofluorocarbon.
  • 6. The process as claimed in claim 1, wherein the temperature is between 120 and 140° C.
  • 7. The process as claimed in claim 1, wherein the temperature is between 130 and 140° C.
  • 8. A heat transfer process using a compression system comprising successively a step of evaporation of a refrigerant fluid, a step of compression of said refrigerant fluid, a step of condensation of said refrigerant fluid at a temperature greater than or equal to 110° C. and a step of expansion of said refrigerant, wherein the refrigerant comprises trans-1-chloro-3,3,3-trifluoropropene.
  • 9. The process as claimed in claim 8, wherein the temperature is greater than or equal to 130° C.
  • 10. The process as claimed in claim 8, wherein the temperature is greater than or equal to 120° C.
  • 11. The process as claimed in claim 8, wherein the refrigerant fluid comprises at least one hydrofluorocarbon.
  • 12. The process as claimed in claim 8, wherein the refrigerant fluid comprises at least one hydrofluoroether.
  • 13. The process as claimed in claim 8, wherein the refrigerant fluid comprises at least one fluoroalkene.
Priority Claims (1)
Number Date Country Kind
08 57032 Oct 2008 FR national
CROSS REFERENCE TO RELATED APPLICATIONS

The present application is a continuation of U.S. application Ser. No. 13/122,890, filed on Apr. 6, 2011, which is a U.S. National stage of International Application No. PCT/FR2009/051943, filed on Oct. 13, 2009, which claims the benefit of French Application No. 0857032, filed on Oct. 16, 2008. The entire contents of each of U.S. application Ser. No. 13/122,890, International Application No. PCT/FR2009/051943, and French Application No. 0857032 are hereby incorporated herein by reference in their entirety.

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Related Publications (1)
Number Date Country
20190048241 A1 Feb 2019 US
Continuations (1)
Number Date Country
Parent 13122890 US
Child 16027743 US