CA2049996A1 - Process and device for recovering hydrocarbons from a gas-air mixture - Google Patents
Process and device for recovering hydrocarbons from a gas-air mixtureInfo
- Publication number
- CA2049996A1 CA2049996A1 CA 2049996 CA2049996A CA2049996A1 CA 2049996 A1 CA2049996 A1 CA 2049996A1 CA 2049996 CA2049996 CA 2049996 CA 2049996 A CA2049996 A CA 2049996A CA 2049996 A1 CA2049996 A1 CA 2049996A1
- Authority
- CA
- Canada
- Prior art keywords
- gas
- air mixture
- condensation
- refrigerant
- cooling
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0039—Recuperation of heat, e.g. use of heat pump(s), compression
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
(57) Abstract A process and a device for recovering hydrocarbons from a gas-air mixture operates in the following manner: first the gas-air mixture is cooled and caused to condense. The hydrocarbons still remaining in the gas-air mixture after condensation are burned in an internal combustion engine. The power thus generated by the engine is used to operate the cooling installation used for the cooling and condensation processes. The cooling installation is so designed and run that the gas-air mixture is cleansed as far as possible of hydrocarbons and impurities on passing through the installation. Fuel is metered into the gas-air mixture down-stream of the cooling installation and upstream of the internal combustion engine.
Description
~' --18329 WO 91/112~0 PCT/~P9~/0~095 2 ~ 9 6 TRANSL~TION
"Process and A~aratus for Recovery of HYdrocarbons~from a Gas-Air Mixture" ~
- -:
The invention relates to a process for an apparatus for recovery of hydrocarbons from a gas-air mixture resulting from the decanting-or charging of carburetor or diesel fuels according to the preamble of .-patent claim 1 or of patent claim 6.
From DE 36 09 292 C2 such a process is known in which the gas to be cleaned is cleaned in two successive cleaning stages. After the ~irst cleaning stage, which is formed as a refrigeration unit, the .-remaining impurities in the gas to be cleaned are burned in the second cleaning stage. ~he energy thus liberated is used to drive ~ ;
the first cleaning stage. The first cleaning stage is so driven that the amount o~ the impurities remaining thereafter in the gas is ~u~P~ nt to drive the first cleaning stage with the aid o~ ~he energy liberated in the second cleaning stage.
.
., . ~.i.
18329 W0 91/11240 2 ~ $ ~ PCT/EP9lfO0095 ."' .
With the known method or the known apparatus, the first cleaning :
stage which is formed as a refrigeration device is never utilized at ::
approximately its maximum capacity since the gas stream leaving it must always entrain sufficient combustible hydrocarbons and impuri- .
ties to allow the second stage equipped with a combustion unit to have sufficient capacity for driving the refrigeration unit.
Furthermore, in the case of the known process or the known apparatus :.
at start-up, there are problems in that the combustion apparatus .
initially must be charged with a completely uncleaned waste gas before the refrigeration unit can basically be brought into operation. This can be effected in such manner that contaminants during start-up o~ the entire apparatus, which normally would be condensed out in the refriyeration unit and which are combustible, can be released substantially completely into the atmosphere with the gas stream leaving the Gombustion unit. Besides, it is ad- :
vantageous to provide a separate fuel supply for the combustion apparatus by means of which the combustion apparatus can be brought into operatlon before the start-up o~ the entire apparatus itself.
The in~ention presents the ob~ect of providing a process or an apparatus for the recovery of fuel from a gas or mixture in which .:
the cooling and condensation required for the cleaning is effected . ': ' .
-- 2 -- .
'.; ., ' .. .
, , ' 18329 ~0 ~1/11240 2~ PcT/~Pgl/0oo95 to the greatest possible degree and whereafter the hydrocarbons which remain after cooling and condensation in the gas-air mixture ~ -are usable.
This object is achie~ed according to the invention by the features of the characterizing part of the parent claim 1 or the patent claim 6. According to the invention, the complete capacity of the refrigeration apparatus is used for the condensation and cooling of the gas-air mixture and thus for the separation of hydrocarbons and impurities. Notwithstanding such fuel utilization, an optimum operation of the fueled engine is ensured since this is supplied with the fuel quantity required for its operation. Both the refrig-eration unit and the fueled engine can be optimally utilized to their capacities.
;,' '':.
According to the el~odiment of patent c].aim 2 or patent claim 7, the energy generated in the combustion fuel engine is utilizable in an especially simple way to drive refrigeratlon apparatus.
By maintaining the fuel quantity injected in accordance with patent claim 3 or patent claim 8, no external energy 8upply is required for operation of the cooling apparatus.
"Process and A~aratus for Recovery of HYdrocarbons~from a Gas-Air Mixture" ~
- -:
The invention relates to a process for an apparatus for recovery of hydrocarbons from a gas-air mixture resulting from the decanting-or charging of carburetor or diesel fuels according to the preamble of .-patent claim 1 or of patent claim 6.
From DE 36 09 292 C2 such a process is known in which the gas to be cleaned is cleaned in two successive cleaning stages. After the ~irst cleaning stage, which is formed as a refrigeration unit, the .-remaining impurities in the gas to be cleaned are burned in the second cleaning stage. ~he energy thus liberated is used to drive ~ ;
the first cleaning stage. The first cleaning stage is so driven that the amount o~ the impurities remaining thereafter in the gas is ~u~P~ nt to drive the first cleaning stage with the aid o~ ~he energy liberated in the second cleaning stage.
.
., . ~.i.
18329 W0 91/11240 2 ~ $ ~ PCT/EP9lfO0095 ."' .
With the known method or the known apparatus, the first cleaning :
stage which is formed as a refrigeration device is never utilized at ::
approximately its maximum capacity since the gas stream leaving it must always entrain sufficient combustible hydrocarbons and impuri- .
ties to allow the second stage equipped with a combustion unit to have sufficient capacity for driving the refrigeration unit.
Furthermore, in the case of the known process or the known apparatus :.
at start-up, there are problems in that the combustion apparatus .
initially must be charged with a completely uncleaned waste gas before the refrigeration unit can basically be brought into operation. This can be effected in such manner that contaminants during start-up o~ the entire apparatus, which normally would be condensed out in the refriyeration unit and which are combustible, can be released substantially completely into the atmosphere with the gas stream leaving the Gombustion unit. Besides, it is ad- :
vantageous to provide a separate fuel supply for the combustion apparatus by means of which the combustion apparatus can be brought into operatlon before the start-up o~ the entire apparatus itself.
The in~ention presents the ob~ect of providing a process or an apparatus for the recovery of fuel from a gas or mixture in which .:
the cooling and condensation required for the cleaning is effected . ': ' .
-- 2 -- .
'.; ., ' .. .
, , ' 18329 ~0 ~1/11240 2~ PcT/~Pgl/0oo95 to the greatest possible degree and whereafter the hydrocarbons which remain after cooling and condensation in the gas-air mixture ~ -are usable.
This object is achie~ed according to the invention by the features of the characterizing part of the parent claim 1 or the patent claim 6. According to the invention, the complete capacity of the refrigeration apparatus is used for the condensation and cooling of the gas-air mixture and thus for the separation of hydrocarbons and impurities. Notwithstanding such fuel utilization, an optimum operation of the fueled engine is ensured since this is supplied with the fuel quantity required for its operation. Both the refrig-eration unit and the fueled engine can be optimally utilized to their capacities.
;,' '':.
According to the el~odiment of patent c].aim 2 or patent claim 7, the energy generated in the combustion fuel engine is utilizable in an especially simple way to drive refrigeratlon apparatus.
By maintaining the fuel quantity injected in accordance with patent claim 3 or patent claim 8, no external energy 8upply is required for operation of the cooling apparatus.
~ . , 18329 W0 91/11240 2~ g PCT~P91j~0095 By means of the specific gravity separation given in patent claims 4 or 9, the condensate deriving from the refrigeration unit is separatable without high cost into its components, for example water and liquid fuel.
In accordance with the process of patent claim S, in which the com-bustible fuel engine is continuou51y operated to generate electrical energy, the cooling or condensation stage is si~ultaneously included as part of the supply unit for the combustible-fuel engine.
Fluctuations of the fuel quantity resulting from cooling and condensation are compensated by storage of the fuel and matching metering of further fuel. An advantageous power capacity for a combustion engine operated in such manner can amount to about lO0 kW. With such continuous operation of the combustion engine, the highly volatile hydrocarbons resulting from the cooling and condensation can be utilized logically for energy generation before they are transformed in a gaseous state and can pass into the atmosphere.
;';,.~,~;.., : .. - . ., , : . . . . .. : . .: . : . :. , ~. .:. . . : . ~ ::: :. : .:: . :
18329 ~O 91/11240 2 0 '~ ~ ~ 9 6 PCT/EP91/00095 In the embodiment of the refrigeration unit according to patent claim 10, the refrigerant actually used in the evaporator stage of the evaporator passes from a liquid into the vapor state and removes from the contaminated gas or mixture the medium to be cooled -utilizing the heat of evaporation required for the change of state of the refrigerant. This evaporator stage is followed by an after--evaporator stage; in the latter the refrigerant actually used, now in vapor form, is brought from its evaporation temperature which is lower, by comparison to that of the refrigerant for which the expansion or depressurization control valve is designed by heating to a temperature corresponding to that of the tlatter3 re~rigerant at the expansion valve after e~aporation and the usual superheating.
~his allows complete utilization of the enthalpy of the refrigerant without necessitating the provision of a portion of the evaporator state ag a superheating stretch re~ulting in a loss of power.
The after-evaporation stage, in which the vapor state refrigerant actually used is heated to the temperature o~ the refriyerant for which the expansion or depressurization valve is designed after the required superheating of the latter refrigerant for this expansion .
. .
:
~ , .f~
18329 wo 91/11240 2 ~ 9 ~ PCT/EP91/00095 control valve, is utilizable as a cooling stage because of the comparatively high temperature diEference between this latter temperature and the evaporation temperature of the refrigerant actually used for the capacity thereof.
By ~orresponding constructural configuration and assembly of the evaporator stage and the after-evaporator stage, the medium to be ~ -cooled initially is passed through the after-cooling stage and then passed through the evaporator stage itself. The after-cooling stage is thus effectively used as a precooler. The control of the expansion-control valve is so effected that the refrigerant at the outlet of the evaporator assumes a pressure and temperature for which the expansion-control valve is set for control of the provided parameters. The provision of the evaporator stage according to patent claim 11 allows an especially exact control of the refrig-erant volumetric flow from the superpressure reservoir into the evaporator.
According to patent claim 12, the after-evaporator stage capacity is dimensioned to be sufficient so that even with the precooling, the ~ -temperature of the medium to be cooled is dropped significantly.
. ~ ; . , ~ .............. . . . .... .
,, , , ", ,. ,,~ . : ... , , . . ~ , ., . ;, , , ~ . , ~ ~ : . ., 18329 ~0 91/11240 PC~P91~00095 An especially advantageous operation of the refrigerating unit is effected by the provision according to claim 13 of the expansion--control valve and evaporator in combination with the refrigerant there givPn.
The invention is described in greater detail below with respect to an embodiment thereof with referance to the drawings. They show:
Figure 1 a schematic illustration of an embodiment of the process of the invention or the apparatus of the invention;
Figure 2 an embodiment oP the cascade cooling unit of Figure 1 and Figure 3 an embodimen of the evaporator shown in Figure ~.
-. . ~,:
An air-gas mixture A, which from decanting or filling contains carburetor or diesel fuel, is fed to a refrigerating unit 15. The refrigerating unit 15 is formed from a liquid cooler 17 and a cascade cooling device 18 traversed in succession by the air-~as mixture A. In the refrigerating unit 15, the air-ga~ mixture is cooled and condensed. The condensate which separates out, which is in the liquid form and contains impurities, water and hydrocarbons, is supplied to a specific-gravity separator 22 in which the different components are separated.
: ~ ' . ' " ' ' . ',, ' ' ' ';,'"
18329 WO 91/11240 PCT~EP91/00095 The air-gas mixture B from the refrigerating unit 15, which contains small quantities, still of some impurities of hydrocarbons, is supplied to a combustion-power ~internal combustion] engine lG in which the remaining combustible components are burned.
Between the refrigerating unit 15 and the internal combustion engine 16, a metering device 19 is arranged which injects additional fuel into the air-gas mixtur~ B deriving from the refrigerating unit 15.
This additional fuel quantity can be so dimensioned that the energy recovered from the internal combustion ensine 16 is sufficient to ~ ;
drive the refrigerating unit 15.
During the start-up of the entire system, the internal combustion engine 16 can be initially driven exclu!3ively by the fuel quantity injected. In the metering device 19, the injected quantity of fuel can be matchad to the fuel content in the air-gas mixture B.
From internal combustion engine 16, an exhau6t gas stream C emerges which sati~fles appliaable legal requirements or i~ slgniflcantly therebelow. -- 8 - ~
,',,`' ',~
18329 ~0 91~112~0 2~ ~99 9 6 PCT/EP91jO0095 The mechanical energy recovered by the internal combustion engine 16 is applied t~ a generator 10 in which it is transformed into electrical energy. This electrical energy is used for supply of the refrigerating unit 15. It is, however, also possible to feed this energy into the network 21.
In the cascade cooling unit 18, shown in Figure 2, the refrigerant utilized is conducted from a superpressure reservoir 1 via an :~:
expansion or depressurization control valve 2 into an evaporator 3.
The evaporator 3 has an evaporator stage 4 in which the refrigerant passes form the liquid state into the vapor state. Durlng thls transformation process, the medium to be cooled flowing past the evaporator stage 4, namely in the impure gas-air mixture, has the requisite heat quantity abstracted for evaporation of the refrig-erant. Downstream of the evaporator stage 4 is an after~evaporator stage 5 in which the vapor-form refrige;rant is heated to a tempera-ture detected by a measuring device 6 designed to control the expansion-control valve 2.
This ~fter-evaporation stage is, by corresponding structuring and arrangement of the individual parts of the evaporator with respect to the volumetric flow o~ the medium to be cooled, here the gas-air mixture to be cleaned, usable as a precooler.
.~
. .
.
18329 WO 91/11240 2 ~ ~ ~ 9 ~ ~ PCT/EP91jO0095 Downstream of the evaporator 3, the refrigerant in a conventional manner is conducted through a compressor 9 provided with an inlet .
valve 7 and an outlet valve 8, and a condenser or heat exchanger 10 back to the superpressure reservoir 1.
,'~" '`' '-The refrigerant utilized for the cooliny process has at a pressure of 1 bar, an evaporation temperature of minus 88 degrees C and is injected via a depressurization-control valve or expansion valve 2 ~ :
having at a pressure of 1 bar, an evaporation temperature of minus 45 degrees C. As a result, the following is the effect:
.
The expansion valve 2 opens at a pressure in the evaporator 3 of 3.2 :.
bar. For the refrigerant which at a pressure of 1 bar would have an ~ :
evaporation temperature of minus 45 degrees C, this would give an .:
evaporation temperature of minus 17 deg:rees C. With the refrigerant actually used, however, which has an evaporation temperature at 1 bar of minus 88 degrees C, at this pres!sure o~ 3.2 bar, the evapora- :
tion temperature is minus 65 degrees C. With a properly constructed and set evaporator 3, the expansiGn valve 2 receive~ from the pressure equalization line 11 and the ~easurin~ device 6 forming the ..
thermosensor, which is disposed downstream of the after-evaporator stage 5, the following signals: : :
-- 10 -- ' ~"' ..
f~
1832~ ~0 91/112~0 PCT/~P91jO0095 2 ~ 6 Temperature minus 7 degrees C;
Pressure 3.2 bar.
For the expansion valve 2, with respect to refri~erant ~or which it is normally designed and which at a pressure of 3.2 bar would have an evaporation temperature of minus 17 degrees C, this would mean a superheating of 10 K. The depressurization control or expansion - -valve 2 is thus in the correct operating range. However, operating with the refrigerant utilized in the present case, there is an advantage that it manifests a temperature of minus 65 degrees C at the evaporator stage 4 of the evaporator 3 and a total temperature difference betwePn this temperature and the minus 7 degrees C in the after-evaporator stage u~ed for precool.Lng.
In Figure 3, an embodiment of the evaporator 3 is illustrated in which the evaporator stage 4 and the after-evaporator stage 5 are very compact and with respect to the cooling medium flow D is so arranged that the latter initially traverses the after-evaporator stage 5 serving as precooler. To this is conneated a fir6t sec$ion of the evaporator stage 4 directly traversed by the medium flow following the after-evaporator stage 5, before it is reversed and flows over a second section of the evaporator stage 4 after which it leaves the evaporator 3 a~ the ~ubstantially clean gas-~ir ~ixture E.
In accordance with the process of patent claim S, in which the com-bustible fuel engine is continuou51y operated to generate electrical energy, the cooling or condensation stage is si~ultaneously included as part of the supply unit for the combustible-fuel engine.
Fluctuations of the fuel quantity resulting from cooling and condensation are compensated by storage of the fuel and matching metering of further fuel. An advantageous power capacity for a combustion engine operated in such manner can amount to about lO0 kW. With such continuous operation of the combustion engine, the highly volatile hydrocarbons resulting from the cooling and condensation can be utilized logically for energy generation before they are transformed in a gaseous state and can pass into the atmosphere.
;';,.~,~;.., : .. - . ., , : . . . . .. : . .: . : . :. , ~. .:. . . : . ~ ::: :. : .:: . :
18329 ~O 91/11240 2 0 '~ ~ ~ 9 6 PCT/EP91/00095 In the embodiment of the refrigeration unit according to patent claim 10, the refrigerant actually used in the evaporator stage of the evaporator passes from a liquid into the vapor state and removes from the contaminated gas or mixture the medium to be cooled -utilizing the heat of evaporation required for the change of state of the refrigerant. This evaporator stage is followed by an after--evaporator stage; in the latter the refrigerant actually used, now in vapor form, is brought from its evaporation temperature which is lower, by comparison to that of the refrigerant for which the expansion or depressurization control valve is designed by heating to a temperature corresponding to that of the tlatter3 re~rigerant at the expansion valve after e~aporation and the usual superheating.
~his allows complete utilization of the enthalpy of the refrigerant without necessitating the provision of a portion of the evaporator state ag a superheating stretch re~ulting in a loss of power.
The after-evaporation stage, in which the vapor state refrigerant actually used is heated to the temperature o~ the refriyerant for which the expansion or depressurization valve is designed after the required superheating of the latter refrigerant for this expansion .
. .
:
~ , .f~
18329 wo 91/11240 2 ~ 9 ~ PCT/EP91/00095 control valve, is utilizable as a cooling stage because of the comparatively high temperature diEference between this latter temperature and the evaporation temperature of the refrigerant actually used for the capacity thereof.
By ~orresponding constructural configuration and assembly of the evaporator stage and the after-evaporator stage, the medium to be ~ -cooled initially is passed through the after-cooling stage and then passed through the evaporator stage itself. The after-cooling stage is thus effectively used as a precooler. The control of the expansion-control valve is so effected that the refrigerant at the outlet of the evaporator assumes a pressure and temperature for which the expansion-control valve is set for control of the provided parameters. The provision of the evaporator stage according to patent claim 11 allows an especially exact control of the refrig-erant volumetric flow from the superpressure reservoir into the evaporator.
According to patent claim 12, the after-evaporator stage capacity is dimensioned to be sufficient so that even with the precooling, the ~ -temperature of the medium to be cooled is dropped significantly.
. ~ ; . , ~ .............. . . . .... .
,, , , ", ,. ,,~ . : ... , , . . ~ , ., . ;, , , ~ . , ~ ~ : . ., 18329 ~0 91/11240 PC~P91~00095 An especially advantageous operation of the refrigerating unit is effected by the provision according to claim 13 of the expansion--control valve and evaporator in combination with the refrigerant there givPn.
The invention is described in greater detail below with respect to an embodiment thereof with referance to the drawings. They show:
Figure 1 a schematic illustration of an embodiment of the process of the invention or the apparatus of the invention;
Figure 2 an embodiment oP the cascade cooling unit of Figure 1 and Figure 3 an embodimen of the evaporator shown in Figure ~.
-. . ~,:
An air-gas mixture A, which from decanting or filling contains carburetor or diesel fuel, is fed to a refrigerating unit 15. The refrigerating unit 15 is formed from a liquid cooler 17 and a cascade cooling device 18 traversed in succession by the air-~as mixture A. In the refrigerating unit 15, the air-ga~ mixture is cooled and condensed. The condensate which separates out, which is in the liquid form and contains impurities, water and hydrocarbons, is supplied to a specific-gravity separator 22 in which the different components are separated.
: ~ ' . ' " ' ' . ',, ' ' ' ';,'"
18329 WO 91/11240 PCT~EP91/00095 The air-gas mixture B from the refrigerating unit 15, which contains small quantities, still of some impurities of hydrocarbons, is supplied to a combustion-power ~internal combustion] engine lG in which the remaining combustible components are burned.
Between the refrigerating unit 15 and the internal combustion engine 16, a metering device 19 is arranged which injects additional fuel into the air-gas mixtur~ B deriving from the refrigerating unit 15.
This additional fuel quantity can be so dimensioned that the energy recovered from the internal combustion ensine 16 is sufficient to ~ ;
drive the refrigerating unit 15.
During the start-up of the entire system, the internal combustion engine 16 can be initially driven exclu!3ively by the fuel quantity injected. In the metering device 19, the injected quantity of fuel can be matchad to the fuel content in the air-gas mixture B.
From internal combustion engine 16, an exhau6t gas stream C emerges which sati~fles appliaable legal requirements or i~ slgniflcantly therebelow. -- 8 - ~
,',,`' ',~
18329 ~0 91~112~0 2~ ~99 9 6 PCT/EP91jO0095 The mechanical energy recovered by the internal combustion engine 16 is applied t~ a generator 10 in which it is transformed into electrical energy. This electrical energy is used for supply of the refrigerating unit 15. It is, however, also possible to feed this energy into the network 21.
In the cascade cooling unit 18, shown in Figure 2, the refrigerant utilized is conducted from a superpressure reservoir 1 via an :~:
expansion or depressurization control valve 2 into an evaporator 3.
The evaporator 3 has an evaporator stage 4 in which the refrigerant passes form the liquid state into the vapor state. Durlng thls transformation process, the medium to be cooled flowing past the evaporator stage 4, namely in the impure gas-air mixture, has the requisite heat quantity abstracted for evaporation of the refrig-erant. Downstream of the evaporator stage 4 is an after~evaporator stage 5 in which the vapor-form refrige;rant is heated to a tempera-ture detected by a measuring device 6 designed to control the expansion-control valve 2.
This ~fter-evaporation stage is, by corresponding structuring and arrangement of the individual parts of the evaporator with respect to the volumetric flow o~ the medium to be cooled, here the gas-air mixture to be cleaned, usable as a precooler.
.~
. .
.
18329 WO 91/11240 2 ~ ~ ~ 9 ~ ~ PCT/EP91jO0095 Downstream of the evaporator 3, the refrigerant in a conventional manner is conducted through a compressor 9 provided with an inlet .
valve 7 and an outlet valve 8, and a condenser or heat exchanger 10 back to the superpressure reservoir 1.
,'~" '`' '-The refrigerant utilized for the cooliny process has at a pressure of 1 bar, an evaporation temperature of minus 88 degrees C and is injected via a depressurization-control valve or expansion valve 2 ~ :
having at a pressure of 1 bar, an evaporation temperature of minus 45 degrees C. As a result, the following is the effect:
.
The expansion valve 2 opens at a pressure in the evaporator 3 of 3.2 :.
bar. For the refrigerant which at a pressure of 1 bar would have an ~ :
evaporation temperature of minus 45 degrees C, this would give an .:
evaporation temperature of minus 17 deg:rees C. With the refrigerant actually used, however, which has an evaporation temperature at 1 bar of minus 88 degrees C, at this pres!sure o~ 3.2 bar, the evapora- :
tion temperature is minus 65 degrees C. With a properly constructed and set evaporator 3, the expansiGn valve 2 receive~ from the pressure equalization line 11 and the ~easurin~ device 6 forming the ..
thermosensor, which is disposed downstream of the after-evaporator stage 5, the following signals: : :
-- 10 -- ' ~"' ..
f~
1832~ ~0 91/112~0 PCT/~P91jO0095 2 ~ 6 Temperature minus 7 degrees C;
Pressure 3.2 bar.
For the expansion valve 2, with respect to refri~erant ~or which it is normally designed and which at a pressure of 3.2 bar would have an evaporation temperature of minus 17 degrees C, this would mean a superheating of 10 K. The depressurization control or expansion - -valve 2 is thus in the correct operating range. However, operating with the refrigerant utilized in the present case, there is an advantage that it manifests a temperature of minus 65 degrees C at the evaporator stage 4 of the evaporator 3 and a total temperature difference betwePn this temperature and the minus 7 degrees C in the after-evaporator stage u~ed for precool.Lng.
In Figure 3, an embodiment of the evaporator 3 is illustrated in which the evaporator stage 4 and the after-evaporator stage 5 are very compact and with respect to the cooling medium flow D is so arranged that the latter initially traverses the after-evaporator stage 5 serving as precooler. To this is conneated a fir6t sec$ion of the evaporator stage 4 directly traversed by the medium flow following the after-evaporator stage 5, before it is reversed and flows over a second section of the evaporator stage 4 after which it leaves the evaporator 3 a~ the ~ubstantially clean gas-~ir ~ixture E.
Claims (13)
1. Process for recovering hydrocarbons from a gas-air mixture derived from decanting or loading of carburetor or diesel fuel, in which the gas-air mixture is cooled and brought to condensation, the hydrocarbons remaining in the gas-air mixture after condensation are burned in an internal combustion engine and the energy generated by the internal combustion engine is used for cooling and condensation, characterized in, that by the cooling and condensation of the gas--air mixture it is cleaned substantially completely from hydro-carbons and other impurities and that in the gas-air mixture down-stream from the cooling condensation, fuel is injected.
2. Process according to claim 1, characterized in, that the energy generated in the internal combustion engine drives a generator whose electrical energy is used for cooling and condensation or fed to a [electrical] net.
3. Process according to claim 1 or 2, characterized in, that downstream of the cooling and condensation, fuel is injected in a quantity which together with the hydrocarbon remaining still contained in the gas-air mixture is sufficient for the cooling and condensation.
4. Process according to one of claims 1 - 3, characterized in, that the condensate separated off by the cooling and condensation is divided into its components by specific gravity separation.
5. Process according to claim 1, 2 or 4, characterized in, that the fuel injected into the gas-air mixture downstream of the cooling and condensation at least partly is withdrawn from a gasoline storage in which the hydrocarbons resulting from the cooling and condensation are collected and that such an amount of fuel is injected in the gas-air mixture downstream of the cooling and condensation that the internal combustion engine is driven continuously with a predeter-mined output power.
6. Apparatus for recovery of hydrocarbons from a gas-air mixture resulting from the decanting or loading of carburetor fuel or diesel fuel, with a refrigerating unit (15), in which the gas-air mixture is cooled and brought to condensation, an internal combustion engine (16), which is disposed downstream of the refrigerating unit (15) in which the hydrocarbons remaining yet in the gas-air mixture after the condensation are burned and the generated energy is useful to drive the refrigerating unit (15), characterized in, that the refrigerating unit (15) has a liquid cooler (17) and a cascade cooling device (18) in which the hydrocarbons and impurities are substantially completely separated out of the gas-air mixture, and that between the refrigerating unit (15) and the internal combustion engine (16) a metering device (19) is provided by means of which the gas-air mixture coming out of the refrigerating unit (15) is charged with fuel.
7. Apparatus according to claim 6, characterized in, that a generator (20) is connected to the internal combustion engine (16) by means of which the mechanical energy generated by the internal combustion engine (16) is converted into electrical energy and the electrical energy is useful to drive the refrigerating unit (16) or is feedable into [electrical] net (21).
8. Apparatus according to claim 6 or 7, characterized in, that the metering device (19) is adjustable, that such an amount of fuel is injected into the gas-air mixture that the fuel quantity supplied to the internal combustion engine is sufficient to maintain the opera-tion of the refrigerating unit (15).
9. Apparatus according to one of the claims 6 - 8, characterized in, that a specific gravity separator 22 is connected to the refrigerating unit (15) in which the condensate separated in the refrigerating unit (15) is separable into its components.
10. Apparatus according to one of the claims 6 - 9, characterized in, that the cascade cooling device (18) is provided with an expansion control valve set for a particular refrigerant which controls the volumetric flow of a refrigerant from a superpressure reservoir (1) into an evaporator, on the output region of which a measuring device (6) is arranged which detects the suction gas temperature of the vaporized refrigerant which and the constant suction gas pressure corresponding to the opening setting of the expansion control valve (2) is adjustable, whereby instead of the given refrigerant, a refrigerant is used which has a lower vaporiza-tion temperature, and whereby an evaporator (3) has an after--evaporation stage (5) which heats the refrigerant used to temperature which corresponds to that of the given refrigerant after its evaporation and a superheating.
11. Apparatus according to claim 10, characterized in, that the after-evaporation stage (5) of the evaporator (3) is so configured that the refrigerant actually used has a temperature at the evaporator output which corresponds to that of the given refrigerant after its evaporation and a superheating of 10 Kelvin.
12. Apparatus according to one of the claims 6 - 11, characterized in, that a pressure of 1 bar of the given refrigerant, the expansion or depressurization control valve (2) is set correspondingly for vaporization temperature of minus 40 degrees c and that the actually used refrigerant has a vaporization temperature of minus 88 degrees C.
13. Apparatus according to claim 12, characterized in, that the expansion valve (2) for a vaporization pressure of 3.2 bar which opens at an evaporation temperature of the given refrigerant of minus 17 degrees C opens for the actually-used refrigerant at minus 65 degrees C, and the after-evaporator stage (5) is so constructed that the actually-used refrigerant at the evaporator output has a temperature of minus 7 degrees C.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEP4002123.8 | 1990-01-25 | ||
| DE4002123A DE4002123A1 (en) | 1990-01-25 | 1990-01-25 | METHOD AND DEVICE FOR RECOVERY OF HYDROCARBONS FROM A GAS-AIR MIXTURE |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2049996A1 true CA2049996A1 (en) | 1991-07-26 |
Family
ID=6398746
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA 2049996 Abandoned CA2049996A1 (en) | 1990-01-25 | 1991-01-19 | Process and device for recovering hydrocarbons from a gas-air mixture |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP0464167A1 (en) |
| JP (1) | JPH04504606A (en) |
| CA (1) | CA2049996A1 (en) |
| DE (1) | DE4002123A1 (en) |
| WO (1) | WO1991011240A1 (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE4002123A1 (en) * | 1990-01-25 | 1991-08-01 | Hoelter Heinz | METHOD AND DEVICE FOR RECOVERY OF HYDROCARBONS FROM A GAS-AIR MIXTURE |
| JP4786593B2 (en) * | 2007-05-11 | 2011-10-05 | オリオン機械株式会社 | VOC cooling recovery equipment |
| JP4786591B2 (en) * | 2007-05-11 | 2011-10-05 | オリオン機械株式会社 | VOC cooling recovery equipment |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4110091A (en) * | 1973-07-20 | 1978-08-29 | Linde Aktiengesellschaft | Process for the separation of a gaseous mixture consisting of water vapor, hydrocarbons, and air |
| DE3609292A1 (en) * | 1985-10-15 | 1987-04-16 | Linde Ag | METHOD FOR REMOVING IMPURITIES FROM A GAS |
| DE4002123A1 (en) * | 1990-01-25 | 1991-08-01 | Hoelter Heinz | METHOD AND DEVICE FOR RECOVERY OF HYDROCARBONS FROM A GAS-AIR MIXTURE |
-
1990
- 1990-01-25 DE DE4002123A patent/DE4002123A1/en not_active Withdrawn
-
1991
- 1991-01-19 WO PCT/EP1991/000095 patent/WO1991011240A1/en not_active Application Discontinuation
- 1991-01-19 CA CA 2049996 patent/CA2049996A1/en not_active Abandoned
- 1991-01-19 EP EP19910902181 patent/EP0464167A1/en not_active Ceased
- 1991-01-19 JP JP50244991A patent/JPH04504606A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| EP0464167A1 (en) | 1992-01-08 |
| WO1991011240A1 (en) | 1991-08-08 |
| DE4002123A1 (en) | 1991-08-01 |
| JPH04504606A (en) | 1992-08-13 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request | ||
| FZDE | Dead |