U.S. patent number 3,857,251 [Application Number 05/315,931] was granted by the patent office on 1974-12-31 for lng storage tank vapor recovery by nitrogen cycle refrigeration with refrigeration make-up provided by separation of same vapor.
This patent grant is currently assigned to Technigaz. Invention is credited to Jean Alleaume.
United States Patent |
3,857,251 |
Alleaume |
December 31, 1974 |
**Please see images for:
( Certificate of Correction ) ** |
LNG STORAGE TANK VAPOR RECOVERY BY NITROGEN CYCLE REFRIGERATION
WITH REFRIGERATION MAKE-UP PROVIDED BY SEPARATION OF SAME VAPOR
Abstract
Method and device of treatment of natural gas contained in
storage tanks, for producing liquid nitrogen by extraction of
nitrogen from the vapours resulting from the evaporation of said
liquefied natural gas in said tanks, liquefaction of a portion of
said extracted nitrogen and storage thereof for forming a reserve
of cold.
Inventors: |
Alleaume; Jean (Saint-Cloud,
FR) |
Assignee: |
Technigaz (Paris,
FR)
|
Family
ID: |
9088163 |
Appl.
No.: |
05/315,931 |
Filed: |
December 18, 1972 |
Foreign Application Priority Data
|
|
|
|
|
Dec 27, 1971 [FR] |
|
|
71.46842 |
|
Current U.S.
Class: |
62/623; 62/47.1;
62/50.5 |
Current CPC
Class: |
F25J
1/0221 (20130101); F25J 1/0072 (20130101); F25J
1/0282 (20130101); F25J 1/0284 (20130101); F25J
3/0233 (20130101); F25J 1/0052 (20130101); F25J
1/0242 (20130101); F25J 1/0045 (20130101); F25J
1/0265 (20130101); F25J 1/0277 (20130101); F17C
9/04 (20130101); F25J 3/0257 (20130101); F25J
1/0025 (20130101); F25J 3/0209 (20130101); F25J
1/0251 (20130101); F25J 1/0281 (20130101); F25J
1/005 (20130101); F25J 1/0288 (20130101); F25J
1/025 (20130101); F25J 1/0202 (20130101); F25J
1/0204 (20130101); F25J 2230/20 (20130101); F25J
2200/76 (20130101); F25J 2210/62 (20130101); F25J
2200/74 (20130101); F25J 2270/42 (20130101); F25J
2200/02 (20130101); F25J 2210/90 (20130101); F25J
2215/04 (20130101); F25J 2270/16 (20130101); F25J
2270/06 (20130101); F25J 2220/62 (20130101); F17C
2265/015 (20130101) |
Current International
Class: |
F17C
9/00 (20060101); F17C 9/04 (20060101); F25J
1/00 (20060101); F25J 3/02 (20060101); F25J
1/02 (20060101); F25j 003/02 () |
Field of
Search: |
;62/40,54,9,11,27,28,38,39,28,40,23 |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Monacell; A. Louis
Assistant Examiner: Sever; Frank
Attorney, Agent or Firm: Kenyon & Kenyon Reilly Carr
& Chapin
Claims
What is claimed is:
1. A device for treatment of natural gas stored in liquefied state,
comprising: tank means containing said liquefied natural gas and
including a stop vapor space filled with the gaseous phase
consisting of the vapors resulting from the boil-off of said
liquefied-natural-gas; fractional distillating column means
comprising 9 bottom collecting sump portion for holding
reliquefied-natural-gas, an overhead vapor space collecting top
portion for confining separated gaseous nitrogen and intermediate
upper and lower portions and a sump portion; first vapor conveying
duct means connecting said top vapor space of said tank means to
said intermediate lower portion of said fractional distillating
column means; first vapor pump means inserted in said first duct
means and having its suction side communicating with said top vapor
space and its discharge side communicating with said fractional
distillating column means; reboiler vessel means including a lower
liquid phase holding portion for containing reboiling
liquefied-natural-gas and an upper gaseous phase holding portion
for confining vapors of liquefied-natural-gas; heat exchange pipe
coil means contained within said lower liquid phase holding
portion; first liquid-conveying duct means connecting said sump
portion of said fractional distillating column means to the inlet
of said lower liquid phase holding portion of said reboiler vessel
means; first liquid pump means inserted in said second cut means
and having its suction side communicating with said sump portion of
said fractional distillating column means and its discharge side in
communication in communication with said lower liquid phase holding
portion of said reboiler vessel means; second liquid-conveying duct
means connecting the outlet of said lower liquid phase holding
portion of said reboiler vessel means with said top vapor space of
said tank means; second vapor-conveying duct means connecting said
upper gaseous phase holding portion of said reboiler vessel means
to said intermediate lower portion of said fractional distillating
column means; container means containing liquid-nitrogen and
including a top vapor space filled with the gaseous phase released
by the boil-off of said liquid-nitrogen; reflux condenser drum
means immersed in said liquid-nitrogen within said container means
and including a condensate holding portion containing
liquid-nitrogen and a vapor holding portion filled with gaseous
nitrogen; third liquid-conveying duct means connecting said
condensate holding portion of said reflux condenser drum means to
said intermediate upper portion of said fractional distillating
column means; second liguid pump means inserted in said third
liquid-conveying duct means and having its suction side
communicating with said condensate holding portion of said reflux
condenser drum means and its discharge side communicating with said
intermediate upper portion of said fractional distillating column
means; third vapor-conveying duct means connecting said overhead
collecting top portion of said fractional distillating column means
to the inlet of an immersed portion of said vapor holding portion
of said reflux condenser drum means; main gaseous flow heat
exchanger means having a refrigerating medium flow lath and a
heating medium flow path respectively interconnected in series,
said treating medium flow path including pipe coil means
interconnected in series within said heating medium flow path of
said main heat exchanger means; fourth vapor-conveying duct means
connecting the outlet of said top vapor space of said container
means to the inlet of said refrigerating medium flow path of said
main gaseous flow heat exchanger means; second gas pump means
inserted in said fourth vapor-conveying duct means and having its
suction side communicating with said top vapor space of said
container and its discharge side communicating with said
refrigerating medium flow path of said main gaseous flow heat
exchanger means; power dirven compressor means with at least one
compression stage having an inlet and an outlet connected to the
refrigerating medium flow path and to the heating medium flow path,
respectively, of said main heat exchanger means; and cold phase
separator means including a condensate holding portion for
containing liquid-nitrogen and a vapor holding portion for
confining non-condensed gaseous nitrogen; fourth liquid-conveying
duct means connecting said condensate holding portion of said cold
phase separator means into the body of liquid nitrogen contained in
said container; an outlet and an inlet of said vapor holding
portion of said cold phase separator being connected to the inlet
of the refrigerating medium flow path and to the outlet of the
heating medium flow path, respectively, of said main heat exchanger
means.
2. A method of progressively cryogenically purifying a stored
stationary body of liquefied-natural-gas containing at least a
major portion of methane and a substantial amount of nitrogen mixed
therewith by continuous cyclic process comprising the steps of:
providing a stored stationary body of liquid nitrogen; collecting
the boil-off forming the gaseous phase built up on the top of said
body of liquefied-natural-gas; effecting a fractional distillation
of said boil-off through heat exchange with a boiling refrigerant
by using a cold reflux liquid previously separated and
reliquefied-nitrogen whereby the nitrogen contained in said
boil-off is separated as a gas therefrom and the so purified
remaining boil-off is reliquefied; collecting the purified
hydrocarbon-enriched reliquefied natural gas resulting as the
bottoms from said fractional distillation and returning it to said
body of liquefied-natural-gas which is thus also gradually
enriched; collecting the separated overhead gaseous nitrogen and
the gaseous nitrogen resulting from evaporation of said reflux
liquid and conveying same in a confined condition into said body of
liquid-nitrogen in heat exchanging relationship therewith so as to
condense at least a part of said gaseous nitrogen, the nitrogen
condensate serving as said reflux liquid; recovering the cold
gaseous nitrogen evaporated from said body of liquid-nitrogen and
that resulting from said nitrogen distillate; reliquefying said
recovered gaseous nitrogen and feeding the reliquefield-nitrogen
back to said body of liquid-nitrogen, reboiling at least one
portion of said collected reliquefied-natural-gas at the boiling
temperature of a nitrogen-free liquid-natural-gas through heat
exchange with hot gaseous nitrogen derived from the nitrogen
reliquefaction cycle and feeding the vapors of
liquefied-natural-gas resulting from said reboiling step to said
fractional distillation step to supply reboiling heat thereto, said
hot gaseous nitrogen being cooled thereby, while the reboiled
substantially nitrogen-free liquid-natural-gas is returned to said
body of liquefied-natural-gas; whereas said reliquefying of said
recovered gaseous nitrogen comprises the steps of: reheating said
cold recovered gaseous nitrogen through heat exchange with hot
compressed gaseous nitrogen which is cooled thereby; compressing
said heated gaseous nitrogen in at least one stage and after
cooling same at least through said heat exchange with said cold
recovered gaseous nitrogen and with said reboiling purified liquid
natural gas; subjecting said cooled compressed gaseous nitrogen to
at least one first cold phase separation for condensing at least a
part of said gaseous nitrogen; collecting and returning said
condensed liquid-nitrogen to said body of liquid-nitrogen; said
method also comprising the steps of: collecting the cold compressed
gaseous nitrogen which has not been condensed during said cold
phase separation; expanding at least one portion thereof in at
least one stage while recovering work produced by said expansion
and using said work as power for assisting the compression step;
preheating at least one portion of said expanded gaseous nitrogen
through heat exchange with that compressed gaseous nitrogen which
is about to undergo said cold phase separation thereby further
cooling said last-named compressed gaseous nitrogen; and mixing
said preheated compressed gaseous nitrogen with the stream of said
recovered gaseous nitrogen arriving from said body of
liquid-nitrogen before further preheating same.
3. A method of progressively cryogenically purifying a stored
stationary body of liquefied natural gas containing at least a
major portion of methane and a substantial amount of nitrogen mixed
therewith by a continuous cyclic process comprising the steps of:
providing a stored stationary body of liquid-nitrogen; collecting
the boil-off forming the gaseous phase built up on the top of said
body of liquefied-natural-gas; effecting a fractional distillation
of said boil-off through heat exchange with a boiling refrigerant
by using a cold reflux liquid previously separated and reliquefied
nitrogen whereby the nitrogen contained in said boil-off is
separated as a gas therefrom and the sopurified remaining boil-off
is reliquefied; collecting the purified hydrocarbon-enriched
reliquefied natural gas resulting as the bottoms from said
fractional distillation and returning it to said body of
liquefied-natural-gas which is thus also gradually enriched;
collecting the separated overhead gaseous nitrogen and the gaseous
nitrogen resulting from evaporation of said reflux liquid and
conveying same in a confined condition into said body of
liquid-nitrogen in heat exchanging relationship therewith so as to
condense at least a part of said gaseous nitrogen, the nitrogen
condensate serving as said reflux liquid; recovering the cold
gaseous nitrogen evaporated from said body of liquid-nitrogen and
that resulting from said nitrogen distillate; reliquefying said
recovered gaseous nitrogen and feeding the reliquefied nitrogen
back to said body of liquid-nitrogen, reboiling at least one
portion of said collected reliquefied-natural-gas at the boiling
temperature of a nitrogen-free liquid natural gas through heat
exchange with hot gaseous nitrogen derived from the nitrogen
reliquefaction cycle and feeding the vapors of
liquefied-natural-gas resulting from said reboiling step to said
fractional distillation step to supply reboiling heat thereto, said
hot gaseous nitrogen being cooled thereby, while the reboiled
substantially nitrogen-free liquid-natural-gas is returned to said
body of liquefied natural gas; whereas said reliquefying of said
recovered gaseous nitrogen comprises the steps of: reheating said
cold recovered gaseous nitrogen through heat exchange with hot
compressed gaseous nitrogen which is cooled thereby; compressing
said heated gaseous nitrogen in at least one stage and aftercooling
same at least through said heat exchange with said cold recovered
gaseous nitrogen and with said reboiling purified
liquid-natural-gas; subjecting said cooled compressed gaseous
nitrogen to at least one first cold phase separation for condensing
at least a part of said gaseous nitrogen; collecting and returning
said condensed liquid-nitrogen to said body of liquid nitrogen; and
said method comprising further the steps of collecting the cold
compressed gaseous nitrogen which has not been condensed during
said cold phase separation; preheating at least one portion thereof
through heat exchange with that compressed gaseous nitrogen which
is about to undergo said cold phase separation thereby further
cooling said last-named compressed gaseous nitrogen; and mixing
said preheated compressed gaseous nitrogen with the stream of said
recovered gaseous nitrogen arriving from said body of liquid
nitrogen before further preheating same; expanding another portion
of said non-condensed gaseous nitrogen and recovering the work
produced thereby as power for assisting the compression step; and
mixing said expanded portion with said one portion before
preheating the same.
4. A device according to claim 1, comprising aftercooling means
inserted in series between the outlet of each stage of said
compressor means and the inlet of the heating medium flow path of
said main heat exchanger means and extraneous coolant circulating
means, said aftercooler means being cooled by the circulation of
extraneous coolant of said extraneous coolant circulating
means.
5. A device according to claim 1, comprising work-producing gas
expansion means having its inlet connected to another outlet of the
vapor holding portion of said cold phase separator means and its
outlet connected to an inlet of the refrigerating medium flow path
of said main heat exchanger means.
6. A device according to claim 5, wherein said work-producing gas
expansion means comprises a tubular thermal separator.
7. A device according to claim 5, wherein said work-producing gas
expansion means comprising at least one reciprocating piston engine
coupled to at least one piston compressor forming compressor means
and motor means, said compressor means also being operatively
connected to motor means.
8. A device according to claim 7 wherein said work-producing gas
expansion means comprises turbine means having at least one stage,
compressor means which comprise multiple stages, interstage cooler
means separating said multiple stages and extraneous coolant means
for said stages said turbine means and said compression means being
directly coupled and operatively connected to said motor means.
9. A device according to claim 1, wherein said main heat exchanger
means comprise first and second heat exchangers whose said pipe
coil means are interconnected.
10. A device according to claim 5, comprising further gas flow heat
exchanger means having a heating medium flow path connected in
series between the outlet of the heating medium flow path of said
main heat exchanger means and said inlet of the vapor holding
portion of said cold phase separator means and a refrigerating
medium flow path connected in series between said inlet of the
refrigerating medium flow path of said main heat exchanger means
and on the other hand said one outlet of the vapor holding portion
of said cold phase separator means and said outlet of said
work-producing gas expansion means.
11. A device according to claim 10, wherein said cold phase
separator means consist of first and second cold phase separators,
the outlet of the condensate holding portion of said first cold
phase separator being connected to the inlet of the vapor holding
portion of said second cold phase separator whereas the outlet of
the heating medium flow path of said further heat exchanger means
is connected to an inlet of the vapor holding portion of said first
cold phase separator and the outlet of said first cold phase
separator is connected to the inlet of said work-producing gas
expansion means, the outlet of the vapor holding portion of said
second cold phase separator being connected to the inlet of the
refrigerating medium flow path of said further heat exchanger
means.
12. A device according to claim 1, including a conduit connecting
the outlet of the refrigerating medium flow path of said main
exchanger means to the inlet of said compressor means and
controllable vent pipe means branched off said conduit.
13. A device according to claim 1, including third liquid pump
means at least the suction side of which is immersed in the
liquefied-natural-gas contained in said tank means; pipe line means
leading from the discharge side of said third liquid pump means to
the outside of said tank means towards a consumer station and
auxiliary heat exchanger means comprising a heating medium flow
path connected to the coolant outlet of said aftercooling means and
a refrigerating medium flow path inserted in series in said pipe
line means.
14. A device according to claim 13, including additional heat
exchanger means comprising a heating medium flow path having an
inlet connected through branch duct means to said pipe line means
downstream of said auxiliary heat exchanger means and an outlet
connected to the top vapor space of said tank means, and a
refrigerating medium flow path inserted in series into said pipe
line means upstream of said auxiliary heat exchanger means.
15. A device according to claim 1, wherein said power driven
compressor means comprise a plurality of separate, respectively low
intermediate and high pressure turbine-motor-compressor sets having
each one a workproducing gas expansion turbine, a motor and a
compressor, and drive shaft means, said drive shaft means
operatively and mechanically coupling each set, the gas flow path
of said compressors being interconnected in series and inserted
between the outlet of the refrigerating medium flow path entering
the low pressure compressor and the inlet of the heating medium
flow path fed by the final high pressure compressor to said main
heat exchanger means, with interstage extraneous gas coolant
supplied cooler means connected in series between any two
successive compressors and gas aftercooler means cooled by said
extraneous coolant connected in series between the outlet of said
high pressure compressor and the inlet of the heating medium flow
path of said main heat exchange means; said cold phase separator
means comprising a primary cold phase separator whose vapor holding
portion is connected through an outlet to the inlet of the turbine
of the final high pressure turbine-motor-compressor set and a like
plurality of secondary cold phase separators associated with said
plurality of turbine-motor-compressor sets, respectively; a like
plurality of further gas flow heat exchangers also associated with
said turbine-motor-compressor sets, respectively, the heating
medium flow paths of which are interconnected in series and
inserted between the outlet of the heating medium flow path of said
main heat exchanger means and an inlet of the vapor holding portion
of said primary cold phase separator; the condensate holding
portion of said primary cold phase separator being connected to an
inlet of the vapor holding portion of the first secondary cold
phase separator; the vapor holding portion of each secondary cold
phase separator being connected through an outlet to the inlet of
the refrigerating medium path of the associated further heat
exchanger, the outlet of which is connected to the inlet of the
turbine of the next successive turbine-motor-compressor set, except
for the corresponding outlet of the further heat exchanger
associated with the first or low pressure turbine-motor-compressor
set which outlet is connected to the inlet of the refrigerating
medium flow path of said main heat exchanger means; the condensate
holding portion of each secondary cold phase separator being
connected through an inlet to the outlet of the turbine of the
associated turbine-motor-compressor set through an outlet to an
inlet of the vapor holding portion of the next secondary cold phase
separator, except for the outlet of the last secondary cold phase
separator associated with the first or low pressure
turbine-motor-compressor set which outlet is connected to said
fourth liquid-conveying duct means.
16. A device according to claim 15, wherein each
turbine-motor-compressor set comprises multiplying gear means with
two output shafts operatively coupled to drive shafts of said
turbine and said compressor, respectively, and with an input shaft
operatively coupled to said motor, said compressor having an
axially directed gas inlet and a tangentially directed gas
outlet.
17. A device according to claim 15, mounted on board a ship and
wherein the turbine-motor and compressor of each
turbine-motor-compressor set are housed in a same casing and said
motor comprises a steam turbine whose steam pressure is slightly
lower than the gas pressure in said gas flow path.
18. A method according to claim 3, wherein said cold phase
separation comprises a first separation producing liquid nitrogen
which is subject to a second separation producing liquid nitrogen
which is returned to said body of liquid nitrogen whereas the
non-condensed gaseous nitrogen resulting from said first separation
is expanded and mixed with the non-condensed gaseous nitrogen
resulting from said second separation.
Description
The present invention relates to a method of treatment of natural
gas contained in a liquefied state in storage and/or transportation
tanks, of the type consisting in producing liquid nitrogen by
utilizing, to this end, the boil-off of the liquefied natural gas,
the methane and higher-hydrocarbon fraction of which is
simultaneously re-liquefied, as well as a device for carrying out
said method, usable especially on board methane tankers or in land
storage plants.
The invention aims at providing simple means for producing liquid
nitrogen usable partly as a cold-producing fluid for the
re-liquefaction of methane, and partly for sale.
The resulting simplification enables liquefaction units to be
obtained which are sufficiently compact and economical to be used
on board methane tankers or in liquefied-natural-gas land storage
plants. To this end, the invention provides a method of treatment
of natural gas contained in a liquefied state in storage and/or
transportation tanks, of the type consisting in producing liquid
nitrogen from the boil-off of the liquefied gas and characterized
in that nitrogen is extracted from the vapours resulting from the
evaporation of the liquefied natural gas contained in the said
tanks, at least a portion of the extracted nitrogen is liquefied
and the liquid nitrogen is stored as a reserve of cold.
After the liquefied natural gas has been unloaded, use is made of
the said reserve of cold to pre-cool the tanks and fill them with
an inert atmosphere before again filling the tanks with liquefied
natural gas.
As compared with the known methane liquefaction methods comprising
an indirect cycle using in particular nitrogen as a cold-producing
fluid, the method of the present invention differs therefrom by the
fact that the nitrogen used in an open circuit as a cold-producing
fluid is extracted from the evaporations of the liquefied natural
gas conveyed in the tanks of methane tankers or stored in land
reservoirs. One of the main advantages offered by the invention
results from the fact that the nitrogen extracted from the
liquefied natural gas is free from interfering impurities such as
steam, carbon dioxide, sulphur oxide, oxygen and so forth, which
are present in the gases usually employed for the production of
liquid nitrogen (atmospheric air or gases resulting from
combustion).
Another advantage lies in the fact that the nitrogen extracted from
the liquefied-natural-gas evaporations already has a temperature
close to that of liquid methane, i.e. about -160.degree. C under
the usual conditions of transportation and storage of the liquefied
natural gases. This low initial temperature of the nitrogen
contained in the liquefied natural gas reduces the amount of cold
necessary to liquefy the same and, in case of partial liquefaction
of the available nitrogen, the nitrogen which is rejected to the
atmosphere in a gaseous state supplies previously the frigories
corresponding to its sensible heat, thus facilitating the
reliquefaction of the nitrogen fraction entering the cycle.
This results in a substantial reduction of the refrigerating power
which is necessary to enable the indirect cycle using nitrogen as a
cold-producing fluid to ensure the re-liquefaction of the total
amount of methane which is present in the or boil-off of the
contents of the tanks of the methane tankers or the land storge
plant.
According to another feature of the invention, the method of
re-liquefaction of the methane vapours resulting from the
evaporation of liquefied natural gas, with simultaneous extraction
of nitrogen, consists in treating the liquefied-natural-gas vapours
by way of cryogenic distillation or fractioning by bringing them
into contact with a reflux liquid rich in nitrogen, so as to obtain
gaseous nitrogen, on the one hand, and a condensed hydrocarbon
mixture practically free from nitrogen, on the other hand, the
latter then being returned into the liquefied-natural-gas tanks.
The cold for the condenser of the distillation column is provided
by the evaporation of the liquid nitrogen contained in a reservoir.
The liquid-nitrogen vapours of the reservoir are mixed with the
gaseous nitrogen extracted from the natural gas in order to be
introduced into a nitrogen re-liquefaction cycle.
The invention is also characterized by a device for the
re-liquefaction of liquefied-natural-gas vapours and simultaneous
extraction of nitrogen, the said device comprising a column for the
cryogenic distillation or fractioning of liquefied-natural-gas
vapours, connected, on the one hand, to the liquefied-natural-gas
tanks by a vapour supply conduit and by a re-boiler drum for the
return of the said condensed hydrocarbon mixture to the said tanks,
and, on the other hand, to a reflux drum placed in the said
liquid-nitrogen reservoir, the said reflux drum comprising a return
outlet to the said distillation column and a second outlet to the
said nitrogen re-liquefaction cycle.
The invention therefore results in a highly profitable exploitation
of, for instance, a methane tanker, for it makes it possible, by
means of an insignificant energy make-up, to re-liquefy all the
liquid-natural-gas evaporation while extracting simultaneously the
nitrogen contained in the liquid-natural-gas vapours, and to thus
form a liquid nitrogen reserve capable of providing high-potential
cold which can be used on board the tanker for the pre-cooling of
the tanks and the tank filling conduits, for preparing a further
liquid-natural-gas cargo, or on land for all the known uses of
liquid nitrogen.
Where the invention is applied to stationary land-storage tanks, it
makes it possible not only to re-liquefy all the methane vapours
resulting from the evaporation of the liquefied natural gas, to
enrich the liquefied natural gas, but also to extract the nitrogen
contained in the said natural gas and store the liquid nitrogen
thus obtained. The nitrogen extracted from the natural-gas vapours
is practically pure and free from interfering impurities, and can
be sold at interesting prices.
The invention will be better understood and other objects,
characteristics and advantages thereof will appear as the following
description proceeds, with reference to the appended drawings given
solely by way of example illustrating several forms of embodiment
of the invention and wherein:
FIG. 1 is a general diagrammatic view of a plant according to the
invention, applicable to a methane tanker or a stationary storage
plant;
FIG. 1a is a simplified diagrammatic view of the same plant;
FIG. 2 is a general diagrammatic view of an alternative of
embodiment of the invention;
FIG. 3 is a diagrammatic view of one exemplary embodiment of a
compressor and a turbine used in the invention;
FIG. 4 is a view of another embodiment of a compressor and a
turbine according to the invention;
FIG. 5 is a graphic representation of the nitrogen re-liquefaction
and refrigeration cycle according to the invention.
In the exemplary embodiment of the invention illustrated in FIG. 1,
a liquefied-natural-gas tank is shown at 1 and a liquid nitrogen
reservoir is designated by the reference numeral 2. The
liquid-natural-gas vapours are sucked by a blower 3 into a conduit
4 and are conveyed into a cryogenic distillation or fractioning
column 5. The column 5 is connected, on the one hand, to a
re-boiler drum 6 through a supply conduit 7, a re-liquefied
natural-gas pump 8 and through a return conduit 9 for the
liquefied-natural-gas vapours. On the other hand, the column 5 is
connected to a reflux drum 10 placed within the liquid nitrogen
reservoir 2, through a nitrogen vapour supply conduit 11, and a
conduit 12 with a pump 13 for the return of liquid nitrogen into
the said column.
The circuit of re-liquefaction of the liquefied-natural-gas vapours
proceeding from the tank 1 is shown in thicker lines.
The gaseous nitrogen proceeding from the reflux drum 10 and
resulting from the liquid-nitrogen evaporations obtained in the
tank 2 is conveyed by the conduits 14 and 15 into the nitrogen
liquefaction circuit. This circuit comprises a conduit 16
connected, on the one hand, to the conduits 14 and 15 and, on the
other hand, to a blower 47 delivering into a series of heat
exchangers 17, 18, 19 which are intended to heat the gaseous
nitrogen, a multi-stage compressor 20 driven by a motor 21, a heat
exchanger 22, using for instance water or any other suitable
cooling fluid such as air, propane, ammonia, freon and so forth,
serving to cool the nitrogen compressed in the compressor 20.
The compressed nitrogen then re-passes through the coil 23 of the
heat exchanger 19, the coil 24 of the heat exchanger 25, and then
the coils 26, 27, 28 of, respectively, the heat exchanger 18, the
reboiler drum 6 and the heat exchanger 17. The nitrogen thus cooled
passes through the coil 29 of a heat exchanger 30 before being
introduced into cold separates 31 and 32. The liquid nitrogen
collected at the bottom of the cold separator 31 is conveyed
through a conduit 33 into the cold separator 32, and the liquid
nitrogen collected in this second cold separator 32 returns to the
reservoir 2 through a conduit 34. The gaseous nitrogen contained in
the first cold separator 31 is conveyed through a conduit 35 into
an expansion-with-work plant 36 which may be constituted by a
two-stage turbine or a thermal separator of a known type,
comprising a group of pipes closed at one end and in which the gas
is subjected to expansion with work, the corresponding energy being
released in the form of heat, or still by a reciprocating-motion
expansion machine coupled for instance to a piston compressor.
The gaseous nitrogen expanded in the plant 36 is mixed with the
gaseous nitrogen resulting from the second cold separator 32 and
then passes through the heat exchanger 30 where it cools the
nitrogen passing through the coil 29 and is injected into the said
nitrogen liquefaction circuit through the conduit 16 before the
heat exchanger 17.
The distillation column 5, the re-boiler drum 6, the heat
exchangers 17, 18, 30, the cold separators 31 and 32, the
expansion-with-work plant 36 are placed in a chamber filled with
low-temperature gaseous nitrogen, the said chamber being shown in
FIG. 1 by the dotted outline 40.
The device just described operates as follows:
The liquefied-natural-gas vapours are conveyed from the tank 1 into
the fractioning column 5 where they are cooled by contact with the
liquid rich in nitrogen proceeding from the reflux drum 10. The
nitrogen contained in the natural-gas vapours remains in a gaseous
state, whereas the tower bottom liquid, which is constituted by a
mixture rich in hydrocarbons and poor in nitrogen, is then returned
to the re-boiler drum 6. The latter is at the boiling temperature
of nitrogen-free liquid-natural-gas, so that the hydrocarbon
mixture returned into the tank 1 contains practically no
nitrogen.
The vapours from the top of the distillation column 5 are conveyed
into the reflux drum 10 where they are partially liquefied. The
distillate consitituted by the remaining gaseous nitrogen is
conveyed into the previously described nitrogen liquefaction
circuit where it is first successively heated in the exchangers 17,
18 and 19 and then compressed in the compressor 20, cooled by
passing through the coils of the exchangers 19, 20, 25, 18, 17, 30,
and then either condensed in the cold separators 31 and 32 or
expanded in the plant 36 and recycled into the liquefaction
circuits.
In case of nitrogen overproduction, the gaseous nitrogen may be
made to escape to open air through the conduit 41 placed right
before the compressor. Use may also be made of the heat exchangers
22 and 25 to heat the liquefied natural gas contained in the tank 1
and intended for either the boiler of a tanker or a network for
distribution to consumers.
In this case, the natural gas is delivered by a pump 42 into the
coil 43 of a heat exchanger 44, and then into the coil 45 of a
second heat exchanger 46, supplied, for instance, with
high-temperature water from the heat exchanger 22. The natural gas
thus vaporized may either pass through the heat exchanger 25 where
it takes heat from the compressed nitrogen, or be used directly. A
portion of the natural gas vaporized at the outlet of the exchanger
46 is conveyed into the exchanger 44 to vaporize the liquid natural
gas.
An alternative of embodiment of the invention is shown in FIG. 2,
wherein, instead of arranging on one and the same shaft-line the
motor 21, the multi-stage compressor 20 and the multi-stage
expansion plant 36, the same function may be fulfilled by grouping
on three different shaft-lines an electric motor (or a steam
turbine), a single-stage or two-stage compressor and a single-stage
or two-stage expansion plant. In this case, it is preferable to
select comparable pressure levels for the outlet of a compressor
and the inlet of the corresponding turbine in each of the modules
thus formed. This, indeed, enables the thrust on the shaft bearings
of the modules to be reduced.
According to this modification of the invention, the compression
and expansion circuit for the gaseous nitrogen, shown in FIG. 2,
comprises three electric motors 51, 52, 53 which may also be
replaced by steam turbines, three compressors 54, 55, 56 ensuring
low-pressure, medium-pressure and high-pressure levels
respectively. With each of these motor-compressor sets are
respectively associated turbines 57, 58, 59 for the expansion of
the compressed nitrogen.
In this case, the gaseous nitrogen, after having passed through the
exchangers 17, 18, 19, passed successively through the three
compression stages 54, 55, 65 and is cooled after each compression
in a heat exchanger 60 using for instance water or any other
suitable refrigerating fluid, the circulation pumps and circuits of
which are not shown. Thereafter, the nitrogen repasses, as in the
first embodiment, through the heat exchangers 19, 18, the re-boiler
drum 6 and the exchanger 17. The compressed nitrogen then passes
through the coils of three exchangers 61, 62, 63 and then arrives
in a first cold separator 64 wherefrom the gaseous nitrogen is
conveyed to the turbine 59 and the liquid nitrogen is conveyed to a
second cold separator 65. The gaseous nitrogen partially expanded
in the turbine 59 passes through the cold separator 65 and then
through the heat exchanger 63 and the second turbine 58. The liquid
nitrogen proceeding from the cold separator 65 is injected into a
third separator 66 into which is also conveyed the expanded gaseous
nitrogen proceeding from the turbine 58. The gaseous nitrogen
contained in the separator 66 is again conveyed into an exchanger
62 and then passes in the turbine 57 where it is expanded and then
conveyed into a fourth cold separator 67. Likewise, the liquid
nitrogen from the separator 66 is returned into the separator 67.
The gaseous nitrogen from the latter separator then passes through
the heat exchanger 61 and is injected at the beginning of the
nitrogen liquefaction cycle, before the exchanger 17.
FIG. 3 illustrates an example of embodiment of a
motor-compressor-turbine set corresponding to one of the sets used
in the embodiment shown in FIG. 2. In this case, the motor, for
instance 51, is connected through a step-up gear 70 and bearings
71, 72, to the compressor 54 and the turbine 57. In the example
illustrated, the compressor 54 is provided with a tangential outlet
and an axial inlet.
On board ships, where an auxiliary boiler is generally available
for the ship's steam requirements, it is preferable to form the
motor-compressor-turbine sets by using a steam turbine instead of
the motor, a centrifugal compressor and a centripetal expansion
turbine as shown in FIG. 4. The steam turbine 80, the compressor 81
and the expansion turbine 82 are mounted in one and the same body.
The latter, as well as the volutes and diffusers of the expansion
turbine, are made from cyrogenic metal. The various elements are
assembled within the common body through the medium of
heat-insulating members arranged to avoid any heat-conducting
bridges between the said elements. Moreover, the pressure of the
steam used in the turbine 81 is slightly lower than the nitrogen
pressure in order to avoid any pollution of the nitrogen by the
steam at the rotary joints.
The main advantage of the arrangement just described consists in
the use of a modular construction system and in that the power used
in each module is only a fraction of the total power, thus
facilitating the supply of energy by the networks on board a ship.
Moreover, it is possible to achieve various dimensions and
rotational speeds in each of the modules.
The nitrogen cooling cycle according to the invention is
illustrated in FIG. 5, where the entropy values S are plotted in
abscissae against enthalpy values H plotted in ordinates.
At A, nitrogen is vaporized through condensation of the
liquefied-natural-gas vapours in the distillation column 5. The
line A B shows the heating of the gaseous nitrogen in the heat
exchangers 17, 18, 19, whereas the line B C corresponds to the
compression of the nitrogen in a four-stage compressor 20. The
curve C D corresponds to the cooling of the nitrogen compressed in
the exchangers 22, 19, 25, 18, 27, 17, 29 and the cold separators
31 and 32. The line D E corresponds to the expansion of the gaseous
nitrogen in the plant 36, whereas the dotted line E A represents
the vaporization of the liquid nitrogen and the compression of the
vapour in the blower 3.
Owing to the method and device of the invention, the production of
nitrogen on board a methane tanker is always much higher than the
quantity of liquid nitrogen consumed by the ship, either to
compensate for the regrigerant fluid losses in the natural-gas
vapour re-liquefaction unit, or to pre-cool and to fill the tanks
with an inert atmosphere. In the case of a methane tanker having
just received a natural-gas cargo, the tank 1 is, of course, full
of liquefied natural gas. So is the reservoir 2, the liquid
nitrogen contained in the latter having been produced mainly during
the empty return trip of the methane tanker. Since the tank 1 is
practically full, the distillation column 5 operates at its full
working rate since, the amount of methane to be re-liquefied being
at a maximum. Part of the necessary cold may be obtained by slowly
vaporizing the liquid nitrogen of reservoir 2. During the return
trip, when the tanks 1 have been emptied, the volume of gas
conveyed to the distillation tower is greatly reduced. Indeed, the
boil-off in the liquefied-natural-gas tanks is reduced when the
latter contain only a small amount of liquid. The refrigerating
capacity necessary to re-liquefy the methane is therefore reduced
and the plant may be used to condensate a larger fraction of the
nitrogen contained in these evaporations. The liquid nitrogen thus
produced accumulates in the reservoir 2 which progressively fills
during the return trip. enables
The volume of nitrogen conveyed to the compressor therefore differs
very little from that conveyed to the compressor during the outward
trip, in the course of which the tanks 1 are practically full and
the reservoir 2 empties. Thus, the time difference in phase of the
variations of the levels in the liquefied-natural-gas tanks 1 and
in the liquid nitrogen reservoir results in a regulation of the
rate of flow from the compressor and from the expansion plant 36.
The relatively regular use of these machines emables them to be
better dimensioned.
In case the invention is applied to land storage tanks, the heat
exchanger 25 enables the cold of the natural gas to be recovered
and used to produce an additional amount of liquid nitrogen, which
is stored in the reservoir 2. In the same manner as on board
methane tankers, the volume of nitrogen sucked by the nitrogen
compressor remains substantially constant in time.
Considering the case of a natural gas, the nitrogen content of
which is not negligible, such as, for instance, Algerian natural
gas, at least ten times the amount of nitrogen necessary for the
ship's needs is available, in which case the excess nitrogen is
rejected to the atmosphere after having given up all its sensible
heat (from -150.degree. to +10.degree.C approximately) to the
nitrogen which is to be re-liquefied. This additional quantity of
cold is far from being negligible and the refrigerating power to be
supplied for the re-liquefaction of the liquefied-natural-gas
vapours is thus reduced by about 12 percent.
In the case of land storage, the nitrogen produced in excess is
stored and then sold.
Of course, the invention is by no means limited to the forms of
embodiment described and illustrated, which have been given by way
of example only. In particular, it comprises all the means
constituting technical equivalents to the means described as well
as their combinations, should the latter be carried out according
to the spirit of the invention.
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