U.S. patent application number 10/469090 was filed with the patent office on 2004-04-15 for method for ethane recovery, using a refrigeration cycle with a mixture of at least two coolants, gases obtained by said method, and installation therefor.
Invention is credited to Paradowski, Henri.
Application Number | 20040069015 10/469090 |
Document ID | / |
Family ID | 8860440 |
Filed Date | 2004-04-15 |
United States Patent
Application |
20040069015 |
Kind Code |
A1 |
Paradowski, Henri |
April 15, 2004 |
Method for ethane recovery, using a refrigeration cycle with a
mixture of at least two coolants, gases obtained by said method,
and installation therefor
Abstract
The invention concerns a method and an installation for
refrigerating gas mixtures, for cryogenic separation of a
pressurised gas (1) constituents. The method comprises a
refrigerating cycle wherein a fluid (13) is separated in a
separator tank (B2) into a less volatile fraction (4), for
producing refrigeration at a relatively high first temperature in
an exchanger (E1), and into a more volatile second fraction (5) for
producing refrigeration at a relatively low temperature in an
exchanger (E2). The heated and expanded fractions (4, 5) are
brought together then compressed in a compressor (K1). A fraction
(26) derived from said compressor (K1) is cooled to supply the
fraction (13).
Inventors: |
Paradowski, Henri; (Cergy,
FR) |
Correspondence
Address: |
OSTROLENK FABER GERB & SOFFEN
1180 AVENUE OF THE AMERICAS
NEW YORK
NY
100368403
|
Family ID: |
8860440 |
Appl. No.: |
10/469090 |
Filed: |
August 25, 2003 |
PCT Filed: |
February 4, 2002 |
PCT NO: |
PCT/FR02/00419 |
Current U.S.
Class: |
62/620 |
Current CPC
Class: |
F25J 2210/12 20130101;
F25J 2205/04 20130101; C07C 7/09 20130101; F25J 3/0209 20130101;
F25J 3/0219 20130101; F25J 2215/62 20130101; F25J 3/0238 20130101;
F25J 2205/82 20130101; F25J 2200/02 20130101; F25J 2270/902
20130101; F25J 3/0233 20130101; C07C 7/09 20130101; F25J 2270/12
20130101; F25J 2200/74 20130101; F25J 2270/18 20130101; F25J
2270/66 20130101; C07C 9/06 20130101 |
Class at
Publication: |
062/620 |
International
Class: |
F25J 003/00 |
Foreign Application Data
Date |
Code |
Application Number |
Feb 26, 2001 |
FR |
0102582 |
Claims
1. A process for recovering the ethane contained in a pressurized
gas (1) containing methane and C.sub.2 and higher hydrocarbons,
operating a refrigerating cycle in which a relatively less-volatile
first refrigerant (2) is compressed, cooled and expanded in order
thereafter to be used for cooling said pressurized gas (1) to be
separated or first separation products to a relatively high first
temperature, and in which a relatively more-volatile second
refrigerant (3) is compressed, cooled and expanded in order
thereafter to be used for cooling at least second separation
products obtained from said pressurized gas (1) to a relatively low
second temperature *1, *2 characterized in that the first and
second refrigerants (2, 3) are used as a mixture when they are
compressed and cooled, in that this mixture then undergoes a
separation into a first fraction (4) essentially containing the
relatively less-volatile first refrigerant (2) and into a second
fraction (5) essentially containing the relatively more-volatile
second refrigerant (3), in that the first refrigerant is used in
the form of the first fraction, for cooling to the relatively high
first temperature, and in that the second refrigerant is used in
the form of the second fraction, for cooling to the relatively low
second temperature.
2. The process as claimed in claim 1, characterized in that the
first fraction (4) is cooled in a first exchanger (E1), expanded to
give a first expanded fraction (6), then warmed in said first
exchanger, before being introduced into a low-pressure stage (7) of
a compressor (K1).
3. The process as claimed in claim 2, characterized in that the
second fraction (5) is cooled in the first exchanger (E1) and then
in a second exchanger (E2), expanded, then warmed in said second
exchanger and mixed with the expanded first fraction (6).
4. The process as claimed in claim 2 or claim 3, characterized in
that a third fraction (8) is tapped off the first fraction (4)
after it has been cooled in the first heat exchanger (E1) and in
that said third fraction (8) is expanded and warmed in said first
exchanger (E1) in order to deliver an expanded and warmed fourth
fraction (9), which is introduced into a medium-pressure stage (10)
of the compressor (K1).
5. The process as claimed in claim 4, characterized in that a
gaseous fifth fraction (11) is tapped off from the refrigerants
undergoing compression in the compressor (K1) at a medium pressure,
slightly above that of the expanded and warmed fourth fraction (9),
and is cooled and expanded to the same pressure as said fourth
fraction (9) and then mixed with the latter.
6. The process as claimed in any one of the preceding claims,
characterized in that said first and second refrigerants (2, 3) are
used as a mixture with a third refrigerant (12).
7. The process as claimed in claim 6, characterized in that the
refrigerants are methane, ethylene and propane.
8. A methane-enriched gas obtained by the process as claimed in one
of the preceding claims.
9. An ethane-enriched product obtained by the process as claimed in
one of claims 1 to 7.
10. A product enriched with C.sub.2 and higher hydrocarbons,
obtained by the process as claimed in one of claims 1 to 7.
11. A plant for recovering the ethane contained in a pressurized
gas (1) containing methane and C.sub.2 and higher hydrocarbons,
this plant comprising means for compressing, cooling and expanding
a relatively less-volatile first refrigerant (2), means for
cooling, by means of the first refrigerant, said pressurized gas
(1) to be separated or first separation products to a relatively
high first temperature, and means for compressing, cooling and
expanding a relatively more-volatile second refrigerant (3), means
for cooling, by means of the second refrigerant (3), at least
second separation products obtained from said pressurized gas (1)
to a relatively low second temperature, characterized in that the
first and second refrigerants (2, 3) are used as a mixture when
they are compressed and cooled and in that this plant comprises
means for this mixture to undergo a separation into a first
fraction (4) essentially containing the relatively less-volatile
first refrigerant (2) and into a second fraction (5) essentially
containing the relatively more-volatile second refrigerant (3), the
first refrigerant being used in the form of the first fraction for
cooling to the relatively high first temperature and the second
refrigerant being used in the form of the second fraction for
cooling to the relatively low second temperature.
Description
[0001] The present invention relates in general, and according to a
first of its aspects, to the gas industry, and in particular to a
method of recovering the ethane contained in a pressurized gas
comprising methane and C.sub.2 and higher hydrocarbons, operating a
multicomponent refrigeration cycle.
[0002] The term "multicomponent refrigeration cycle" should be
understood to mean a refrigeration cycle using a refrigerant
mixture composed of at least two refrigerants.
[0003] More precisely, the invention relates, according to its
first aspect, to a process for recovering the ethane contained in a
pressurized gas containing methane and C.sub.2 and higher
hydrocarbons, operating a refrigerating cycle in which a relatively
less-volatile first refrigerant is compressed, cooled and expanded
in order thereafter to be used for cooling said pressurized gas to
be separated or first separation products to a relatively high
first temperature, and in which a relatively more-volatile second
refrigerant is compressed, cooled and expanded in order thereafter
to be used for cooling at least second separation products obtained
from said pressurized gas to a relatively low second
temperature.
[0004] Refrigeration processes of this type are well known to those
skilled in the art and have been used for many years.
[0005] These refrigeration processes have drawbacks as regards
operating costs, because of energy consumption associated with the
low thermodynamic efficiency of these refrigeration cycles.
[0006] Such known processes also have drawbacks as regards
operating costs generated by maintenance difficulties and by the
frequency of intervention work, for example on compression plants,
pumps or else on measurement and control equipment.
[0007] These drawbacks themselves entail excessive costs that
extend the period of amortization of the financial investment in
such plants because of production stoppages.
[0008] In this context, it is a first object of the present
invention to provide a process, which moreover is in accordance
with the generic definition given in the above preamble, which is
essentially characterized in that the first and second refrigerants
are used as a mixture when they are compressed and cooled, in that
this mixture then undergoes a separation into a first fraction
essentially containing the relatively less-volatile first
refrigerant and into a second fraction essentially containing the
relatively more-volatile second refrigerant, in that the first
refrigerant is used in the form of the first fraction, for cooling
to the relatively high first temperature, and in that the second
refrigerant is used in the form of the second fraction, for cooling
to the relatively low second temperature.
[0009] This process allows the operating costs of the plant,
especially as regards energy consumption, to be limited by a higher
thermodynamic efficiency, and also, as regards maintenance, by
reducing the number of items of equipment in the plant by combining
two refrigeration circuits into a single one. Thus, the maintenance
operations are simplified, the time required to determine the
causes of a failure of the plant is shortened and, consequently,
any production stoppage will be shorter than when plants using a
process according to the prior art are used.
[0010] According to a first aspect of the process of the invention,
the first fraction may be cooled in a first exchanger, expanded to
give a first expanded fraction, then warmed in the first exchanger,
before being introduced into a low-pressure stage of a
compressor.
[0011] According to the first aspect of the process of the
invention, the second fraction may be cooled in the first exchanger
and then in a second exchanger, expanded, then warmed in the second
exchanger and mixed with the expanded first fraction.
[0012] According to the first aspect of the process of the
invention, a third fraction may be tapped off the first fraction
after it has been cooled in the first heat exchanger and the third
fraction may be expanded and warmed in the first exchanger in order
to deliver an expanded and warmed fourth fraction, which may be
introduced into a medium-pressure stage of the compressor.
[0013] According to the first aspect of the process of the
invention, a gaseous fifth fraction may be tapped off from the
refrigerants undergoing compression in the compressor (K1) at a
medium pressure, slightly above that of the expanded and warmed
fourth fraction, and then cooled and expanded to the same pressure
as said fourth fraction and then mixed with the latter.
[0014] According to a second aspect of the process of the
invention, the first and second refrigerants can be used as a
mixture with a third refrigerant.
[0015] According to the second aspect of the process of the
invention, the refrigerants may be methane, ethylene, and
propane.
[0016] According to a third of its aspects, the invention relates
to a methane-enriched gas and to an ethane-enriched product that
are obtained by the present process as well as to a product
enriched in C.sub.2 and higher hydrocarbons, obtained by the
present process.
[0017] According to a fourth of its aspects, the invention relates
to a plant for recovering the ethane contained in a pressurized gas
containing methane and C.sub.2 and higher hydrocarbons, operating
in particular a multicomponent refrigeration cycle, this plant
using a refrigeration cycle and comprising means for compressing,
cooling and expanding a relatively less-volatile first refrigerant,
means for cooling, by means of the first refrigerant, said
pressurized gas to be separated or first separation products to a
relatively high first temperature, and means for compressing,
cooling and expanding a relatively more-volatile second
refrigerant, means for cooling, by means of the second refrigerant,
at least second separation products obtained from said pressurized
gas to a relatively low second temperature, characterized in that
the first and second refrigerants are used as a mixture when they
are compressed and cooled and in that this plant comprises means
for this mixture to undergo a separation into a first fraction
essentially containing the relatively less-volatile first
refrigerant and into a second fraction essentially containing the
relatively more-volatile second refrigerant, the first refrigerant
being used in the form of the first fraction for cooling to the
relatively high first temperature and the second refrigerant being
used in the form of the second fraction for cooling to the
relatively low second temperature.
[0018] The invention will be more clearly understood and further
objects, features, details and advantages thereof will become more
clearly apparent in the course of the description that follows,
with reference to the appended schematic drawings given solely by
way of example but implying no limitation, and in which:
[0019] FIG. 1 shows a functional block diagram of a plant according
to one embodiment of the prior art;
[0020] FIG. 2 shows a functional block diagram of a plant according
to a preferred embodiment of the invention.
[0021] The following symbols may in particular be read from both
these figures: "FC" stands for "flow controller", "GT" stands for
"gas turbine", "LC" stands for "liquid level controller", "PC"
stands for "pressure controller", "SC", stands for "speed
controller" and "TC" stands for "temperature controller".
[0022] For the sake of clarity and conciseness, the lines used in
the plants shown in FIGS. 1 and 2 will be indicated by the same
reference numbers as the gaseous fractions that flow therein.
[0023] Referring to FIG. 1, the plant shown is intended for
treating a dry charge gas, in particular for isolating therefrom,
on the one hand, a fraction composed mainly of methane essentially
free of C.sub.2 and higher hydrocarbons and, on the other hand, a
fraction composed mainly of ethane and other C.sub.2 and higher
hydrocarbons essentially free of methane.
[0024] This plant has three independent circuits. A first circuit
corresponds to the path followed by a gas to be purified, a second
circuit corresponds to the cooling cycle of a refrigeration unit,
the refrigerant of which is ethylene, and a third circuit
corresponds to the cooling cycle of a refrigeration unit whose
refrigerant is propane.
[0025] More precisely, in the first circuit, a charge gas 1,
available at 15.degree. C. and 18 bar, with a flow rate of 3903
kmol/h, is cooled in an exchanger E1 in order to deliver a cooled
gas 302 at -17.52.degree. C. and 17.8 bar. The latter is further
cooled in a second exchanger E2, in order to deliver a partially
condensed, cooled fluid 303 at -30.00.degree. C. and 17.6 bar. The
stream 1 is composed of 0.1% carbon dioxide, 24.3% methane, 74.4%
ethane and 1.2% propane.
[0026] The fluid 303 is then introduced into a tank V1 where it
undergoes separation of its liquid and gaseous constituents:
[0027] the gas phase, stream 304, available with a flow rate of
2219 kmol/h, is cooled to -60.degree. C. and partially condensed in
an exchanger E3 in order to deliver a fluid 305 at 17.4 bar. This
fluid 305 feeds a distillation column T1 in its upper part;
[0028] the liquid phase, stream 306, available with a flow rate of
1684 kmol/h, is pumped by a pump P1, flows in a line that includes
a controlled valve 321, the opening of which depends on a liquid
level controller present in the tank V1, in order to deliver a
stream 307 at -29.8.degree. C. and 19.6 bar. The latter stream is
then introduced into a middle part of the distillation column
T1.
[0029] Produced at the top of the column T1 is a vapor 308 at
-65.79.degree. C. and 17.2 bar, available with a flow rate of 1358
kmol/h, which is cooled in an exchanger E4 in order to deliver a
partially condensed fluid 309 at -90.degree. C. and 17.0 bar. This
fluid is then separated in a tank V2 into a gas fraction 310 in an
amount of 971 kmol/h, composed of 0.1% carbon dioxide, 94.9%
methane and 5.0% ethane, and into a liquid fraction 311 in an
amount of 387 kmol/h, composed of 0.4% carbon dioxide, 47.6%
methane and 52.0% ethane, which is pumped by a pump V2 along a line
312. This line 312 includes a controlled-opening valve 322, the
opening of which depends on the flow rate in this same line.
[0030] The liquid fraction transported in the line 312 is then
introduced into the last stage of the column T1.
[0031] The gas fraction 310 coming from the tank V2, at a
temperature of -90.0.degree. C., flows through a heat exchanger E6
in order to deliver a warmed fraction 313 at -35.0.degree. C., this
fraction 313 then flows through a heat exchanger E7 in order to
deliver a warmed fraction 326, before passing into a
controlled-opening valve 317, the opening of which depends on the
pressure in the line 326. On leaving the valve 317, the product is
collected in a delivery line 320 at 20.0.degree. C. and leaves the
plant.
[0032] In its lower part, the distillation column T1 has several
trays that are connected in pairs via warming circuits, two of
which have been shown. These are the circuits 315, 316 and 318,
319. Each of these warming circuits constitutes a lateral reboiler
in the case of the circuit 315, 316 and a column bottom reboiler in
the case of the circuit 318, 319.
[0033] The fluid flowing in the line 315, with a flow rate of 3000
kmol/h and at a temperature of -20.26.degree. C., is warmed in the
heat exchanger E1 by heat exchange with the charge gas 1 in order
to deliver a warmed fluid 316 at -16.61.degree. C. which is then
introduced onto a tray below the tray where the withdrawal of the
fluid 315 takes place. The temperature of the fluid flowing in this
circuit 315, 316 is regulated by means of a controlled-opening
valve 323 placed in a branch line of the circuit 315, 316 that does
not pass through the exchanger E1. The opening of this valve 323 is
controlled by a temperature controller connected to the line
302.
[0034] Similarly, the fluid flowing in the line 318 with a flow
rate of 3341 kmol/h. and at a temperature of -16.15.degree. C.,
which is located at a stage below the stage where the warmed fluid
316 is introduced, is warmed in a heat exchanger E5 by heat
exchange with a refrigerant consisting of propane, in order to
deliver a warmed fluid 319 at -14.87.degree. C. This fluid is
introduced onto a tray below the tray from which the fluid 318 is
withdrawn. The temperature of the fluid flowing in this circuit
318, 319 is regulated by means of a controlled-opening valve 324,
placed in a branch line for the refrigerant transported in lines
220, 221, which branch line does not pass through the exchanger E5.
The opening of this valve 324 is controlled by a temperature
controller connected to the line 319.
[0035] Finally, the residual liquid obtained at the bottom of a
column T1, which is enriched in C.sub.2 and higher hydrocarbons, is
withdrawn at a temperature of -14.87.degree. C. and a pressure of
17.4 bar, in an amount of 2932 kmol/h via a line 314. The latter
has a valve 325, the opening of which is controlled by a liquid
level controller for the liquid at the bottom of column T1.
[0036] In the second circuit, which corresponds to the cooling
cycle of a refrigeration unit whose refrigerant is ethylene, a
stream of liquid ethylene 100 with a flow rate 2570 kmol/h, a
temperature of -30.degree. C. and a pressure of 19.58 bar is
withdrawn from a storage tank V5. This stream 100 is divided
into:
[0037] (a) a first stream 117 with a flow rate of 1993 kmol/h,
which is expanded to 6.79 bar and cooled to -63.degree. C. by
passing it through a valve 120 in order to deliver a stream 101
that is mixed with a stream 104 in order to give a stream 102 that
feeds the exchanger E3 with refrigerating ethylene. The opening of
the valve 120 is controlled by a liquid level controller in the
exchanger E3;
[0038] (b) a second stream 114 with a flow rate of 577 kmol/h which
is expanded to 18.58 bar and cooled to -80.degree. C. in the
exchanger E6 in order to give a warmed stream 115.
[0039] The 577 kmol/h of the stream 115 are divided into:
[0040] (a) 417 kmol/h constituting a first stream 116 which is
expanded to 1.83 bar and cooled to -93.degree. C. by passing
through a valve 121 in order to deliver a stream 106 that feeds the
exchanger E4 with refrigerating ethylene. The opening of the valve
121 is controlled by a liquid level controller contained in the
exchanger E4. In addition, this liquid level controller is
servocontrolled by another liquid level controller contained in the
separating tank V2;
[0041] (b) 160 kmol/h constituting a second stream, that flows in a
line 105 provided with a valve 122, the opening of which depends on
the flow rate in the line 105, in order to give a stream 104 at
-79.62.degree. C. and 6.79 bar. This stream 104 is mixed with the
stream 101 in order to give a stream 102, prior to it being
introduced into the exchanger E3.
[0042] Vaporizing the ethylene contained in the exchanger E4 allows
the stream 8 coming from the top of the column T1 to be cooled. The
ethylene vapor thus obtained--stream 107 at -93.degree. C. and 1.83
bar--is sent into the low-pressure stage of the compressor K1,
passing via the suction tank V3.
[0043] Vaporizing the ethylene contained in the exchanger E3 allows
the stream 4 coming from the tank V1 to be cooled. The ethylene
vapor thus obtained--stream 103 at -62.83.degree. C. and 6.79
bar--is sent into the medium-pressure stage of the compressor K1,
passing via the suction tank V4.
[0044] The compressed ethylene obtained at the outlet of K1
delivers a fluid 112 at 17.75.degree. C. and 20.6 bar with a flow
rate of 2570 kmol/h, which is cooled and condensed by successively
passing through the exchanger E8, to give a fraction 118 at
-7.degree. C. and 20.1 bar, and then the exchanger E9, to give a
fraction 119 at -30.degree. C. and 19.6 bar, before feeding the
tank V5 with liquid ethylene.
[0045] In the third circuit, corresponding to the cooling cycle of
a refrigeration unit whose refrigerant is propane, a pressurized
stream 220 of liquid propane with a flow rate of 4340 kmol/h is
withdrawn from a storage tank V6 at 42.degree. C. and 18 bar. This
stream 220 is cooled in the exchanger E5 by heat exchange with the
liquid flowing in the lines 18, 19 in order to deliver a cooled
fluid 221 at 33.64.degree. C. and 17.5 bar. In parallel with the
cooling circuit, passing through the exchanger E5, a line having a
valve 24 allows the energy exchanges within E5 to be regulated.
[0046] The 4340 kmol/h of the cooled fluid 221 are then separated
into two streams:
[0047] a first stream 200 of 4030 kmol/h, which is expanded by
passing through a valve 226 in order to deliver a stream 201 at
3.46 bar and -10.degree. C. The opening of the valve 226 is
controlled by a liquid level controller contained in the exchanger
E8. The stream 201 feeds the exchanger E8 with refrigerating
propane;
[0048] a second stream 222 of 310 kmol/h, which is cooled in the
exchanger E7 in order to give the stream 223 at -25.degree. C.
[0049] The stream 223 is expanded by passing through a valve 229,
the opening of which is controlled by the flow rate in the line, to
give an expanded stream 224 at 1.48 bar.
[0050] The stream of propane 201 introduced into the exchanger E8
is partially vaporized in order to give a vapor phase 203 in an
amount of 1387 kmol/h and a liquid phase 204 in an amount 2643
kmol/h. This stream 204 is divided into two streams:
[0051] 1700 kmol/h constituting a stream 205, which is expanded by
passing through a valve 227, the opening of which depends on the
liquid level contained in the exchanger E9, in order to deliver a
stream 206 at 1.48 bar and -33.degree. C. that feeds the exchanger
E9 with refrigerating propane;
[0052] 943 kmol/h constituting a stream 208 which is expanded by
passing through a valve 228, the opening of which depends on the
liquid level contained in the exchanger E2, in order to deliver a
stream 225 at 1.48 bar and -33.degree. C., which feeds the
exchanger E2 with refrigerating propane.
[0053] The streams 225 and 224 are merged, prior to their being
introduced into the exchanger E2, to give a stream 209.
[0054] Vaporizing the propane in the exchanger E2 allows the stream
2 to be cooled and partially condensed. The propane vapor thus
obtained--stream 210 at -33.degree. C. and 1.48 bar--is mixed with
a gas stream 207 coming from the exchanger E9 in order to give a
stream 211 which is sent firstly to a suction tank V7 and then sent
to the low-pressure stage of a compressor K2.
[0055] Vaporizing the propane in the exchanger E9 allows the stream
118 to be cooled and partially condensed. The propane vapor thus
obtained--stream 207 at -33.degree. C. and 1.48 bar--is mixed with
the gas stream 210 coming from the exchanger E9 in order to give
the stream 211, which is sent firstly to the suction tank V7 and
then sent to the low-pressure stage of the compressor K2.
[0056] Vaporizing the propane in the exchanger E8 allows the stream
112 to be cooled and partially condensed. The propane vapor thus
obtained--stream 203 at -10.degree. C. and 3.46 bar--is firstly
sent to the suction-tank V8 and then sent to the medium-pressure
stage of the compressor K2.
[0057] The compressor K2 delivers a stream 217 of hot compressed
propane gas at 78.02.degree. C. and 18.6 bar, with a flow rate of
4340 kmol/h. This stream 217 is cooled in a first exchanger E10, to
deliver a cooled stream 218 at 52.36.degree. C. and 18.3 bar, and
then in a second exchanger E11, to deliver a liquid stream 219 at
42.degree. C. and 18.0 bar. The latter liquid is then stored in the
tank V6.
[0058] Referring now to FIG. 2, the plant shown is intended for
treating a dry charge gas, in particular for isolating therefrom,
on the one hand, a fraction composed mainly of methane essentially
free of C.sub.2 and higher hydrocarbons and, on the other hand, a
fraction composed mainly of ethane and other C.sub.2 and higher
hydrocarbons essentially free of methane.
[0059] This plant has two independent circuits. A first circuit
corresponds to the path followed by a gas to be purified and a
second circuit corresponds to the cooling cycle of a refrigeration
unit, the refrigerant of which is a mixture of at least three
different products that may in particular be propane, ethylene and
methane.
[0060] More precisely, in the first circuit, a charge gas 1,
available at 15.degree. C. and 18 bar, with a flow rate of 3903
kmol/h is cooled to -60.degree. C. and 17.7 bar in an exchanger E1,
which here is a plate exchanger, in order to deliver a cooled gas
303. The latter feeds a distillation column T1 in its upper part.
The stream 1 is composed of 0.1% carbon dioxide, 24.3% methane,
74.4% ethane and 1.2% propane.
[0061] In the same way as in the process described in FIG. 1, a
vapor 308 is produced at the top of column T1, at -66.21.degree. C.
and 17.0 bar and a flow rate of 1342 kmol/h, which is cooled in an
exchanger E2 in order to deliver a partially condensed fluid 309.
The streams 308 and 309 are composed of 0.16% carbon dioxide, 81.8%
methane and 18.0% ethane. The stream 309 is then separated in a
tank V2 into a gas fraction 310 and into a liquid fraction 311.
This liquid fraction 311 is transported under gravity in a line
that includes a controlled-opening valve 322, the opening of which
depends on the liquid level in the tank V1.
[0062] The liquid fraction 311 is then introduced into the final
stage of the column T1.
[0063] The gas fraction 310 coming from the tank V2 is composed of
0.1% carbon dioxide, 94.9% methane and 5.0% ethane. This fraction
enters a heat exchanger E2 at -90.degree. C. in order to deliver a
warmed fraction 326 at -70.degree. C., then passes in succession
through the exchanger E1 and through a controlled valve 317, the
opening of which depends on the pressure in the line 326. On
leaving the valve 317, the product is collected in a delivery line
320 at 39.degree. C. and leaves the plant.
[0064] In its lower part, the distillation column T1 has several
trays that are connected in pairs via warming circuits, two of
which are shown. These are the circuits 315, 316 and 318, 319. Each
of these warming circuits constitutes a lateral boiler in the case
of the circuit 315, 316 and a column bottom reboiler in the case of
the circuit 318, 319.
[0065] The fluid flowing in the line 315 with a flow rate of 1000
kmol/h and a temperature of -40.7.degree. C. is warmed in the heat
exchanger E1 in order to deliver a warmed fluid 316 at
-19.14.degree. C. This is then introduced onto a tray below the
tray from which the fluid 315 is withdrawn. The temperature of the
fluid flowing in this circuit 315, 316 is regulated by means of a
controlled-opening valve 323 placed in a branch line of the circuit
15, 16, which branch line does not pass through the exchanger E1.
The opening of this valve 323 is controlled by a temperature
controller connected to the line 316 downstream of the point where
the fluids flowing in the line 316 mixes with the fluid flowing in
the branch line with the valve 323.
[0066] Similarly, the fluid flowing in the line 318 with a flow
rate of 3790 kmol/h and a temperature of -17.36.degree. C. is
warmed in the heat exchanger E1 in order to deliver a warmed fluid
319 at -14.94.degree. C. This is then introduced onto a tray below
the tray from which the fluid 318 is withdrawn. The temperature of
the fluid flowing in this circuit 318, 319 is regulated by means of
a controlled-opening valve 324 placed in a branch line of the
circuit 315, 316, which branch line does not pass through the
exchanger E1. The opening of this valve 324 is controlled by a
temperature controller connected to the line 316 downstream of the
point where the fluid flowing in the line 319 mixes with the fluid
flowing in the branch line with the valve 324.
[0067] Finally, the residual liquid obtained at the bottom of the
column T1, which is enriched with C.sub.2 and higher hydrocarbons,
is withdrawn via a line 314 that has a valve 325 whose opening is
controlled by a liquid level controller for the liquid in the
bottom of the column T1. This liquid, available at -14.94.degree.
C. and 17.4 bar, is composed of 0.1% carbon dioxide, 1% methane,
97.4% ethane and 1.5% propane.
[0068] In the second circuit, corresponding to the cooling cycle of
a refrigeration unit whose refrigerant is a mixture of at least
three products, a refrigerating mixture 13 composed of 5% methane
12, 25% ethylene 3, and 70% propane 2, at a temperature of
42.degree. C. and at a pressure of 27.79 bar, and the flow rate of
which is 3970 kmol/h, is separated in a tank V2 into a first
fraction 4 essentially containing the less-volatile first
refrigerant 2 and into a second fraction 5 essentially containing
the more-volatile second refrigerant 3 and the more-volatile third
refrigerant 12.
[0069] The stream 5, constituting the vapor phase of the separating
tank V2, which is composed of 9.8% methane, 36.3% ethylene and
53.9% propane and the flow rate of which is 1469 kmol/h, is cooled
and condensed in the exchanger E1 in order to give a stream 14
available at -60.degree. C.
[0070] The stream 14 is then cooled in an exchanger E2 in order to
give a stream 15 available at -90.degree. C. and 27.1 bar. This
stream 15 is expanded in a valve 16 to give a stream 17 at a
pressure of 2.3 bar and a temperature of -96.degree. C. The opening
of the valve 16 is regulated by a temperature controller in the
line 310.
[0071] The stream 17 is warmed in the exchanger E2 and partially
vaporizes, so as to meet the refrigeration requirements of the
exchanger E2, in order to deliver the stream 18 at a temperature of
-67.9.degree. C. and a pressure of 2.2 bar at the outlet of the
exchanger.
[0072] The stream 4, constituting the liquid phase from the
separating tank V2, is composed of 2.2% methane, 18.3% ethylene and
79.5% propane, the flow rate of which is 2501 kmol/h, is cooled in
the exchanger E1 in order to give a stream 19 available at
-60.degree. C.
[0073] The stream 19 is then separated into two streams:
[0074] a stream 8, the flow rate of which is 1000 kmol/h, is
expanded to 8.1 bar by passing through a valve 20, to give a stream
21. The latter is vaporized and warmed in the exchanger E1 to give
a stream 9 at a temperature of 38.5.degree. C. and a pressure of
7.8 bar;
[0075] a stream 22, the flow rate of which is 1501 kmol/h, is
expanded to 2.2 bar in a valve 23 and then mixed with the stream 18
to give the stream 6. The latter, available at a temperature of
-64.93.degree. C. and a pressure of 2.2 bar, composed of 6.0%
methane, 27.2% ethylene and 66.8% propane, is vaporized and warmed
in the exchanger E1 in order to deliver a stream 7 available at
38.5.degree. C. and 1.9 bar.
[0076] The stream 7 is sent to the low-pressure stage of a
compressor K1, passing via a suction tank V3. A stream 11, coming
from the compressor K1 with a flow rate of 2970 kmol/h
corresponding to all of the stream 7 entering the low-pressure
stage of the compressor, is introduced into a water exchanger E11
at a pressure of 8.0 bar and a temperature of 113.75.degree. C. in
order to produce a cooled stream 25 at 42.0.degree. C. and 7.7
bar.
[0077] The stream 9 flows through a suction tank V4 and then mixes
with the stream 25, to deliver a stream 10 with a flow rate of 3970
kmol/h, at 41.01.degree. C. and 7.7 bar. The latter stream 10 is
introduced into a medium-pressure stage of the compressor K1.
[0078] A stream 26 coming from a high-pressure stage of the
compressor K1 with a flow rate of 3970 kmol/h, at 111.66.degree. C.
and 28.39 bar, is cooled in a water exchanger E10 in order to give
a stream 27 at 54.36.degree. C. Finally, this stream 27 is cooled
to 42.0.degree. C. in a water exchanger E12, to give the stream
13.
[0079] The performance characteristics of the two processes are now
given by the means of comparative tables.
1 Comparison of the powers of the compressors (in kW): (The powers
are based on 82% polytropic efficiencies) Conventional Process
according process to the invention (FIG. 1) (FIG. 2) Ethylene 2124
compressor Propane 7406 compressor Refrigerant 8708 mixture
compressor Total 9530 8708
[0080] The process according to the invention allows a power saving
of 9.4%.
2 Comparison of the refrigerating water exchangers Conventional
process Process of the invention Heat Exchange Heat Exchange Water
exchanged MTD area exchanged MTD area exchanger (kW) (.degree. C.)
(m.sup.2) (kW) (.degree. C.) (m.sup.2) E10 3239 22.1 293 5989 35.2
341 E11 16426 8.88 3700 4451 24.4 365 E12 8211 6.88 2388 Total
19665 3993 18651 3094
[0081] The area of the refrigerating water exchangers for the
process according to the invention 29% is less than that of the
conventional process. The water consumption is 5.4% less in the
case of the process of the invention.
3 Comparison of the cryogenic exchangers: Conventional process
Process of the invention Heat Exchange Heat Exchange exchanged MTD
area exchanged MTD area Exchanger (kW) (.degree. C.) (m.sup.2) (kW)
(.degree. C.) (m.sup.2) E1 2000 11.2 357 30100 7.27 8286 E2 5658
6.74 1679 2367 3.49 1356 E3 5514 15.7 702 E4 1397 11.4 245 E5 1258
53.2 47 E6 606 8.59 141 E7 570 12.4 595 E8 929 11.0 169 E9 7500
3.75 4000 Total 25432 7935 32467 9642
[0082] The process according to the invention uses a 21% higher
total exchange area than the known process. However, the cost of
these exchangers is lower.
4 Comparison of the number of equipment items: Conventional Process
of the process invention Cryogenic 9 2 exchangers Water exchangers
2 3 Tanks 8 4 Column 1 1 Compressors 2 1 Pumps 2 0 Total 24 11
[0083] The process of the invention comprises only 11 equipment
items instead of 24 in the case of the known process.
5 Comparison of the number of control systems: Conventional Process
of the process invention Flow rate control 3 1 Level control 7 2
Temperature 2 4 control Pressure control 1 1 Total 13 8
[0084] The new process possesses 8 control systems instead of 13 in
the case of the conventional process.
[0085] The invention is therefore beneficial in limiting the energy
consumption when producing purified gases. This objective is
achieved while allowing a high level of selectivity in separating
methane from the other constituents when operating the process.
[0086] Thus, the results obtained by the invention afford major
advantages, these consisting in a substantial simplification and a
substantial saving in both the construction and the technology of
the equipment and in the methods of operating them, as well as in
the quality of the products obtained by these methods.
* * * * *