METHOD AND UNIT FOR PROCESSING A GAS MIXTURE CONTAINING NITROGEN AND METHANE

Abstract

A method for processing a gas mixture containing nitrogen and methane, the gas mixture being at least partly liquefied using a mixed refrigerant circuit and is expanded in a storage tank, wherein: formed in the storage tank are a liquid phase, which is depleted in nitrogen and enriched with methane relative to the gas mixture, and a vapour phase, which is enriched with nitrogen and depleted in methane relative to the gas mixture; at least some of the vapour phase is compressed, at least partly liquefied, and subjected to low-temperature rectification; and formed in the low-temperature rectification are a top gas rich in nitrogen and lean in methane, and a bottom liquid lean in nitrogen and rich in methane. The invention provides that the partial liquefaction of the vapour phase is caused by cooling by means of heat exchange using the mixed refrigerant circuit.

Claims

1-10. (canceled)

11. A method for processing a gas mixture containing nitrogen and methane, wherein the gas mixture is at least partly liquefied using a mixed refrigerant circuit and expanded in a storage tank, wherein a liquid phase, which is depleted in nitrogen and enriched with methane relative to the gas mixture, and a vapor phase, which is enriched with nitrogen and depleted in methane relative to the gas mixture, are formed in the storage tank, wherein at least some of the vapor phase is compressed, at least partly liquefied, and subjected to low-temperature rectification, wherein a top fraction rich in nitrogen and lean in methane and a bottom liquid lean in nitrogen and rich in methane are formed in the low-temperature rectification, and wherein the liquefaction of the gas mixture containing nitrogen and methane and the partial liquefaction of the vapor phase take place using a single, mixed refrigerant circuit, wherein the liquefaction of the gas mixture containing nitrogen and methane and the partial liquefaction of the vapor phase take place in separate heat exchangers, a partial stream of the sump liquid drawn off from the low-temperature rectification is at least partly vaporized against a top gas drawn off from the low-temperature rectification, and the at least partly condensed top gas is supplied to the low-temperature rectification as a return stream, and the top fraction withdrawn from the low-temperature rectification has a nitrogen content of at least 99 mol %.

12. The method according to claim 11, wherein the top fraction drawn off from the low-temperature rectification has further inert components—in particular, hydrogen and/or helium—in addition to nitrogen, wherein the concentration of all inert components, including nitrogen, is at least 99 mol %.

13. The method according to claim 11, wherein a partial stream of the sump liquid from the low-temperature rectification is cooled against the top fraction to be heated and is returned to the storage tank.

14. The method according to claim 11, wherein the at least partial liquefaction of the vapor phase from the storage tank is assisted by heating the top fraction from the low-temperature rectification, and wherein the vapor and liquid fractions formed thereby are separated from one another and fed to the low-temperature rectification at different feed positions.

15. The method according to claim 11, wherein sump liquid from the low-temperature rectification is cooled against the top fraction from the low-temperature rectification in a subcooler, the cooled sump liquid expanded in a head condenser in which it acts as a coolant, completely evaporated thereby, and finally used as further coolant for the subcooler, wherein the evaporated sump liquid, after use as further coolant for the subcooler, is returned together with the vapor phase from the storage tank before compression.

16. The method according to claim 11, wherein, in the mixed refrigerant circuit, a mixed refrigerant is provided in a receiving vessel and fed to an intercooler via a first compression stage or compressor unit of a refrigerant compressor, wherein the compressed mixed refrigerant is cooled in the intercooler and fed to a first refrigerant separator, wherein a first refrigerant gas phase and a first refrigerant liquid phase are formed in the first refrigerant separator, wherein the first refrigerant gas phase is supplied to a second compression stage or compressor unit of the refrigerant compressor compressed, and, after cooling in an aftercooler, fed to a second refrigerant separator, wherein a second refrigerant gas phase and a second refrigerant liquid phase are formed in the second refrigerant separator, wherein the second refrigerant liquid phase is returned to the first refrigerant separator and wherein the first refrigerant liquid phase together with the second refrigerant gas phase is subcooled by heat exchange, expanded, and used as a refrigerant for heat exchange with at least one part of the gas mixture and at least one part of the vapor phase, wherein a mixture of the first refrigerant liquid phase and the second refrigerant gas phase is returned to the receiving vessel after the heat exchange.

17. The method according to claim 16, wherein the compositions and/or volume streams of the first and/or second refrigerant gas phases and/or refrigerant liquid phases can be controlled.

18. The method according to claim 11, wherein the gas mixture containing nitrogen and methane is natural gas or a gas mixture formed using natural gas.

19. The method according to claim 11, wherein the at least partial liquefaction of the gas mixture is carried out at a pressure level of 25 to 90 bar, the storage tank is operated at a pressure level of 1 to 5 bar, and/or in which the low-temperature rectification is carried out at a pressure level of 15 to 30 bar.

20. The method according to claim 11, wherein the mixed refrigerant consists of a proportion of more than 95% nitrogen, methane, ethane and/or ethylene, propane, butane and/or pentane, and isomers thereof.

Description

[0028] The method according to the invention for processing a gas mixture containing nitrogen and methane and further embodiments thereof are explained in more detail below with reference to the FIGURE.

[0029] The gas mixture 1, e.g., natural gas, which is to be processed and which contains nitrogen and methane, is cooled against the refrigerant of a mixed refrigerant circuit by heat exchange in a heat exchanger E3 and at least partly liquefied. This mixture 2 is then expanded in a storage tank L via a valve V3.

[0030] The refrigerant against which the gas mixture 1 is cooled by heat exchange originates from a mixed refrigerant circuit in which a mixed refrigerant 26 is provided in a receiving vessel D1. This mixed refrigerant has the composition explained above. The mixed refrigerant is compressed 20 to an intermediate pressure via a first compressor stage or compressor unit C1.I of a refrigerant compressor and then cooled in an intercooler E1 and partly condensed. In a refrigerant separator D2, a first refrigerant gas phase 21 and a first refrigerant liquid phase 23 are separated from one another, and the first refrigerant gas phase 21 is compressed 22 to the circuit pressure via a second compressor stage or compressor unit C1.II of the refrigerant compressor and cooled in an aftercooler E2 and partly condensed. In a refrigerant separator D3, a second refrigerant gas phase 29 and a second refrigerant liquid phase 28 are separated from one another. The second refrigerant liquid phase 28 is expanded in the partly condensed refrigerant feed 20 via the expansion valve V1 upstream of the refrigerant separator D2. The first refrigerant liquid phase 23 is increased in pressure in a pump P1 to the circuit pressure, and a partial stream thereof, together with a first partial stream 30 of the second refrigerant gas phase 29, is used as refrigerant for the heat exchange with the gas mixture 1, containing nitrogen and methane, in the heat exchanger E3. For this purpose, it is first subcooled in the heat exchanger E3, expanded in the expansion valve V2, and guided through the heat exchanger E3 via the line 25 back into the receiving vessel D1.

[0031] After expansion V3 of the at least partly liquefied mixture 2 and by means of the introduction of heat from the outside, an almost binary vapor phase 3, consisting of methane and enriched inert components, is formed in the storage tank L, which binary vapor phase is compressed by means of a compressor C2—preferably, to a pressure between 15 and 30 bar—and cooled in the coolers E4 and E5. The cooled vapor phase 4 is subsequently partly liquefied in the downstream sump boiler E6 of the separation column T1, and the resulting gas fraction 6 is fed to the heat exchanger E5 for further condensation and subcooling after separation in the separator D4. According to the invention, the provision of cold in the heat exchanger E5 likewise takes place via the previously described mixed refrigerant circuits, wherein a partial stream 27 of the first refrigerant liquid phase 23 pumped up to the circuit pressure, together with a second partial stream 31 of the second refrigerant gas phase 29, is used as refrigerant for the heat exchange with the method streams to be cooled. For this purpose, the aforementioned, combined partial streams 27 and 31 are first subcooled in the heat exchanger E5, expanded in the expansion valve V11, and guided through the heat exchanger E5 via the line 32 back into the receiving vessel D1.

[0032] The partly liquefied stream 4 is separated in the separator D4 into a vapor phase 6 and a liquid phase 5, wherein the liquid phase is fed from the separator directly into the separation column T1, while the vapor phase is further liquefied in the heat exchanger E5 before it is likewise fed into the separation column T1 via the expansion valve V4.

[0033] Sump liquid 8, which mainly contains methane, is removed from the separation column T1 and evaporated via the sump boiler E6 to yield a first part 8′, and returned to the sump of the separation column T1, cooled to yield a second part 10 via the heat exchanger E5 and returned to the storage tank L via the expansion valve V6, and cooled to yield a third part 9 via a subcooler E8 and used as coolant after expansion in the valve V 7 in the head condenser E7 of the separation column T1. The third part of the sump liquid is evaporated thereby in the head condenser E7, supplied via line 12 to the subcooler E8 in which it acts as a coolant, and subsequently returned via the expansion valve V9 before the compression C2 of the vapor phase 3. A gas 11, which is rich in nitrogen, possibly contains further inert components, and is low in methane, is removed from the separation column T1, cooled via the head condenser E7, and at least partly condensed and returned as return flow into a head section of the nitrogen separation column T1. The nitrogen-rich top gas 7 from the separation column T1 is discharged, via the subcooler E8 and the heat exchanger E5—in both of which it acts as coolant—as a nitrogen product stream having a content of nitrogen and, possibly, further inert components of at least 99 mol %, out of the process via the expansion valve V10.

[0034] The use of the mixed refrigerant circuit according to the invention for both the at least partial liquefaction of the gas mixture containing nitrogen and methane in the heat exchanger E3, and the distillative separation of the nitrogen and, possibly, further inert components from the vapor phase formed in the storage tank, and the at least partial liquefaction of the vapor phase in the heat exchanger E5 taking place for this purpose, has the advantage that the temperature in the heat exchangers E3 and E5 with the mixed refrigerant circuit can be precisely adjusted, and an economical process control is thus facilitated. By means of suitable method conditions, different temperatures can be realized in the heat exchangers E3 and E5 which are supplied via the mixed refrigerant circuit, so that the two method steps can be operated at the ideal temperature in each case—in particular, by adjusting an ideal mixing ratio of the first refrigerant liquid phase and the second refrigerant gas phase respectively, as well as different amounts of refrigerant, even though they are supplied via the same cooling circuit.

[0035] The method according to the invention also facilitates the production of a methane-rich liquid stream 10, which is supplied to the storage tank L via valve V6 as described.

[0036] By using an almost pure sump stream 9, the methane content of which is typically more than 95 mol %, the pressure-expanded sump stream is evaporated in the heat exchanger E7 at an almost constant temperature in order to produce a reflux for the separating column T1. As a result, the head condenser can be designed as a heat exchanger seated in a liquid bath. This leads to a very robust design of the heat exchanger and, additionally, to stable operating conditions. An enrichment of heavier hydrocarbons in the stream to be evaporated in the heat exchanger E7 can, additionally, be easily prevented by extracting a small amount of liquid stream—preferably, less than 5% of the amount of stream 9—from the upper part of the separating column T1.