Patent Application
20110146343
The present invention relates to a process and an apparatus for the separation of air by cryogenic distillation.
Very large gas or coal gasification sites may be built in the near future. All gasification processes require large quantities of high pressure oxygen.
Air separation unit (ASU) plant sizes have been growing steadily over the last four decades and there is no sign for the trend to stop. With plant sizes getting larger and larger, liquid back-up issues become impractical or impossible for plant outages lasting for more than a few hours.
Current technologies would allow plant sizes up to 7000 metric tonnes of oxygen per day. Presently, largest reference plant sizes are between 4000 and 5000 metric tonnes per day.
Coal gasification in the near future for example may require very large oxygen consumption reaching as high as 50 000 T/D. Gas-to-liquid GTL plant is another example with high oxygen requirement in the range of 20 000-40 000 T/D. It becomes obvious there is a need for an improved and rational production concept for oxygen in such large facilities.
This invention provides a new approach for building large facilities requiring multiple large trains of oxygen plants. A new concept for cost effective production back-up is also integrated in this new scheme.
This invention covers three main aspects for the cryogenic process for large air separation facilities:
In order to reach a very high production throughput a different process scheme for air separation plant is needed. The traditional double column process operates at low feed air pressure about 6 bar requiring large adsorption vessels for front end clean up to remove moisture and CO2 prior to the cryogenic portion of the oxygen plant.
In most situations, the nitrogen flow at the top of the column dictates the column size, or the plant size. The bottleneck occurs not only at the top of the low pressure column but also at the top of the high pressure column. Therefore, in order to significantly increase the production output, the selected process must reduce the vapor flow at the top of all columns.
The top flow of the high pressure column can be reduced by generating the plant refrigeration by expanding some feed air into the low pressure column. The expanded air flow must be limited otherwise the distillation efficiency would be reduced, since the expanded air flow decreases the reboil and reflux of the low pressure column.
The top flow of the low pressure column can be minimized by extracting nitrogen from the top of the high pressure column such that less nitrogen will reach the low pressure column hence reducing the low pressure column's top vapor flow. Again, the extracted nitrogen flow must be limited because of the distillation efficiency consideration.
The double column scheme is not very well adapted when it comes to maximizing the expanded air flow or the high pressure nitrogen extraction. Indeed, for oxygen purities of about 95-97% mol, approximately 25-30% of the total feed air can be expanded to the low pressure column. With this much expanded air, it becomes difficult to efficiently extract nitrogen from the high pressure column. It is clear that the air expansion can reduce the top vapor flow of the high pressure column but does not reduce the top flow of the low pressure column since the nitrogen contained in the expanded air must exit at the top of the low pressure column. Without the expanded air, as high as 20-25% of the total air flow can be removed as nitrogen at the top of the high pressure column. Since the oxygen flow represents 20% of the feed air, this means a flow representing about 55-60% of the total air feed flow must exit at the top of the low pressure column. If more nitrogen is removed from the high pressure column, the distillation efficiency will suffer resulting in loss of oxygen recovery and higher air flow is needed to produce the given amount of oxygen. Therefore this technique of nitrogen removal can improve the top flow of the low pressure column but has no effect on the top flow of the high pressure column.
According to the present invention, there is provided a process for the cryogenic separation of air using a multiple column distillation system comprising at least a higher pressure column (“HP column”) and a lower pressure column (“LP column”), said process comprising: feeding cooled feed air to the high pressure column for separation into high pressure nitrogen-enriched overhead vapor and crude liquid oxygen; feeding at least one low pressure column feed stream comprising nitrogen and oxygen to the low pressure column for separation into nitrogen-rich overhead vapor and liquid oxygen; refluxing the low pressure column with a liquid stream from or derived from the high pressure column; feeding expanded air to an auxiliary separation column for separation into auxiliary column nitrogen-rich overhead vapor and oxygen-rich liquid and removing the nitrogen rich overhead vapour as a product stream; feeding bottom liquid from the auxiliary column to an intermediate location of the low pressure column; and refluxing the auxiliary column with a nitrogen rich liquid stream from or derived from the HP column.
According to optional features;
According to a further aspect of the invention, there is provided an apparatus for the cryogenic separation of air comprising: a high pressure column for separating cooled feed air into high pressure nitrogen-enriched overhead vapor and crude liquid oxygen; a low pressure column for separating at least one low pressure column feed stream comprising nitrogen and oxygen into low pressure nitrogen-rich overhead vapor and liquid oxygen; conduit means for feeding a liquid stream from or derived from the high pressure column as reflux to the low pressure column; an auxiliary separation column for separating air into auxiliary column nitrogen-rich overhead vapor and oxygen-rich liquid; conduit means for removing the nitrogen rich overhead vapour as a product; conduit means for expanding and feeding oxygen-rich liquid from the auxiliary column to an intermediate location in the low pressure column; and conduit means for feeding a nitrogen rich liquid stream from or derived from the HP column as reflux to the auxiliary column.
A modified triple column process as illustrated in
The apparatus comprises a high pressure column 100, an intermediate pressure column 101 and a low pressure column 102. An auxiliary column 103 is also used.
The air feed to this process is at about 11 bar which results in more compact and less bulky adsorber vessels. The adsorbers can be used for higher air flow since the air is more dense and high pressure is more favorable for the adsorption of moisture and CO2.
The top vapor flow of the high pressure column is reduced by expanding high pressure feed air into the auxiliary low pressure column which distils the air in to a top nitrogen stream and a bottom liquid rich in oxygen. The auxiliary low pressure column operates at a similar pressure to the low pressure column, it is fed by liquid nitrogen reflux at the top. This pressure may be lower than, higher than or equal to the pressure of the low pressure column. A liquid air stream can be optionally fed to this auxiliary column to improve its distillation performance.
Air 1 at 11 bar is divided into three streams following compression, cooling and purification.
One of the streams is stream 8 which cools in the heat exchanger 90 to form stream 6 which is sent in gaseous form to the high pressure column 100. It is separated in the high pressure column 100 into a nitrogen rich stream at the top and a rich liquid stream 10 rich in oxygen at the bottom. The nitrogen rich stream condenses in a first condenser 91 to yield a first liquid reflux stream. Some nitrogen 42 can be extracted at the top of the high pressure column as a product stream and sent to the heat exchanger 90 to be warmed. A portion 11 of the first reflux stream is sent to the low pressure column 102 as reflux stream 14 and to the auxiliary column 103 as reflux 15. Portion 89 of the reflux stream may serve as a nitrogen liquid product. All or a portion of the bottom rich liquid 10 is sent to the bottom of the intermediate column 101 for further distillation. The intermediate column operates at an intermediate pressure between the high pressure column's pressure and the low pressure column's pressure. The first condenser 91 transfers heat between the top of the high pressure column and the bottom of the intermediate column. The intermediate column separates the rich liquid into a second nitrogen rich gas at the top and a very rich liquid 12 at the bottom. Part of the second nitrogen rich gas condenses in a second condenser 92 to yield a second reflux stream and the rest 40 is removed as a gaseous stream and warmed in heat exchanger 90. The very rich liquid 12 is sent to the low pressure column 102 as feed. A portion of the second reflux stream 16 formed in the condenser 92 may be sent to the low pressure column as reflux. The second condenser 92 transfers heat between the top of the intermediate column 101 and the bottom of the low pressure column 102.
Instead of only expanding the feed air to the low pressure column, a portion 31 of feed air is expanded into an auxiliary column 103 using a turbine 80. The auxiliary column works at a pressure between 1.1 bar absolute and 1.8 bar absolute, which is about the same as the pressure of the low pressure column 102. A portion of liquid reflux 15 produced in either high pressure column or intermediate column is fed to the top of the auxiliary column as reflux. This auxiliary column 103 separates the expanded air 32 into nitrogen rich gas 21 at the top and a second rich liquid 60 rich in oxygen at the bottom. The second rich liquid is then expanded and transferred to the low pressure column 102 as feed. The auxiliary column 103 can be located above the low pressure column 102 such that the second rich liquid 60 can flow into the low pressure column by gravity feed, or a transfer pump can be used. The low pressure column 102 separates its feeds into the oxygen liquid 70 at the bottom and low pressure nitrogen gas 20 at the top. The oxygen liquid is pumped to high pressure and vaporized in the main exchanger 90 to yield the gaseous high pressure oxygen product 72. A portion 2 of feed air is further compressed in a warm booster 84, cooled in the heat exchanger 90, to form stream 3, compressed in a cold compressor 82 to form high pressure stream 4 and is used to condense against vaporizing liquid oxygen product in the main exchanger 90. The fluid 5 coming from the exchanger 90 is liquefied and sent to the high pressure column 100.
Part of the feed air 30 at 11 bars may or may not be expanded as stream 33 in turbine 81 to form stream 34 which is sent to the low pressure column 102.
By feeding a very rich liquid produced in the intermediate column to the low pressure column the distillation performance of the low pressure column is greatly improved such that significant expanded air flow to the second low pressure column, combined with significant nitrogen extracted in the high pressure column and/or the intermediate column, can be performed with good oxygen recovery rate.
In the embodiment described in
The vapor flow rate in the auxiliary column 103 is determined such that the diameters of the upper sections of the low pressure column 102 are not larger than that for any other section of the multiple distillation column system. Here the low pressure column 102 has the same diameter throughout as the high pressure column 100.
The enhancement of the distillation performance provided by the triple column arrangement of columns 100, 101 and 102 allows us to achieve a vapor flow rate at the top of the auxiliary separation column 103 greater than about 50 percent of the vapor flow rate at the top of the upper low pressure column sections under normal operation.
The traditional approach for backing up the production facilities consisting of several trains operating in a parallel fashion is to install a full size spare train. This spare train or unit can be put in service in a short time to take over the slack of production caused by the outage of one of the components of the other trains. Since the probability of having two outages occurring at the same time is low, it is of common practice to have only one spare train to assure the reliability of the multiple trains. In some situations, if the start up time of the spare unit must be very short or instantaneous then all equipment including the spare unit must run permanently at a reduced rate; when one unit is shut down then the production rate of the remaining units can be increased very rapidly to maintain the overall production.
Another approach, also called boosting, to address the backup problem is to oversize each train such that its production rate can be increased or boosted in the event of outage of one train to maintain the overall production.
The above approaches are illustrated in
It is clear that the above provisions for backup is costly in terms of capital expenditure since the spare equipment or the extra production abilities are not fully utilized in the majority of the time. Therefore there is a need to improve the cost and effectiveness of the backup equipment, especially in case of large facilities consisting of multiple trains.
The process of
The air in column 100 is separated into a crude oxygen stream 10 and nitrogen rich streams. The crude oxygen stream is sent to the bottom of the low pressure column. The increase of total air flow can be performed via only increasing of flow of stream 31 to expander 80 and column 103. In this case, where under normal flow the column 103 operates at a lower or identical pressure to that of column 102, the column 103 will be operated at a higher pressure to that of column 102. The air flow feeding the other columns 100, 101 and 102 can be kept constant to avoid the increase of back pressure described above. The back pressure will increase in column 103 and at the outlet of expander 80. By confining the increase of back pressure in the dedicated circuit of the expander 80 and the second low pressure column 103, and only on a fraction of the total stream, more flow can be pushed through the system for production increase. And the penalty on the whole system, caused by the increase of flow and the increase of back pressure, can be avoided. There will be higher pressure drop and higher back pressure on the circuit of expander 80 and column 103, but the penalty on power consumption will be minimal and can be easily justified during the backup mode. Except for the dedicated circuit, at higher flow of boosting mode, the main circuits of the process will operate at essentially the same pressure as in normal condition. Therefore the boosting can be achieved without having to oversize the heat exchanger train and the associated piping equipment.
