Method and appliance for separating a mixture containing carbon dioxide by cryogenic distillation

Abstract

In a method for separating at least one lighter impurity of a gaseous mixture containing at least 30% mol of carbon dioxide, a liquid (101) enriched with carbon dioxide is drawn off into a vat of a distillation column (25), at least part (27) of the liquid enriched with carbon dioxide is vaporized and then heated to a first temperature higher than the boiling temperature thereof in the exchanger and leaves the exchanger at the hot end thereof, and at least part of the vaporized and heated liquid is sent from the hot end of the exchanger at the first temperature, without being cooled in the exchanger and without having been compressed, to the lower part of the distillation column, where it participates in the distillation while enriching itself.

Claims

1. A method for separating at least one lighter impurity of a gaseous mixture containing at least 30% mol of carbon dioxide comprising: i) cooling the gaseous mixture in a heat exchanger, the heat exchanger comprising a hot end, the gaseous mixture entering the heat exchanger at the hot end, and the cooled gaseous mixture or a fluid derived from the gaseous mixture, this fluid containing at least 60% carbon dioxide, being separated by a distillation column, the distillation column having a head and a bottom part, ii) removing a liquid enriched in carbon dioxide from the distillation column, iii) drawing off a gas depleted in carbon dioxide and enriched in at least one lighter impurity at the head of the column and reheating this drawn off gas in the heat exchanger, sending at least a part of the liquid enriched in carbon dioxide to the heat exchanger wherein at least one part of the liquid sent to the heat exchanger is vaporized and then super-heated to a first temperature in the heat exchanger and leaves from the heat exchanger at the hot end thereof, and at least a part of the vaporized and heated liquid is sent from the hot end of the heat exchanger at the first temperature, without being cooled in the heat exchanger and without having been compressed, to the bottom part of the distillation column, thereby becoming enriched in at least one lighter impurity, wherein the at least part of the liquid enriched in carbon dioxide that has been vaporized and then super-heated is divided into two parts, one part being returned to the column at the first temperature and the other part constituting at least a part of a final product.

2. The method of claim 1, wherein the first temperature is at least 5° C. higher than the boiling point.

3. The method of claim 1, wherein first temperature is higher than 0° C.

4. The method of claim 3, wherein the first temperature is higher than 10° C.

5. The method of claim 1, wherein the gaseous mixture goes into the heat exchanger at the hot end thereof at a temperature between 2 and 10° C. higher than the first temperature.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) For a further understanding of the nature and objects for the present invention, reference should be made to the following detailed description, taken in conjunction with the accompanying drawings, in which like elements are given the same or analogous reference numbers and wherein:

(2) FIG. 1 illustrates one embodiment of the present invention; and

(3) FIG. 2 illustrates another embodiment of the present invention.

DESCRIPTION OF PREFERRED EMBODIMENTS

(4) According to the invention, in FIG. 1, a gaseous mixture 1 containing at least 30%, even at least 40% of carbon dioxide and at least one light impurity, that can be oxygen, carbon monoxide, nitrogen, argon, hydrogen, methane or at least two of these components, is separated to form a fluid richer in carbon dioxide. The gaseous mixture originates from a source 100 that can be an oxycombustion unit followed by scrubbing units for removing the water and other contaminants, such as dust, SO.sub.x, NO.sub.x. The gaseous mixture is compressed as required, for example to a pressure above 6 bar abs. The pressurized gaseous mixture 1 is cooled in a heat exchanger 43 with brazed aluminum plates or with tubes. The cooled gaseous mixture is, if necessary, treated in a treatment means, for example a separation means 113. This separation means 113 can constitute a phase separator or several phase separators in series to increase the carbon dioxide content of the gaseous mixture upstream of the column 25, for example to reach at least 80% of carbon dioxide for the liquid from a phase separator. The separation means 113 can alternatively or additionally comprise adsorbant beds and/or a distillation column, for example a column to eliminate NOx gases.

(5) The liquid 11 enriched in carbon dioxide is sent to the head of the separation column at low temperature 10. The head gas is drawn off at the head of the column and is enriched in light components relative to the liquid 11. A part 106 of the gas is discharged to the atmosphere and the rest 6 is reheated in the exchanger 43.

(6) The tank liquid 101 contains more than 90% of carbon dioxide and is separated into two parts. One part 31 is expanded in a valve 39 and is vaporized in the heat exchanger to form a gaseous product rich in carbon dioxide. The rest 27 is sent to an intermediate level of the heat exchanger 43, is vaporized therein and is heated up to the hot end of the exchanger to a first temperature. The vaporized throughput leaves the exchanger at the hot end at the first temperature and is then divided into two, one part 23 serving as product and the rest 31 being returned to the column 25. The gas 31 is neither compressed nor expanded between the hot end and the column 25. The gas 31 at the first temperature is returned to the bottom part of the column 25, without having been reheated or cooled, in or outside of the exchanger 43, and rises in the column 25 by being enriched in light impurities.

(7) All the frigories for the separation, apart from those generated by Joule Thomson expansion, are produced by vaporization of the throughputs 27, 31. Thus, the input for the throughput 27 serves to vaporize the liquid to produce frigories for the process and to produce the reboiling gas.

(8) If a part or all of the cold of the cold box is generated by the vaporization of the liquid obtained from the column at a pressure level corresponding to that of the column, it will therefore be possible to exploit the same intermediate input.

(9) The drawing off of the gas 31, 49 at the hot end of the exchanger makes it possible to simplify the main exchanger. No intermediate output is required. The cost of the exchanger, and of the connections around the exchanger are therefore reduced in this way. The gas going into the column 25 will no longer be at the boiling point or at the dew point but very greatly superheated.

(10) The table below gives compositions for FIG. 1.

(11) TABLE-US-00001 Feed Throughput Throughput Throughput throughput 1 11 101 31 Compositions (% mol) CO.sub.2 79.4  99   >99.99   >99.99 O.sub.2 7.6 0.4   1 ppmv   1 ppmv N.sub.2 8.5 0.2 <1 ppmv <1 ppmv Ar 4.5 0.4 <1 ppmv <1 ppmv Pressure (bara) 21   11   11    11 Temperature 35   −47.3  −37.6  +32 (° C.) Throughput 212 066     151 123     156 721    9 925  (kg/h)

(12) Since the steam 31 is not at equilibrium, a part of the liquid/gas contact in the bottom of the column will not be the subject of distillation but of heat transfer with regard to this case. Since the purity of the gas 6 is inconsequential, the deterioration of the distillation which results therefrom is not damaging.

(13) Thus, this column 25 is like a stripping column. However, this effect is highly attenuated because the quantity of vapor needed is lower when the gas is hotter (to achieve the same liquid CO.sub.2 purity). There is no impact on the overall energy consumption. Thus, the price of the apparatus is reduced without increasing the operating costs.

(14) For this scheme, the absence of any carbon dioxide compressor will be noted.

(15) In FIG. 2, a wet gas 1 containing carbon dioxide and oxygen or carbon monoxide is compressed in a compressor 3. This compressor 3 comprises four stages 3A, 3B, 3C, 3D, each being followed by a cooling means 5A, 5B, 5C, 5D. After cooling in the cooling means 5D, the gas 1 is cooled by the cooler 5E to form the gas 7 and sent into a scrubbing unit 9 to remove the moisture. The dry gas formed 11 is cooled in a first exchanger 43 where it is cooled and is partially condensed. The partially condensed gas is sent to a phase separator 13. The liquid from the phase separator 13 is sent to a valve 21 to form the liquid 23 and gas generated by the expansion which feed the distillation column 25 at the head.

(16) A gas enriched in oxygen and/or nitrogen 6 is drawn off from the head of the column and sent upstream of the cooler 5D. Alternatively, it can be returned to the oxycombustion unit from which the gas 1 originates.

(17) A part 27 of the tank liquid of the column 25, rich in carbon dioxide, is sent to the first exchanger 43. This part of the tank liquid 27 is vaporized and is reheated by passing entirely through the first exchanger 43 and is divided into two. One part 61 is sent downstream of the compressor 47 and the rest 31 is sent through a control valve 62 into the tank of the column 25.

(18) It is also possible to treat the tank liquid 27 in a second distillation column to produce a second tank liquid which is then vaporized in the exchanger 43.

(19) The rest of the tank liquid 29 is not heated in the exchanger but is sub-cooled in the sub-cooler 63 then mixed with a cycle fluid 51. The sub-cooling can also be done in the exchanger 43. The mixture formed 31 is divided into three parts. The part 37 is expanded by the valve 41 at low pressure and sent to a phase separator. The gas from the phase separator is reheated in the first exchanger and the liquid from the phase separator is vaporized in the first exchanger 43 and then the gas and the vaporized liquid are compressed in a compressor 47. The part 35 is expanded by the valve 39 at a medium pressure, vaporized in the first exchanger 43 and then compressed by a compressor 45. The mixture 49 thus formed by mixing the gas 61 and the compressed gases in the compressors 45, 47 is compressed in a compressor 51, condensed then divided into two. One part 56 is pressurized by a pump 53 to form a liquid product. The rest 55 is cooled in the first exchanger 43, is expanded in the valve 57 and mixed with the throughput 29 to be returned to the first exchanger 43, in refrigeration cycle.

(20) The gas 15 from the phase separator 13 is reheated in the first exchanger 43 to form a throughput 17 which is reheated by the reheaters 5F, 5G and expanded by two turbines 19F, 19G in series to form the expanded throughput 19.

(21) It will be understood that many additional changes in the details, materials, steps and arrangement of parts, which have been herein described in order to explain the nature of the invention, may be made by those skilled in the art within the principle and scope of the invention as expressed in the appended claims. Thus, the present invention is not intended to be limited to the specific embodiments in the examples given above.