AIR SEPARATION PROCESS USING CRYOGENIC DISTILLATION

Abstract

[ 4   Q air π   K  ( P P 0 )  0.35 ]  1 / 2 ( I ) In a process for the separation of air into at least one constituent by cryogenic distillation of air in a system of columns (1, 3) comprising at least one column (1, 3) for producing at least gaseous oxygen and/or nitrogen as product, if the operating pressure of the largest-diameter column is P>2 bar abs, then the diameter (in metres) of this column is less than (I), where : Qair is the sum of the flow rates in Sm3/h of the air feeding the column system and K is the capacity per unit area of the column and P0 is equal to 2 bar abs.

Description

The present invention relates to an air separation process using cryogenic distillation. In particular, it relates to air separation processes for the production of large quantities of oxygen with a content of greater than 90 mol % with a yield of greater than 90% in a unit comprising at least one column operating at low pressure and at least one column operating at high pressure, at least one column of which containing at least one section of structured packings of the cross-corrugated type.

Cross-corrugated packings are described in EP-A-0 367 817 and EP-A-0 491 591.

U.S. Pat. No. 5,653,126 describes the use of cross-corrugated structured packings having a density of at least 500 m²/m³ with a low HETP for the separation of air.

Typically, cross-corrugated packings have corrugations at 45° with the axis of the column in which they are installed. The packings may or may not be perforated and are generally formed by folded metal foil strips.

The increase in demand for gas separation units of large capacity (production greater than 2000 tonnes of gas produced per day) has led to the need to design distillation columns of increasing diameter, despite the frequent use of pressurized distillation processes (with columns operating at pressures above 2 bar abs).

Transport problems become significant when the diameter of the elements exceeds 3 m, or even 4.5 m, and these are sometimes insurmountable for columns greater than 6 m in diameter.

If it was desired to increase the ratio of oxygen production (in t/d of pure product) to cross section (in m²) of the low-pressure column, that is to say to reduce the diameter of the low-pressure column for constant oxygen production (or given air throughput), for a unit comprising a medium-pressure column thermally coupled to a low-pressure column or for a unit comprising three columns, including a medium-pressure column thermally coupled to a low-pressure column and an intermediate-pressure column fed from the medium-pressure column, the only solutions were:

• • to increase the withdrawal of nitrogen from the medium-pressure column (or from the intermediate-pressure column), but above a level of withdrawal representing between 15-20% of the air throughput, it is found that:
    • either the oxygen yield of the unit drops dramatically for a given oxygen purity
    • or the oxygen purity drops dramatically for a given oxygen withdrawal;
  • to increase the pressure of the unit (low pressure>2 bar abs), but this is highly penalizing from the energy standpoint if the pressure of the waste nitrogen is not utilized (that is to say by expansion in order to make liquid, or as product pressure).

In an air separation unit producing large quantities of oxygen and nitrogen, if it was desired to reduce the diameter of this column, the only solutions were:

• • to increase the withdrawal of lean liquid and of liquid nitrogen, but above a certain ratio it is found that the purity of the nitrogen and of the lean liquids dramatically drops and that the oxygen yield of the unit collapses;
  • to increase the flow of blown air, but above a certain ratio the performance of the unit is greatly degraded—reduction in oxygen yield (or in oxygen purity), reduction in medium-pressure gaseous nitrogen (or in purity of medium-pressure gaseous nitrogen);
  • to increase the liquid air flow, but this flow is set by the production of pumped products and the production of liquid products (liquid oxygen, liquid nitrogen, liquid argon), or a substantial loss of energy;
  • to increase the pressure of the unit (with a medium pressure>8 bar abs), but this is highly disadvantageous from the energy standpoint if the pressure of the waste nitrogen is not utilized (that is to say by expansion in order to make liquid, or as product pressure).

The object of the present invention is to alleviate the problems of the prior art by allowing the column diameters to be reduced for a given oxygen production.

One object of the invention is to provide a process for the separation of air into at least one constituent by cryogenic distillation of air in a system of columns comprising at least one column

• • a) for producing at least gaseous oxygen as product, such that the oxygen yield is greater than 90% (preferably 95%) and the oxygen purity is greater than 90 mol % oxygen (preferably 95 mol % oxygen or even 99 mol % oxygen) and/or
  • b) for producing at least nitrogen such that the nitrogen yield is greater than 85% (preferably greater than 90%) and the nitrogen purity is greater than 99 mol % nitrogen (preferably 99.99 mol % nitrogen or even 99.999 mol % nitrogen)
• characterized in that:
  • if the operating pressure of the largest-diameter column is P<2 bar abs, then the diameter (in metres) of this column is less than:

${\left(\frac{4Q_{\mathrm{air}}}{\pi K}\right)}^{1/2}$

• if the operating pressure of the largest-diameter column is P>2 bar abs, then the diameter (in metres) of this column is less than:

$\left[\frac{4Q_{\mathrm{air}}}{\pi K\left(\frac{P}{P_0}\right)0.35}\right]1/2$

• where:
  • Q_air is the sum of the flow rates in Sm³/h of the air feeding the column system;
  • K is the capacity per unit area of the column and equals at least 21000 Sm³/m² (preferably at least 23000 Sm³/m² or even at least 25000 Sm³/m²); and
  • P₀ is equal to 2 bar abs.

The yield is the percentage number of oxygen molecules in all the oxygen-rich products relative to the number of oxygen molecules in the feed air for the separation unit.

The capacity per unit area of the column is the ratio of the molar volume of gas sent into the column to the mean cross section of the column.

According to other optional features:

• • the largest-diameter column of the column system contains at least one section filled with a gas/liquid contactor allowing material exchange between the gaseous phase and the liquid phase such that its effectiveness is defined by a TUH (Transfer Unit Height) of less than 350 mm (preferably less than 300 mm);
  • the gas/liquid contactor is composed of cross-corrugated structured packings having a density of less than 500 m²/m³, preferably less than 400 m²/m³;
  • the column system comprises at least one double column formed by a medium-pressure column and a low-pressure column, the medium-pressure column being thermally coupled to the low-pressure column, and the low-pressure column constituting the largest-diameter column;
  • the ratio of the oxygen produced to the cross section of the low-pressure column is greater than or equal to 150 t/d/m²;
  • the ratio of the flow rate of air sent to the column system to the cross section of the low-pressure column is not less than 21000 Sm³/h/m², preferably not less than 23000 Sm³/h/m² and even more preferably not less than 25000 Sm³/h/m²;
  • the ratio of the gaseous air sent to the medium-pressure column to the cross section of the low-pressure column is not less than 18000 Sm³/h/m² (preferably not less than 20000 Sm³/h/m² and even more preferably not less than 22000 Sm³/h/m²); and
  • at least one section of the medium-pressure column contains cross-corrugated structured packings with a density not exceeding 500 m²/m³, or even 400 m²/m³.

It is another object of the invention to provide an air separation unit using cryogenic distillation, comprising a column system, the diameter of the largest-diameter column being between 3 and 6 m, the largest-diameter column containing at least one gas/liquid contactor section consisting of cross-corrugated structured packings having a density not exceeding 500 m²/m³, or even 400 m²/m³. Surprisingly, this is economically advantageous as even if the height of the columns is increased and the architecture is modified, the diameter reduction effect is predominant. Moreover, the drawback of the increased height can be resolved by placing the column sections at the desired height, side by side with fluid transfer pipes.

Preferably, the largest-diameter column contains only cross-corrugated structured packings having a density not exceeding 500 m²/m³, or even 400 m²/m³.

In certain cases, all the columns of the column system contain only cross-corrugated structured packings having a density not exceeding 500 m²/m³, or even 400 m²/m³.

A fluid will be called a “product” if it is output from the air separation unit with the content of one of its constituents being:

• • greater than 85 mol %, if the constituent is oxygen;
  • greater than 95 mol %, if the constituent is nitrogen.

The extraction efficiency of a constituent will be defined by the ratio of the molar quantity of the said constituent entering the separation unit via the feed fluids to the molar quantity of the same constituent leaving via the product(s), the content of this constituent being greater than or equal to those mentioned above.

Cross-corrugated structured packings with a density not exceeding 500 m²/m³, or even 400 m²/m³, may be installed in the medium-pressure column and/or the low-pressure column of a double column, in the medium-pressure column and/or the low-pressure column and/or the intermediate-pressure column of a triple (Etienne) column, an argon column, a mixing column or any other type of air gas separation column.

A packing has a density of less than 500 m²/m³ if its mean density (without deducting the area of any perforations) does not exceed 500 m²/m³.

The invention will be described in greater detail with reference to the figure.

FIG. 1 shows an air separation unit according to the invention.

In a unit according to the invention, a double column comprises a medium-measure column 1 operating at between 5 bar abs and 20 bar abs and a low-pressure column 3 operating at a pressure between 1.2 bar abs and 8 bar abs. The low-pressure column is larger in diameter than the medium-pressure column, but it is possible in some cases for the medium-pressure column to be larger in diameter than the low pressure column. The two columns are thermally coupled to each other by a reboiler/condensor 5, for example of the bath type.

The low-pressure column 3 contains only sections of structured packings 2 having a density not exceeding 500 m²/m³, for example having a density of 400 m²/m³.

The medium-pressure column 1 contains only sections of structured packings 2 having a density close or identical to the above values.

A stream of cooled and purified air 7 is sent to the medium-pressure column 1 and oxygen-enriched and nitrogen-enriched liquid streams 9, 11 are sent from the medium-pressure column to the low-pressure column after an expansion step.

Withdrawn from the bottom of the low-pressure column is a stream of gaseous oxygen 13 as product, with an oxygen yield of greater than 90% (preferably greater than 95%). The oxygen purity is greater than 90 mol % oxygen (preferably greater than 95 mol % oxygen or even 99 mol % oxygen).

At the top of the low-pressure column, gaseous nitrogen 15 is withdrawn with a nitrogen yield of greater than 85% (preferably greater than 90%). The purity of the nitrogen is greater than 99 mol % nitrogen (preferably greater than 99.99 mol % nitrogen or even 99.999 mol % nitrogen).

A stream of waste nitrogen 17 is withdrawn from an upper level of the low-pressure column.

The diameter (in metres) of the low-pressure column is less than:

$\left[\frac{4Q_{\mathrm{air}}}{\pi K\left(\frac{P}{P_0}\right)0.35}\right]1/2$

• where:
  • Q_air is the sum of the flow rates in Sm³/h of the air feeding the column system;
  • K is the capacity per unit area of the column and equals at least 21000 Sm³/m² (preferably at least 23000 Sm³/m² or even at least 25000 Sm³/m²); and
  • P₀ is equal to 2 bar abs.

To give a numerical example, it will be assumed that an installation has to treat an air throughput of 500 000 Sm³/h. According to the invention, if the low-pressure column is operated at a pressure below 2 bar abs, the cross section of the low-pressure column will therefore be less than:

• • (500000/21000)m²
  • (preferably less than (500000/23000) m² or even less than (500000/25000) m²)
• and the diameter less than:

$\left[\frac{4(500000/21000}{\pi }\right]1/2$

• i.e. 5.5 m (preferably 5.26 m, or even at most 5.05 m).

If the low-pressure column is operated at 3 bar abs, the cross section of the low-pressure column will therefore be less than:

$\left(\frac{500000}{21000}\right)m^2$

• • (preferably less than (500000/23000) m² or even less than (5000000/25000) m²)
• and the diameter less than:

$\left(\frac{4\left(\frac{500000}{21000}\right)}{\pi {\left(3/2\right)}^{0.35}}\right)1/2$

• i.e. 5.13m (preferably 4.9 m, or even at most 4.7 m).

Claims

1. Process for the separation of air into at least 5. one constituent by cryogenic distillation of air in a system of columns (1, 3) comprising at least one column (1, 3) ( 4  Q air π   K ) 1 / 2 [ 4   Q air π   K  ( P P 0 )  0.35 ]  1 / 2

a) for producing at least gaseous oxygen as product, such that the oxygen yield is greater than 90% (preferably 95%) and the oxygen purity is greater than 90 mol % oxygen (preferably 95 mol % oxygen or even 99 mol % oxygen) and/or

b) for producing at least nitrogen such that the nitrogen yield is greater than 85% (preferably greater than 90%) and the nitrogen purity is greater than 99 mol % nitrogen (preferably 99.99 mol % nitrogen or even 99.999 mol % nitrogen)

characterized in that: if the operating pressure of the largest-diameter column (3) is P<2 bar abs, then the diameter (in metres) of this column is less than:

if the operating pressure of the largest-diameter column is P>2 bar abs, then the diameter (in metres) of this column is less than:

where:

Qair is the sum of the flow rates in Sm3/h of the air feeding the column system;

K is the capacity per unit area of the column and equals at least 21000 Sm3/m2 (preferably at least 23000 Sm3/m2 or even at least 25000 Sm3/m2); and

P0 is equal to 2 bar abs.

2. Process according to claim 1, in which the largest-diameter column (3) of the column system contains at least one section (2) filled with a gas/liquid contactor allowing material exchange between the gaseous phase and the liquid phase such that its effectiveness is defined by a TUH (Transfer Unit Height) of less than 350 mm (preferably less than 300 mm).

3. Process according to claim 2, in which the gas/liquid contactor is composed of cross-corrugated structured packings having a density of less than 500 m2/m3, preferably less than 400 m2/m3.

4. Process according to claim 1, 2 or 3, in which the column system comprises at least one double column formed by a medium-pressure column (3) and a low-pressure column (1), the medium-pressure column being thermally coupled to the low-pressure column, and the low-pressure column constituting the largest-diameter column.

5. Process according to claim 4, producing oxygen in which the ratio of the oxygen produced to the cross section of the low-pressure column is greater than or equal to 150 t/d/m2.

6. Process according to claim 4 or 5, in which the ratio of the flow rate of air sent to the column system to the cross section of the low-pressure column is not less than 21000 Sm3/h/m2, preferably not less than 23000 Sm3/h/m2 and even more preferably not less than 25000 Sm3/h/m2.

7. Process according to claim 4, 5 or 6, in which the ratio of the gaseous air sent to the medium-pressure column (1) to the cross section of the low-pressure column is not less than 18000 Sm3/h/m2 (preferably not less than 20000 Sm3/h/m2 and even more preferably not less than 22000 Sm3/h/m2).

8. Process according to claim 7, in which at least one section (2) of the medium-pressure column (1) contains cross-corrugated structured packings with a density not exceeding 500 m2/m3, or even 400 m2/m3.

9. Air separation unit using cryogenic distillation, comprising a column system, the diameter of the largest-diameter column (3) being between 3 and 6 m, the largest-diameter column containing at least one gas/liquid contactor section (2) consisting of cross-corrugated structured packings having a density not exceeding 500 m2/m3, or even 400 m2/m3.