Process for distilling alkaline caprolactam product at reduced pressure

Abstract

The invention relates to a process for distilling alkaline caprolactam product at reduced pressure, said alkaline caprolactam product comprising (i) caprolactam, (ii) organic impurities, and (iii) one or more bases selected from the group consisting of alkali hydroxide and alkali amino caproate, characterized in that the alkalinity of the alkaline caprolactam product is less than 5 meq. per kg of caprolactam.

Description

The invention relates to a process for purifying caprolactam, which process involves distilling alkaline caprolactam product at reduced pressure.

The production of caprolactam generally involves the preparation of caprolactam product, e.g. by Beckmann rearrangement, followed by purification of the caprolactam product to obtain polymerizable grade caprolactam product. The purification can include distillation of the caprolactam product at reduced pressure in the presence of a base, e.g. alkali hydroxide or an alkali amino caproate. Large ranges are mentioned for the amount of added base. DD-A-202870 describes a process in which caprolactam product is purified by distillation under reduced pressure after addition of 0.05 to 1.0% of the alkali salt of caproic acid to the caprolactam product to be purified. U.S. Pat. No. 3,839,324 describes a process in which caprolactam is subjected to an alkaline distillation in vacuo, wherein sodium hydroxide is present as 0.05-0.5 percent by weight. U.S. Pat. No. 5,496,941 describes a process wherein caprolactam is distilled in the presence of a base, the amount of added base as a rule being chosen from 0.05 to 0.9 mol. % based on caprolactam. U.S. Pat. No. 4,457,807 describes a process in which untreated caprolactam containing 0.2 mg of solid NaOH per gram of caprolactam (5 mmol NaOH per kg of caprolactam) is supplied to a rectification column wherein rectification is effected under reduced pressure.

It is now found that the quality of the purified caprolactam, e.g. as expressed by the PAN number, is influenced by the alkalinity of the caprolactam product to be distilled. In particular, the PAN number is found to decrease when the alkalinity of the alkaline caprolactam product is decreased to below 5 meq. per kg of caprolactam. The occurrence of undesired fluctuation in quality, e.g. resulting from the oxidation of caprolactam during distillation, is found to decrease when the alkalinity is increased to above 0 meq. per kg of caprolactam.

Accordingly the invention provides a process for purifying caprolactam, which process involves distilling alkaline caprolactam product at reduced pressure, said alkaline caprolactam product comprising (i) caprolactam, (ii) impurities, and (iii) one or more bases selected from the group consisting of alkali hydroxide and alkali amino caproate, characterized in that the alkalinity of the alkaline caprolactam product is less than 5 meq. (5 milli equivalent) per kg of caprolactam.

As used herein alkalinity refers to the alkalinity at a temperature of 25° C. as determined by titration (after diluting the alkaline caprolactam product with water of pH=5.7 to obtain a solution containing 15 wt. % caprolactam) with a 0.01 N HCl solution to a pH of 5.7, whereby $\mathrm{alkalinity}=\frac{v*t}{a*0.15}*1000$
Where:

• • v=ml of HCl solution added
  • t=molarity of HCl solution (=0.01)
  • a=weight of sample (g)

The process according to the invention results in purified caprolactam having a high quality, in particular a low PAN number (as determined in accordance with ISO DIS 8660-Plastics-Determination of permanganate index of caprolactame-Spectometric method, revision of first edition (ISO 8660; 1988)). Moreover a low value for the extinction (as determined in accordance with ISO 7059—caprolactam for industrial use—Determination of absorbance at a wavelength of 290 nm) is obtained.

Preferably, the alkalinity of the alkaline caprolactam product is lower than 4.5 meq. per kg of alkaline caprolactam product, more preferably lower than 4.0 meq. per kg, in particular lower than 3.0 meq. per kg, more in particular lower than 2.0 meq. per kg. This further decreases the PAN number.

Preferably, the alkalinity of the alkaline caprolactam product is higher than 0.05 meq. per kg of alkaline caprolactam product, more preferably higher than 0.10 meq. per kg, in particular higher than 0.15 meq. per kg. Increasing the alkalinity to above these values improves the stability, i.e. the sensitivity to occurrence of undesired fluctuations in quality.

As used herein the values mentioned for the alkalinity and concentrations in the alkaline caprolactam product refer to the values of the alkaline caprolactam product to be distilled. viz. when the alkaline caprolactam product is fed to a distillation zone, i.e. the zone in which the distillation is effected, the mentioned values for alkalinity and other concentrations in the alkaline caprolactam product refer to the values in the alkaline caprolactam product entering the distillation zone.

The alkaline caprolactam product comprises caprolactam. Typically, the alkaline caprolactam product comprises 95 to 99.9 wt. % of caprolactam, in particular at least 97 wt. % of caprolactam, more in particular at least 98 wt. % of caprolactam (relative to the weight of alkaline caprolactam product).

The impurities may be any organic impurities, e.g. low-boiling organic impurities (having a lower boiling point than caprolactam) and/or high-boiling organic impurities (having a higher boiling point than caprolactam).

The alkaline caprolactam product may include water. Preferably, the alkaline caprolactam product comprises less than 5 wt. %, more preferably less than 3 wt. %, in particular less than 2 wt. %, more in particular less than 1 wt. % (relative to the weight of alkaline caprolactam product). A lower amount of water has the advantage that a reduced pressure is easier to create and maintain during distilling.

The alkaline caprolactam product comprises one or more bases selected from the group consisting of alkali hydroxide and alkali amino caproate. Preferably the one or more bases are selected from the group consisting of sodium hydroxide, sodium amino caproate, potassium hydroxide, and potassium amino caproate, more preferably selected from the group consisting of sodium hydroxide and sodium amino caproate. Preferably, at least 75 mol. %, more preferably at least 85 mol. %, in particular at least 95 mol. %, more in particular substantially all of said one or more bases is alkali amino caproate. Increasing the relative amounts of alkali amino caproate has the advantage that the occurrence of polymerization during the distillation is lessened. The formation of oligomers and polymers is disadvantageous since it may result fouling of the distillation equipment. Moreover caprolactam is lost. The above percentages are given relative to the total molar quantity of said one or more bases.

The process according to the invention is preferably a process for the purification of caprolactam product, said caprolactam product comprising (i) caprolactam and (ii) impurities, wherein said process comprises adding one or more of the bases to said caprolactam product to yield the alkaline caprolactam product. Preferably, the alkali hydroxide is added as an aqueous solution of alkali hydroxide.

Typically, the caprolactam product comprises 15 to 99.9 wt. % of caprolactam, in particular at least 50 wt. % of caprolactam, more in particular at least 75 wt. % of caprolactam. Typically, the caprolactam product is aqueous caprolactam product comprising water. Typically the sum quantity of water and caprolactam and water in the caprolactam product is preferably at least 95 wt. %, in particular at least 97 wt. %, more in particular at least 98 wt. %. These percentages are given relative to the weight of the caprolactam product. In one embodiment of the invention, the caprolactam product has an acidity of between 0 and 5 meq. per kg caprolactam, is neutral, or has an alkalinity of between 0 and 5 meq. per kg caprolactam. In this embodiment the alkaline caprolactam product can be prepared by adding very small amounts of said one ore more bases. This results in purified caprolactam having a good quality, as expressed by the PAN number, and a good stability. As used herein acidity refers to the acidity at a temperature of 25° C. as determined by titration (after diluting the alkaline caprolactam product with water of pH=5.7 to obtain a solution containing 15 wt. % caprolactam) with a 0.01 N NaOH solution to a pH of 5.7, whereby $\mathrm{acidity}=\frac{v*t}{a*0.15}*1000$
Where:

• • v=ml of NaOH solution added
  • t=molarity of NaOH solution (=0.01)
  • a=weight of sample (g)

Preferably, the caprolactam product is neutral or has an alkalinity of between 0 and 5 meq. per kg of caprolactam. In an embodiment, the process comprises adding between 0.05 and 10 mmol of the one or more bases per kg caprolactam, preferably between 0.05 and 5.0 mmol per kg, more preferably between 0.10 and 4.5 mmol per kg, in particular between 0.15 and 3.0 mmol per kg, more in particular between 0.20 and 2.0, most preferably less than 1.0 mmol per kg caprolactam. Preferably, the amount of added base is decreased when the caprolactam product is less acidic/more alkaline. In an embodiment, the alkaline caprolactam product is directly obtained after addition of the one or more bases, and the alkaline caprolactam product may be distilled without further steps prior to said distilling. In another embodiment, alkaline product obtained following the addition is subjected to one or more purification steps, e.g. to a step in which water is separated from the alkaline product, to obtain the alkaline caprolactam product to be distilled.

In a preferred embodiment, the process involves adding alkali hydroxide to the caprolactam product, yielding an alkaline product, and reacting at least part of said alkali hydroxide in the alkaline product to form alkali amino caproate prior to the distilling. This has the advantage that the alkali amino caproate can be formed without needing separate equipment for preparing said alkali amino caproate. In this embodiment, the alkali hydroxide is preferably added to caprolactam product comprising at least 3 wt. % water, more preferably at least 5 wt. % of water (relative to the total weight of the caprolactam product). Alkali hydroxide may advantageously be converted to form alkali amino caproate during a water separation step.

The process according to the invention may be a batch process or a continuous process. Preferably, the process is a continuous process.

The caprolactam product to which said one or more bases may be added may be obtained in various ways, e.g. by Beckmann rearrangement. A Beckmann rearrangement of cyclohexanone oxime may be effected in the presence of sulphuric acid or oleum, resulting in a Beckmann rearrangement mixture. A base, preferably ammonia, may be added to the Beckmann rearrangement mixture, resulting in a neutralized Beckmann rearrangent mixture. In an embodiment of the invention the preparation of the caprolactam product includes, (a) recovering from a neutralized Beckmann rearrangement mixture, by extraction with an organic solvent, an organic product comprising the organic solvent and caprolactam, (b) recovering from said organic product, by extraction with water or by evaporation of the organic solvent in the presence of water, an aqueous caprolactam product. Following its recovery from the organic product, the aqueous caprolactam product is preferably hydrogenated in the presence of a hydrogenation catalyst. In the event that the aqueous caprolactam product is recovered from the organic product by evaporation of the organic solvent in the presence of water, the organic product is preferably washed with water or with an alkaline aqueous solution prior to said evaporation. In the event that the aqueous caprolactam product is recovered from the organic product by extraction with water, the aqueous caprolactam product is preferably subjected to an ion exchanger prior to hydrogenation. Preferably said one or more bases are added to the aqueous caprolactam product after a hydrogenation step.

The distillation may be carried out in any suitable distillation zone, for instance a distillation column. The distillation is effected at reduced pressure. Preferably the distillation is effected at a pressure of less than 50 kPa, more preferably less than 20 kPa, in particular less than 10 kPa. Preferably, the temperature is between 100 and 200° C., more preferably between 110 and 180° C. These temperatures refer to the temperature in the bottom of the distillation column in which the distillation is effected. Typically, the distilling includes separating low-boiling organic impurities (having a lower boiling point than caprolactam) from the alkaline caprolactam product and/or separating organic high-boiling impurities (having a higher boiling point than caprolactam) from the alkaline caprolactam product. Preferably, the distilling includes, in a first step, separating out as a top product low-boiling impurities from the alkaline caprolactam product while leaving alkaline caprolactam product containing high-boiling impurities as a bottom product, and, in a second step, separating out high-boiling impurities from the bottom product, and recovering purified caprolactam as a top product.

Preferably, the caprolactam is ε-caprolactam

The invention will now be elucidated with reference to the following examples without, however, being limited thereto.

In all examples the specifications given were determined as follows:

• • PAN: ISO DIS 8660-Plastics-Determination of permanganate index of caprolactam-Spectometric method, revision of first edition ISO 8660; 1988,
  • E₂₉₀: ISO 7059—caprolactam for industrial use—determination of absorbance at a wavelength of 290 nm,
  • Volatile bases (VB) ISO 8661—Caprolactam for industrial use—Determination of volatile bases content—Titrimetric method after distillation.
  • Alkalinity: titration with an aqueous solution of 0.01 M hydrochloric acid.

EXAMPLE I

In a continuous process for the production of pure caprolactam, a stream of caprolactam product was continuously produced by Beckmann rearrangement of cyclohexanone oxime in the presence of oleum, neutralizing the Beckmann rearrangement mixture with ammonia, separating caprolactam from the neutralized Beckmann rearrangement by extraction techniques. Said stream was subjected to a series of purification steps including purification with an ion exchanger, hydrogenation and a first dewatering. The resulting stream of caprolactam product contained about 85 wt. % caprolactam, about 15 wt. % water, and impurities, and had the following specifications (PAN=2.6, E₂₉₀=0.32, VB=0.44 meq/kg, alkalinity=0.02 meq/kg). To this stream was continuously added 4.80 mmol NaOH per kg of caprolactam (as 15% aqueous solution). The resulting stream of alkaline caprolactam product was dewatered in a series of evaporators, the temperatures in the evaporators varying between 80 and 125° C. The total residence time in and between the evaporators was 3 hours. As a result alkaline caprolactam product was obtained containing about 0.5 wt. % water. In said alkaline caprolactam product at least 90% added base appeared to have been reacted to form sodium amino caproate. The alkaline caprolactam product (alkalinity 4.83 meq/kg) leaving the series of evaporators was distilled in two steps under reduced pressure. In the first step low-boiling impurities and water were separated in a distillation column, at (bottom) temperature of 175° C., and a pressure of 5.2 kPa, the residence time being several minutes. In the second step high-boiling impurities were separated in a distillation column at a (bottom) temperature of 133° C., a pressure of 1.2 kPa, the residence time being 1 hour. The specifications of the resulting purified caprolactam are indicated in table 1.

EXAMPLES II-VIII

Example I was repeated with the difference that different amounts of NaOH were added, resulting in different values for the alkalinity of the feed of the first distillation step (distillation at 175° C.). The specifications of the caprolactam obtained after distillation are indicated in table 1.

TABLE 1
		Alkalinity feed
	Added	First distillation
Example	NaOH	(175° C.) step	PAN	E290	VB	Alkalinity
Nr.	mmol	meq			meq	meq
	NaOH/	OH—/kg			OH−/kg	OH−/kg
	kg capr
I	4.80	4.83	3.71	0.14	0.16	0.012
II	2.90	2.92	3.60	0.13	0.14	0.015
III	1.25	1.29	3.54	0.13	0.11	0.017
IV	0.90	0.95	2.88	0.11	0.12	0.013
V	0.75	0.78	2.89	0.12	0.18	0.012
VI	0.60	0.65	2.59	0.12	0.12	0.011
VII	0.50	0.55	1.15	0.06	0.11	0.024
VIII	0.30	0.32	1.26	0.07	0.17	0.023

These examples show that the PAN number is decreased without impairing the other properties of the caprolactam, if the amount of added NaOH and, consequently, the alkalinity the alkaline caprolactam product is decreased. Moreover the extinction decreases with decreasing amount of added NaOH.

Claims

1. Process for distilling alkaline caprolactam product at reduced pressure, said alkaline caprolactam product comprising (i) caprolactam, (ii) organic impurities, and (iii) one or more bases selected from the group consisting of alkali hydroxide and alkali amino caproate, characterized in that the alkalinity of the alkaline caprolactam product is less than 5 meq. per kg of caprolactam.

2. Process according to claim 1, wherein the alkalinity of the alkaline caprolactam product is between 0.10 and 3 meq. per kg of caprolactam.

3. Process according to claim 2, wherein the alkalinity of the alkaline caprolactam product is between 0.15 and 2 meq. per kg of caprolactam.

4. Process according to claim 1, wherein said one or more bases are selected from the group consisting of sodium hydroxide, sodium amino caproate, potassium hydroxide, potassium amino caproate.

5. Process according to claim 1, wherein at least 75 mol. % of said one or more bases is alkali amino caproate.

6. Process according to claim 1, wherein said alkaline caprolactam product comprises at least 95 wt. % of caprolactam.

7. Process according to claim 1 for the purification of caprolactam product, said caprolactam product comprising (i) caprolactam and (ii) impurities, wherein said process comprises adding one or more bases selected from the group consisting of alkali hydroxide and alkali amino caproate to said caprolactam product in an amount so as to yield the alkaline caprolactam product.

8. Process according to claim 7, wherein the caprolactam product has an acidity of between 0 and 5 meq. per kg of caprolactam, is neutral, or has an alkalinity of between 0 and 5 meq. per kg of caprolactam.

9. Process according to claim 7, wherein the process involves adding said one or more bases to said caprolactam product in an amount of less than 10 mmol per kg caprolactam.

10. Process according to claim 9, wherein the process involves adding to said caprolactam product between 0.10 and 5 mmol of said one or more bases per kg of caprolactam.

11. Process according to claim 10, wherein the process involves adding to said caprolactam product between 0.15 and 3 mmol of said one or more bases per kg of caprolactam.

12. Process according to claim 7, wherein the caprolactam product comprises at least 15 wt. % of caprolactam.

13. Process according to claim 12, wherein the caprolactam product comprises water and the sum quantity of water and caprolactam in the caprolactam product is at least 95 wt. %.

14. Process according to claim 7, wherein the process involves adding alkali hydroxide to said caprolactam product yielding an alkaline product, and converting at least part of said alkali hydroxide in the alkaline product to form alkali amino caproate prior to said distilling.

15. Process according to claim 1, wherein the caprolactam is obtained by a Beckmann rearrangement.

16. Process according to claim 1, wherein the process involves distilling the alkaline caprolactam product at a temperature between 100 and 200° C.

17. Process according to claim 1, wherein the process involves distilling the alkaline caprolactam product at a pressure of less than 10 kPa.

18. Process according to claim 1, wherein said distilling includes separating out low-boiling impurities from the alkaline caprolactam product and/or separating out high-boiling impurities from the alkaline caprolactam product.

19. Process according to claim 18, wherein said distilling includes, in a first step, separating out as a top product low-boiling impurities from the alkaline caprolactam product while leaving alkaline caprolactam product containing high-boiling impurities as a bottom product, and, in a second step, separating out high-boiling impurities from the bottom product, and recovering caprolactam as a top product.

20. Process according to claim 1, wherein the process is a continuous process.