Process for the preparation of solid iron (III) complexes

Abstract

Fe(III) complexes having high bulk density and a process for the production of the same without the generation of heavy metal-contaminated effluents are disclosed. Solid complexes of EDTANaFe and EDTAKFe having high bulk densities are formed by reaction with ferric sulfate containing low chromium levels, followed by total drying of the resulting mixture in the same processing equipment without the prior separation of the sulfate salts formed.

Description

BACKGROUND OF THE INVENTION

Conventional processes for the production of solid Fe(III) chelates for agricultural and other uses generate waste crystal liquors with high concentrations of iron and heavy metals, particularly chromium. Such heavy metals are problematic from an environmental standpoint. The economic implications of properly disposing of such streams are significant, and are often prohibitive. In addition, the waste liquor can contain some soluble product. Although disposal of the waste liquors without recovering the product results in yield loss, recovery of contained product is not economical.

A conventional process for producing the complexes involves reacting chelating agents, such as EDTANa.sub.4 or DTPANa.sub.5, with ferric chloride solution, followed by filtration, washing and drying. However, one major source of chromium contamination is the ferric chloride used as the ferric iron source. Where low cost grade ferric chloride derived from scrap iron is used, the chromium concentration of the waste streams produced is on the order of 30 ppm. Higher grade ferric chloride can be used, which can reduce the chromium concentration in the waste streams to about 2-3 ppm; however, this higher grade ferric chloride is more expensive. A further drawback of ferric chloride is the highly corrosive properties of the slurries and liquors produced from the chelating agent/ferric chloride reactions.

Prior art drying processes include spray drying and drum drying. However, the resulting product is often very dusty, which creates handling problems.

Accordingly, there is a need to find an alternative production process which reduces or eliminates the generation of high heavy metal effluents without adding significant cost.

SUMMARY OF THE INVENTION

The problems of the prior art have been solved by the instant invention, which provides solid Fe(III) complexes having high bulk density and a process for the production of the same without the generation of heavy metal-contaminated effluents. In particular, the present invention relates to the production of solid complexes of EDTANaFe and EDTAKFe having high bulk densities by reaction with ferric sulfate containing low chromium levels, followed by total drying of the resulting mixture without the prior separation of the sulfate salts formed. The reaction and drying process are carried out in the same processing equipment. By eliminating the separation step and drying the total reaction product, no waste liquor is generated. The product loss of prior art processes due to the presence of some soluble product in the waste liquor is thereby eliminated.

DETAILED DESCRIPTION OF THE INVENTION

The present invention concerns a total drying process for iron(III) complexes, and the resulting products formed thereby. Preferably the equipment used is a high torque combination of a mixer or with a reactor dryer, such that the mixing or reaction and the drying are carried out in the same equipment chamber. The equipment should be constructed of stainless steel, preferably 316 stainless steel suitable equipment utilizes a mechanically fluidized ploughshare action to agitate the particles to be dried. Scrapers on the agitator shaft are instrumental in freeing the heat transfer surface of dried material. The equipment produces some agglomeration, which leads to the high bulk density of the product. In addition, high shear choppers reduce large agglomerate masses to promote thoroughly dried particle interiors. Preferably the equipment utilizes hydraulic drive. Such equipment is available from Littleford Bros., Inc., Florence, Ky.

Prior to drying, a slurry is formed by reaction of pH-adjusted chelating agents with an iron source, preferably 50% ferric sulfate solution. The reaction is illustrated for EDTANa.sub.4 as follows:

EDTANa.sub.4 +0.5Fe.sub.2 (SO.sub.4).sub.3 .fwdarw.EDTANaFe+1.5Na.sub.2 SO.sub.4. Other salts of the chelating agents can be used, such as the potassium salts. The pH-adjusted chelating agent is prepared by neutralizing free alkali metal (e.g., sodium or potassium) hydroxide with the acid chelate, or with a mineral acid, such as 50% or 93% sulfuric acid. The chelating agent is available from W. R. Grace & Co.-Conn. as Hamp-Ene.RTM. 100S and is one of the feedstocks to the reactor/dryer. A slurry is then formed by reacting the chelating agent with ferric sulfate solution at about 40.degree.-50.degree. C. Preferably the chelating agent is as concentrated as possible in order to reduce the evaporative load on the drying equipment utilized. In the same piece of equipment, the resulting slurry is vacuum dried to a blend of the alkali metal salt of the iron (III) chelate and alkali metal sulfate. In contrast to conventional spray drying processes, the instant vacuum drying employs relatively long residence times which depend upon the steam pressure and the vacuum applied.

Since the entire product is vacuum dried without separation of the alkali metal sulfate salt formed, no effluent is produced and the yield is 100% (less any physical losses that occur). Although the iron content of the final product is lower than the prior art products from which the salt has been separated, a significant savings results from the absence of any effluent and the said 100% yield of product.

One surprising aspect of the instant process is the high bulk density of the resulting product formed. A comparison of the total iron content and bulk densitites of the products formed in accordance with the instant invention with that of the iron chelate formed from a prior art process (wherein the alkali metal chloride salt has been separated) is illustrated in Table 1.

TABLE 1______________________________________ BULK DENSITYPRODUCT % Fe LB/Cu Ft______________________________________EDTANaFe (prior art) 12.6 37.1EDTANaFe/Na.sub.2 SO.sub.4 8.73 62.1EDTAKFe/K.sub.2 SO.sub.4 7.80 61.8______________________________________ The very high bulk densities of the instant products is a further advantage which offsets the slightly lower iron content of the products due to the presence of the alkali metal sulfate.

The total dried product may be milled to remove any gritty material. For commerical applications, it may be desirable to have 100% of the material pass through a 25 mesh sieve. A sieve analysis has demonstrated that about 7% of EDTANaFe/Na.sub.2 SO.sub.4 is greater than 25 mesh and therefore requires milling to meet the desirable specifications.

It would be obvious to those skilled in the art that the disclosed process should be generally applicable to preparation of the Fe(III) complexes of ligands other than EDTA.

The following examples will serve to illustrate various embodiments of the instant invention.

EXAMPLE 1

Production of EDTANaFe/Na.sub.2 SO.sub.4

The equipment used was a Littleford reactor/dryer MR5. EDTANa.sub.4 solution was charged to a hold tank and free alkali therein was neutralized with 93% sulfuric acid. As the iron source, 50% Fe.sub.2 (SO.sub.4).sub.3 was used. The Fe.sub.2 (SO.sub.4).sub.3 was charged to the reactor/dryer and warmed to about 40.degree. C. The neutralized chelate was then added in an amount of 3% excess over iron, and the resulting slurry was vacuumed dried to a blend of EDTANaFe and Na.sub.2 SO.sub.4. The data are provided in Table II.

EXAMPLE 2

Production of EDTAKFe/K.sub.2 SO.sub.4

The reaction and drying were carried out as in Example 1, except that the chelating agent was EDTAK.sub.4 solution. The data are provided in Table III.

TABLE II__________________________________________________________________________ % Active Molecular Weight At Ingredient Weight Moles 100% Actual A.I. Sp. Gravity Lb/gal Gallons__________________________________________________________________________TO PRODUCE EDTANaFe - PRODUCT CODE NOS. 150 & 600HampEne 100 S (EDTANa4) 38.0% 380.2 1.030 392 1031 1.270 10.6 97.4Free NaOH in H-100 S 1.5% 40.0 0.386 15H2SO4 93.0% 98.0 0.193 19 20 1.840 15.3 1.3Fe2(SO4)3 50.0% 399.9 0.500 200 400 1.440 12.0 33.3Water 0Total 1451 132.1PRODUCTEDTANaFe 367.1 1.000 367Na2SO4 142.0 1.693 240Total Anhydrous Pure Product 608Total Product @ Fe Content of 8.7% 642__________________________________________________________________________ SCALE = 1.0 LB MOLE OF IRON Note: the 8.7% Fe value was the Fe content of product produced from the Littleford trial TABLE III__________________________________________________________________________TO PRODUCE EDTAKFe__________________________________________________________________________HampEne K4 100 S (EDTAK4) 44.4% 444.6 1.030 458 1031 1.320 11.0 93.8Free KOH in H-K4-100 S 1.5% 56.1 0.276 15H2SO4 93.0% 98.0 0.138 14 15 1.840 15.3 0.9Fe2(SO4)3 50.0% 399.9 0.500 200 400 1.440 12.0 33.3Water 0Total 1446 128.1PRODUCTEDTAKFe 383.2 1.000 383K2SO4 174.3 1.638 285Total Anhydrous Pure Product 669Total Product @ Fe Content of 7.8% 716__________________________________________________________________________ Note: the 7.8% Fe value was the Fe content of product produced from the Littleford trial

Claims

1. A process for producing iron (III) complexes of alkali metal salts of EDTA, comprising:

a. neutralizing free alkali present in an alkali metal salt solution of EDTA with and neutralizing free alkali in the alkali metal salt solution of EDTA with acid;

b. reacting the neutralized alkali metal salt solution with ferric sulfate to form a slurry containing alkali metal sulfate.

c. vacuum drying said slurry without the prior separation of said alkali metal sulfate, said reacting and vacuum drying steps being carried out in the same processing equipment.

2. The process of claim 1 wherein the alkali metal salt of EDTA is EDTANa.sub.4.

3. The process of claim 1 wherein the alkali metal salt of EDTA is EDTAK.sub.4.

4. The process of claim 1 wherein the neutralization is carried out with EDTA acid.

5. The process of claim 1 wherein the neutralization is carried out with sulfuric acid.