Process for producing ammonium (meth-) acrylate

DESCRIPTION

The present invention relates to a process for preparing ammonium (meth-) acrylate, aqueous ammonium (meth-) acrylate solutions obtainable by such process, and (meth- ) acrylic acid homopolymers or copolymers obtainable by polymerizing such ammonium (meth-) acrylate. The invention furthermore relates to a modular, relocatable bioconversion unit for manufacturing aqueous ammonium (meth-) acrylate solutions.

BACKGROUND OF THE INVENTION

Homopolymers of acrylic acid may be used for various applications such as surface coatings, adhesives, sealants, etc. Copolymers of (meth-) acrylic acid and for example acrylamide may be used for applications such as mining and oilfield applications, and agriculture. Examples include its use in the exploration and production of mineral oil, in particular, as thickener in aqueous injection fluids for enhanced oil recovery or as rheology modifier for aqueous drilling fluids. Further examples include its use as flocculating agent for tailings and slurries in mining activities.

The raw material for homo- and copolymers of acrylic acid is typically the monomer acrylic acid. In the case of copolymers in addition to acrylic acid the raw material would also include at least one further ethylenically unsaturated monomer that is co- polymerisable with acrylic acid, and typically this would frequently be acrylamide. In principal, there exists two different methods to produce acrylic acid on an industrial scale: Chemical synthesis and biological synthesis, wherein the biological synthesis methods are more and more on the rise due to milder reaction conditions and inherent process safety. Due to the milder reaction conditions and the quantitative conversion of the nitrile, expensive downstream processing steps such as distillation or ion exchange can be avoided in the biological synthesis, thus resulting in cheaper plants with drastically reduced plant footprint.

There are two distinct pathways for the enzymatic hydration of nitriles in plants and microorganisms that have been applied in industrial production of acrylic acid. One pathway comprises two enzymatic steps wherein a nitrile hydratase converts a nitrile to an amide which subsequently is hydrolysed by an amidase to yield acrylic acid

(US6670158). The other pathway is a single-step reaction catalysed by nitrilases (US6162624), which is advantageous compared to the two-step reaction, because the latter requiring an extensive amount of equipment for the two stages. WO 97/21817 discloses suitable conditions for carrying out the enzymatic hydration of nitriles using nitrilases. US 2009/0311759 describes a process for producing acrylamide by allowing acrylonitrile to undergo a hydration reaction by the use of a microbial catalyst containing nitrile hydratase in an aqueous medium to obtain acrylamide reaction solution. The process includes a step of removing impurities from the reaction solution.

However, even when using a single-step reaction catalysed by nitrilases, for the obtained acrylic acid still further processing steps like purification and drying are necessary in order to obtain acrylic acid, which is suitable for the production of homo- and/or copolymers in acceptable quality. More specifically, without cleaning and drying before storage, aqueous ammonium (meth-) acrylate solutions could degrade, which could lead to reduced performance of the resulting polymers.

SUMMARY OF THE INVENTION

In the light of the prior art the technical problem underlying the present invention was the provision of a process for preparing aqueous ammonium (meth-) acrylate solutions that overcome the disadvantages of those methods known in the art. The process for preparing aqueous ammonium (meth-) acrylate solutions of the present invention comprises a relocatable bioconversion unit. Due to the conductions of the

bioconversion in a relocatable bioconversion unit, cleaning and drying steps can be avoided. The method for preparing an aqueous ammonium (meth-) acrylate solution enables high product quality for subsequent polymer production and overcomes the disadvantages known in the art.

The problem is solved by the features of the independent claims. Preferred

embodiments of the present invention are provided by the dependent claims.

The invention therefore relates to a process for producing aqueous ammonium (meth-) acrylate solutions, said process comprising the following steps:

(a) adding the following components (i) to (iii) to a reactor to obtain a composition for bioconversion:

(i) a biocatalyst capable of converting (meth-) acrylonitrile to ammonium (meth-) acrylate;

(ii) (meth-) acrylonitrile;

(iii) aqueous medium; and

(b) performing a bioconversion on the composition obtained in step (a) in a reactor; wherein the reactor is a relocatable bioconversion unit. The composition obtained in step (a) is also called reaction mixture.

In a preferred embodiment the (meth-) acrylonitrile concentration of the composition at the end of the bioconversion is below 10.0 % (w/w), is below 1.0 % (w/w), is below 0.1 % (w/w), preferably below 0.01 % (w/w), more preferably below 0.001 % (w/w), most preferably below 0.0001 % (w/w) by weight of the (meth-) acrylonitrile in the aqueous medium.

In a preferred embodiment the concentration of ammonium (meth-) acrylate at the end of the bioconversion is at least 10% (w/w), at least 15% (w/w), at least 20% (w/w), at least 25% (w/w), at least 30% (w/w), at least 35% (w/w), preferably at least 40% (w/w), at least 45% (w/w), more preferably at least 50% (w/w), more preferably at least 51 % (w/w), more preferably at least 52% (w/w), more preferably at least 53% (w/w), even more preferably at least 54% (w/w), most preferably at least 55% (w/w) by weight of the ammonium (meth-) acrylate monomers in the aqueous medium.

In a preferred embodiment the biocatalyst is an enzyme having nitrilase activity.

In a preferred embodiment the biocatalyst having nitrilase activity is one selected from the group consisting of an isolated nitrilase, a recombinant construct, a recombinant vector comprising the recombinant construct, a recombinant microorganism comprising the recombinant construct, and a recombinant microorganism comprising the recombinant vector.

In a preferred embodiment the biocatalyst is a recombinant microorganism selected from the group consisting of Bacillus Hcheniformis, Bacillus pumilus, Bacillus subtiHs, Escherichia coH, Saccharomyces cerevisiae, Rhodococcus rhodocrous, and Pichia pastoris.

In a preferred embodiment the relocatable bioconversion unit comprises a reaction vessel having a volume from 10 m ³ to 150 m ³ , means for mixing the reaction mixture and means for controlling the temperature of the reaction mixture. This may for instance be from about 20 m ³ to about 120 m ³ , suitably from about 20 m ³ to about 100 m ³ , preferably from about 20 m ³ to 50 m ³ . The reaction vessel the reaction vessel may, for instance, be a single walled reaction vessel.

In an alternative embodiment the relocatable bioconversion unit comprises a double- walled reaction vessel having a volume from 10 m ³ to 150 m ³ , means for mixing the reaction mixture and means for controlling the temperature of the reaction mixture. This may for instance be from about 20 m ³ to about 120 m ³ , suitably from about 20 m ³ to about 100 m ³ , preferably from about 20 m ³ to 50 m ³ .

In a preferred embodiment the relocatable bioconversion unit comprises a frame, a double-walled reaction vessel mounted into the frame having a volume from 10 m ³ to 150 m ³ , and an external temperature control circuit comprising at least a pump and a temperature control unit, wherein the reaction mixture is circulated by means of a pump from the reaction vessel into the temperature control unit and back into the reaction vessel, thereby simultaneously controlling the temperature and mixing the reaction mixture.

In a preferred embodiment the relocatable bioconversion unit comprises a frame, a single-walled reaction vessel mounted into the frame having a volume from 10 m ³ to 150 m ³ , and an external temperature control circuit comprising at least a pump and a temperature control unit, wherein the reaction mixture is circulated by means of a pump from the reaction vessel into the temperature control unit and back into the reaction vessel, thereby simultaneously controlling the temperature and mixing the reaction mixture.

In a preferred embodiment the amount of reaction mixture cycled per hour through the temperature control circuit is from 100 % to 1000 % of the total volume of the reaction mixture in the bioconversion unit.

A further aspect of the invention relates to a reactor for manufacturing aqueous ammonium (meth-) acrylate solutions according to the process of the present invention, wherein the reactor is a relocatable bioconversion unit.

The reactor may comprise a stirrer. Suitably the reactor may comprise an external cooling circuit. It may be desirable for the reactor to comprise a stirrer and an external cooling circuit. It is preferable, however, for the reactor to comprise no stirrer. In a preferred embodiment the reactor comprises an external cooling circuit and the reactor comprises no stirrer. By stirrer we mean any active mixing device located in the reactor. Typically, a stirrer may be an impeller, an agitator mounted within the reactor or a moving device which is not fixed, such as a magnetic stirrer. By a reactor comprising no stirrer we mean that no active mixing device is located in the reactor.

In a preferred embodiment the reactor comprises

o a relocatable storage unit for (meth-) acrylonitrile,

o a relocatable bioconversion unit for hydrolyzing (meth-) acrylonitrile in water in the presence of a biocatalyst capable of converting (meth-) acrylonitrile to ammonium (meth-) acrylate,

o optionally, a relocatable unit for removing the biocatalyst from an aqueous

ammonium (meth-) acrylate solution,

o optionally, a relocatable storage unit for an aqueous ammonium (meth-) acrylate solution, and o optionally, at least one relocatable unit for further processing an aqueous ammonium (meth-) acrylate solution.

In a preferred embodiment the reactor for manufacturing aqueous ammonium (meth-) acrylate solutions according to the present invention is used at a fixed production facility.

In a preferred embodiment the reactor for manufacturing aqueous ammonium (meth-) acrylate solutions according to the present invention is combined with a relocatable bioconversion unit for manufacturing an aqueous acrylamide solution.

A further aspect of the invention relates to aqueous ammonium (meth-) acrylate solutions obtainable by the process of the present invention.

A further aspect of the invention relates to (meth-) acrylate homopolymers or copolymers obtainable by polymerizing the ammonium (meth-) acrylate of the aqueous solution.

A further aspect of the invention relates to the use of aqueous ammonium (meth-) acrylate solutions prepared according to the present invention for preparing aqueous solutions of (meth-) acrylate homopolymers or copolymers.

A further aspect of the invention relates to the use of aqueous solutions of (meth-) acrylate homopolymers or copolymers according to the present invention as surface coatings, adhesives, sealants, for mining applications, oilfield applications, water treatment, waste water treatment, paper making or agricultural applications.

DETAILED DESCRIPTION OF THE INVENTION

With regards to the invention, the following can be stated specifically:

In a first aspect the invention relates to a process for producing ammonium (meth-) acrylate, said process comprising the following steps:

(a) adding the following components (i) to (iii) to a reactor to obtain a composition for bioconversion:

(i) a biocatalyst capable of converting (meth-) acrylonitrile to ammonium (meth-) acrylate;

(ii) (meth-) acrylonitrile;

(iii) aqueous medium; and

(b) performing a bioconversion on the composition obtained in step (a) in a reactor; wherein the reactor is a relocatable bioconversion unit.

Surprisingly, it was found that using a relocatable bioconversion unit, aqueous ammonium (meth-) acrylate solutions are obtained, which are suitable for further processing to produce homo- and/or copolymers of (meth-) acrylic acid without drying the obtained aqueous ammonium (meth-) acrylate solutions. With that, drying as time consuming additional process step can be avoided. Surprising was also that the quality of the obtained homo- or copolymers of (meth-) acrylic acid are comparable with the quality of polymers prepared with acrylic acid, which has been cleaned and dried before polymerization. Therefore, a further advantage of the present invention is that for example better subsequent products / polymers can be obtained. Of advantage is also that with avoiding a drying step, the formation of ammonia gas during drying of aqueous ammonium (meth-) acrylate solutions can be avoided. In addition, for the production of copolymers comprising acrylic acid and acrylamide the same educt, namely acrylonitrile, can be used for the production of two different monomers. This offers the advantage of a more efficient sourcing and less transportation. Furthermore, with producing ammonium (meth-) acrylate in situ it is possible to avoid costly and risky transportation of caustic base, which would otherwise be necessary for neutralizing dried acrylic acid before polymerization. Also, risky transportation of caustic acrylic acid can be avoided. Beneficial is in addition the possibility to avoid a separation (e.g.

centrifugation), a purification and/or drying step of the obtained aqueous ammonium (meth-) acrylate solution (ammonium (meth-) acrylate), which will make the further processing of the aqueous ammonium (meth-) acrylate solution according to the present invention easier. Also, a direct use of the aqueous ammonium (meth-) acrylate solution at the site of further processing and/or the use for a subsequent polymer production e.g. to form homopolymers of (meth-) acrylic acid and/or copolymers (e.g. of (meth-) acrylic acid and acrylamide) at the site of application is possible.

Ammonium (meth-) acrylate

As used herein, the term“ammonium (meth-) acrylate” in the context of this invention means ammonium (meth-) acrylate that may be synthesized by hydrolysis of (meth-) acrylonitrile using suitable catalysts. It is known in the art to use biocatalysts capable of converting (meth-) acrylonitrile to ammonium (meth-) acrylate (often referred to as“bio ammonium (meth-) acrylate”). Pure (meth-) acrylic acid is solid. However, typically ammonium (meth-) acrylate according to the present invention is made by bio catalysis and is provided as aqueous solution, for example as aqueous solution comprising about 50 % by wt. of ammonium (meth-) acrylate. Ammonium (meth-) acrylate obtained by means of biocatalysts may still comprise traces of the biocatalyst. For the process according to the present invention an aqueous ammonium (meth-) acrylate solution is used which has been obtained by hydrolyzing (meth-) acrylonitrile in water in presence of a biocatalyst capable of converting (meth-) acrylonitrile to ammonium (meth-) acrylate. As will be detailed below, using biocatalysts for hydrolyzing (meth-) acrylonitrile has significant advantages for the present invention.

Biocatalyst As used herein, the term“biocatalyst” in the context of this invention means nitrilase enzymes, which are capable of catalyzing the hydrolysis of (meth-) acrylonitrile to ammonium (meth-) acrylate. The conversion of (meth-) acrylonitrile to ammonium (meth-) acrylate using a biocatalyst may be called“bioconversion” or“bio-catalysis”.

Preferably, the biocatalyst according to the present invention may be an enzyme with nitrilase activity comprising the sequence selected from the group consisting of an amino acid molecule of SEQ ID NO: 2, 4, 6, 8, 10, 12, 14, 18, 20, 22, 26, 28, 30, 32, 34, 38, 40, 42, 46, 48, 52, 54, 56, 60, 62, 64, 66 and 68 or a functional fragment thereof. Further preferred is that the biocatalyst is an enzyme with nitrilase activity comprising the sequence selected from the group consisting of an amino acid molecule encoded by a nucleic acid molecule of SEQ ID NO 1 , 3, 5, 7, 9, 1 1 , 13, 15, 17, 19, 21 , 25, 27, 29, 31 , 33, 37, 39, 41 , 45, 47, 51 , 53, 55, 59, 61 , 63, 65 and 67 or a functional fragment thereof.

Preferably, the biocatalyst is an isolated nitrilase, a recombinant construct or a recombinant vector, which in particular is comprising said recombinant construct. Further preferred is that the biocatalyst is a recombinant microorganism comprising said recombinant construct or said recombinant vector.

Typically, nitrilase enzymes can be produced by a variety of microorganisms. Preferred microorganisms that can be used in the present invention include, but are not limited to, Gluconobacter oxydans, Gluconobacter asaii, Achromobacter delmarvae,

Achromobacter viscosus, Achromobacter lacticum, Agrobacterium tumefaciens, Agrobacterium radiobacter, Alcaligenes faecalis, Arthrobacter citreus, Arthrobacter tumescens, Arthrobacter paraffineus, Arthrobacter hydrocarboglutamicus, Arthrobacter oxydans, Aureobacterium saperdae, Azotobacter indicus, Brevibacterium

ammoniagenes, Brevibacterium divaricatum, Brevibacterium lactofermentum,

Brevibacterium flavum, Brevibacterium globosum, Brevibacterium fuscum,

Brevibacterium ketoglutamicum, Brevibacterium helcolum, Brevibacterium pusillum, Brevibacterium testaceum, Brevibacterium roseum, Brevibacterium immariophilium, Brevibacterium linens, Brevibacterium protopharmiae, Corynebacterium acetophilum, Corynebacterium glutamicum, Corynebacterium callunae, Corynebacterium

acetoacidophilum, Corynebacterium acetoglutamicum, Enterobacter aerogenes,

Erwinia amylovora, Erwinia carotovora, Erwinia herbicola, Erwinia chrysanthemi, Flavobacterium peregrinum, Flavobacterium fucatum, Flavobacterium aurantinum, Flavobacterium rhenanum, Flavobacterium sewanense, Flavobacterium breve, Flavobacterium meningosepticum, Micrococcus sp. CCM825, Morganella morganii, Nocardia opaca, Nocardia rugosa, Planococcus eucinatus, Proteus rettgeri,

Propionibacterium shermanii, Pseudomonas synxantha, Pseudomonas azotoformans, Pseudomonas jluorescens, Pseudomonas ovalis, Pseudomonas stutzeri, Pseudomonas acidovolans, Pseudomonas mucidolens, Pseudomonas testosteroni, Pseudomonas aeruginosa, Rhodococcus erythropolis, Rhodococcus rhodochrous, Rhodococcus sp. ATCC 15592, Rhodococcus sp. ATCC 19070, Sporosarcina ureae, Staphylococcus aureus, Vibrio metschnikovii, Vibrio tyrogenes, Actinomadura madurae, Actinomyces violaceochromogenes, Kitasatosporia parulosa, Streptomyces avermitilis, Streptomyces coelicolor, Streptomyces flavelus, Streptomyces griseolus, Streptomyces lividans, Streptomyces olivaceus, Streptomyces tanashiensis,

Streptomyces virginiae, Streptomyces antibioticus, Streptomyces cacaoi, Streptomyces lavendulae, Streptomyces viridochromogenes, Aeromonas salmonicida, Bacillus pumilus, Bacillus circulans, Bacillus thiaminolyticus, Escherichia freundii,

Microbacterium ammoniaphilum, Serratia marcescens, Salmonella typhimurium, Salmonella schottmulleri, Xanthomonas citri, Synechocystis sp., Synechococcus elongatus, Thermosynechococcus elongatus, Microcystis aeruginosa, Nostoc sp., N. commune, N.sphaericum, Nostoc punctiforme , Spirulina platensis, Lyngbya majuscula, L. lagerheimii, Phormidium tenue, Anabaena sp., Leptolyngbya sp and so forth.

In some preferred embodiments, the microorganism is a eukaryotic cell. Suitable eukaryotic cells include yeast cells, as for example Saccharomyces spec, such as Saccharomyces cerevisiae, Hansenula spec, such as Hansenula polymorpha,

Schizosaccharomyces spec, such as Schizosaccharomyces pombe, Kluyveromyces spec, such as Kluyveromyces lactis and Kluyveromyces marxianus, Yarrowia spec, such as Yarrowia lipolytica, Pichia spec, such as Pichia methanolica, Pichia stipites and Pichia pastoris, Zygosaccharomyces spec, such as Zygosaccharomyces rouxii and Zygosaccharomyces bailii, Candida spec, such as Candida boidinii, Candida utilis, Candida freyschussii, Candida glabrata and Candida sonorensis, Schwanniomyces spec, such as Schwanniomyces occidentalis, Arxula spec, such as Arxula

adeninivorans, Ogataea spec such as Ogataea minuta, Klebsiella spec, such as Klebsiella pneumonia.

A microorganism of the genus Cupriavidus basilensis, Flavihumibacter solisilvae, Acidovorax facilis 72W, Pseudomonas sp. RIT357, Nocardia brasiliensis NBRC 14402, Pseudomonas fluorscens, Agrobacterium rubi, Candidatus Dadabacteria bacterium CSP1-2, Tepidicaulis marinus, Synechococcus sp. CC9605, Aquimarina atlantica, Arthrobacter sp., Sphingomonas wittichii RW1 , Pseudomonas mandelii JR-1 ,

Salinisphaera shabanensis E1 L3A, Smithella sp. SDB, Bradyrhizobium diazoefficiens, Actinobacteria bacterium RBG_13_55_18, Rhizobium sp. YK2 or Bacterium YEK0313 expressing any of the nitrilases of the invention is another preferred embodiment of the invention.

Further, microorganisms suitable as biocatalyst for the enzymatic conversion of (meth-) acrylonitrile to ammonium (meth-) acrylate, which are known for a person skilled in the art, are able to be applied according to the present invention. Additionally, the specific methods known in the art of culturing (or cultivation, or fermentation) and/or storing the microorganism as well as the respective sequences of polynucleotides which are encoding the enzyme, particularly the nitrilase, are applicable in context of the present invention.

The term "isolated" as used herein means that a material has been removed by the hand of man and exists apart from its original, native environment and is therefore not a product of nature. An isolated material or molecule (such as a DNA molecule or enzyme) may exist in a purified form or may exist in a non-native environment such as, for example, in a transgenic host cell. For example, a naturally occurring nucleic acid molecule or polypeptide present in a living cell is not isolated, but the same nucleic acid molecule or polypeptide, separated from some or all of the coexisting materials in the natural system, is isolated. Such nucleic acid molecules can be part of a vector and/or such nucleic acid molecules or polypeptides could be part of a composition, and would be isolated in that such a vector or composition is not part of its original environment. Preferably, the term "isolated" when used in relation to a nucleic acid molecule, as in "an isolated nucleic acid sequence" refers to a nucleic acid sequence that is identified and separated from at least one contaminant nucleic acid molecule with which it is ordinarily associated in its natural source. Isolated nucleic acid molecule is nucleic acid molecule present in a form or setting that is different from that in which it is found in nature. In contrast, non-isolated nucleic acid molecules are nucleic acid molecules such as DNA and RNA, which are found in the state they exist in nature. For example, a given DNA sequence (e.g., a gene) is found on the host cell chromosome in proximity to neighboring genes; RNA sequences, such as a specific mRNA sequence encoding a specific protein, are found in the cell as a mixture with numerous other mRNAs, which encode a multitude of proteins. However, an isolated nucleic acid sequence comprising for example SEQ ID NO: 1 includes, by way of example, such nucleic acid sequences in cells which ordinarily contain SEQ ID NO: 1 where the nucleic acid sequence is in a genomic or plasmid location different from that of natural cells, or is otherwise flanked by a different nucleic acid sequence than that found in nature. The isolated nucleic acid sequence may be present in single- or double-stranded form. When an isolated nucleic acid sequence is to be utilized to express a protein, the nucleic acid sequence will contain at a minimum at least a portion of the sense or coding strand (i.e., the nucleic acid sequence may be single-stranded). Alternatively, it may contain both the sense and anti-sense strands (i.e., the nucleic acid sequence may be double-stranded).

The term“nitrilase” as used herein refers to an enzyme catalyzing the reaction from meth-acrylonitrile to ammonium meth-acrylate and / or the reaction from acrylonitrile to ammonium acrylate. It also encompasses enzymes that are catalyzing additional reactions despite those mentioned before.

As used herein, the term“nitrilase producing microorganism” or“microorganism” or “biocatalysts” or the like in the context of this invention have the meaning to be able to produce (i.e. they encode and express) the enzyme nitrilase either per se (naturally) or they have been genetically modified respectively. Microorganisms which have been “genetically modified” means that these microorganisms have been manipulated such that they have acquired the capability to express the required enzyme nitrilase, e.g. by way of incorporation of a naturally and/or modified nitrile hydratase gene or gene cluster or the like. Produced products of the microorganisms that can be used in the context of the present invention are also contemplated, e.g. suspensions obtained by partial or complete cell disruption of the microorganisms.

The terms“nitrilase producing microorganism” or“microorganism” or“biocatalysts” or the like, include the cells and/or the processed product thereof as such, and/or suspensions containing such microorganisms and/or processed products. It is also envisaged that the microorganisms and/or processed products thereof are further treated before they are employed in the embodiments of the present invention.“Further treated” thereby includes for example washing steps and/or steps to concentrate the microorganism etc. It is also envisaged that the microorganisms that are employed in the embodiments of the present invention have been pre-treated by a for example drying step. Also known methods for cultivating of the microorganisms and how to optimize the cultivation conditions via for example addition of urea or cobalt are compassed by the embodiments of the present invention. Advantageously, the microorganism can be grown in a medium containing urea, acetonitrile or acrylonitrile as an inducer of the nitrilase.

As used herein, the term "vector" refers to a nucleic acid molecule capable of transporting another nucleic acid molecule to which it has been linked. One type of vector is a genomic integrated vector, or "integrated vector", which can become integrated into the genomic DNA of the host cell. Another type of vector is an episomal vector, i.e., a plasmid or a nucleic acid molecule capable of extra-chromosomal replication. Vectors capable of directing the expression of genes to which they are operatively linked are referred to herein as "expression vectors". In the present specification, "plasmid" and "vector" are used interchangeably unless otherwise clear from the context.

The term“recombinant microorganism” includes microorganisms which have been genetically modified such that they exhibit an altered or different genotype and/or phenotype (e. g., when the genetic modification affects coding nucleic acid sequences of the microorganism) as compared to the wild type microorganism from which it was derived. A recombinant microorganism comprises at least one recombinant nucleic acid molecule.

The term "recombinant" with respect to nucleic acid molecules refers to nucleic acid molecules produced by man using recombinant nucleic acid techniques. The term comprises nucleic acid molecules which as such do not exist in nature or do not exist in the organism from which the nucleic acid molecule is derived, but are modified, changed, mutated or otherwise manipulated by man. Preferably, a "recombinant nucleic acid molecule" is a non-naturally occurring nucleic acid molecule that differs in sequence from a naturally occurring nucleic acid molecule by at least one nucleic acid. A“recombinant nucleic acid molecules” may also comprise a“recombinant construct” which comprises, preferably operably linked, a sequence of nucleic acid molecules not naturally occurring in that order. Preferred methods for producing said recombinant nucleic acid molecules may comprise cloning techniques, directed or non-directed mutagenesis, gene synthesis or recombination techniques.

Preferably, the biocatalyst for converting (meth-) acrylonitrile to ammonium (meth-) acrylate may be obtained from culturing the microorganism in a suitable growth medium. The growth medium, also called fermentation (culture) medium, fermentation broth, fermentation mixture, or the like, may comprise typical components like sugars, polysaccharides. For storage of the microorganism, the fermentation broth preferably is removed in order to prevent putrefaction, which could result in a reduction of nitrile hydratase activity. Preferably, the storage does not influence biocatalytic activity or does not lead to a reduction in biocatalytic activity. The biocatalyst may be stored in presence of the fermentation broth components. Preferred in the sense of the present invention is that the biocatalyst may be stored in form of a frozen suspension and may be thawed before use. Further, the biocatalyst may be stored in dried form using freeze-drying, spray drying, heat drying, vacuum drying, fluidized bed drying and/or spray granulation.

The biocatalysts that are used according to the present invention can for example be cultured under any conditions suitable for the purpose in accordance with any of the known methods, for instance as described in the mentioned prior art of this

specification. The biocatalyst may be used as a whole cell catalyst for the generation of acid from nitrile. The biocatalyst may be (partly) immobilized for instance entrapped in a gel or it may be used for example as a free cell suspension. For immobilization well known standard methods can be applied like for example entrapment cross linkage such as glutaraldehyde-polyethyleneimine (GA-PEI) crosslinking, cross linking to a matrix and/or carrier binding etc., including variations and/or combinations of the aforementioned methods. Alternatively, the nitrilase enzyme may be extracted and for instance may be used directly in the process for preparing the amide. When using inactivated or partly inactivated cells, such cells may be inactivated by thermal or chemical treatment.

In a preferred embodiment, the microorganisms are whole cells. The whole cells may be pre-treated by a drying step. The microorganisms that are employed in the context of the present invention may in a preferred embodiment also be used in an aqueous suspension and in a more preferred embodiment are free whole cells in an aqueous suspension. The term "aqueous suspension" thereby includes all kinds of liquids, such as buffers or culture medium that are suitable to keep microorganisms in suspension. Such liquids are well-known to the skilled person and include for example storage buffers at suitable pH such as storage buffers which are used to store microorganisms, TRIS-based buffers, phosphate based buffers, saline based buffers, water in all quality grades such as distilled water, pure water, tap water, or sea water, culture medium, growing medium, nutrient solutions, or fermentation broths, for example the

fermentation broth that was used to culture the microorganisms. During storage for example the aqueous suspension is frozen and thawed before use.

The biocatalyst may be provided as powder, as granulate or as aqueous suspension to the reactor for bioconversion. If provided as powder or granulate it is frequently advisable to prepare an aqueous suspension before adding the catalyst into the reactor / bioconversion unit. In an embodiment, the biocatalyst suspension may be conducted by suspending the biocatalyst powder in water in a vessel comprising at least a mixing device, for example a stirrer, one or more inlets for water, the biocatalyst and optionally further additives and one outlet for the biocatalyst suspension. The volume of the vessel may be for example from 0.1 m ³ to 1 m ³ . The concentration of the biocatalyst in the aqueous biocatalyst suspension may be for example from 1 % to 30% by wt, for example from 5 to 15% by wt. relating to the total of all components of the aqueous suspension. A biocatalyst suspension may be added directly to the bioconversion unit. In another embodiment, a concentrated suspension may be diluted before adding it to the bioconversion unit / reactor where the bioconversion takes place.

Bioconversion

The term“bioconversion” as used herein in the context with any one of the methods of the present invention in general denotes a reaction, wherein (meth-) acrylonitrile is converted to ammonium (meth-) acrylate in the presence of aqueous medium and a biocatalyst. As used herein, the term“composition” includes all components present in the reactor, such as, for example, the biocatalyst, (meth-) acrylonitrile, ammonium (meth-) acrylate and water. The composition may also be called reaction mixture.

Particularly, the bioconversion is performed by contacting a mixture comprising aqueous medium and (meth-) acrylonitrile with the biocatalyst. The term“contacting” is not specifically limited and includes for example bringing into contact with, mixing, admixing, shaking, pouring into, flowing into, or incorporating into. It is thus only decisive that the mentioned ingredients come into contact with each other no matter how that contact is achieved. Aqueous medium comprises all kinds of aqueous liquids, such as buffers at suitable pH, TRIS-based buffers, phosphate based buffers, saline based buffers, water in all quality grades such as distilled water, pure water, tap water, or sea water. The buffer pH is for example in the range of 4 to 9.

Therefore, in one embodiment the present invention relates to a process for producing ammonium (meth-) acrylate, said process comprising the following steps:

(a) adding the following components (i) to (iii) to a reactor to obtain a composition for bioconversion:

(i) a biocatalyst capable of converting (meth-) acrylonitrile to ammonium (meth-) acrylate;

(ii) (meth-) acrylonitrile;

(iii) aqueous medium comprising water; and

(b) performing a bioconversion on the composition obtained in step (a) in a reactor; wherein the reactor is a relocatable bioconversion unit.

The addition of components (i) to (iii) in step (a) may take place in any order or sequence. Also preparing a pre-mix of some or all components (i) to (iii) is possible to obtain a composition for bioconversion according to step (a). The bioconversion can for example be conducted under any conditions suitable for the purpose in accordance with any of the known methods.

When adding the biocatalyst to the reactor in any one of the methods (process) of the present invention, the biocatalyst may be taken directly from the fermentation broth. Alternatively, in accordance with any one of the methods described herein, the biocatalyst may have been dried before being added to the reactor. In this context the term“before” does not necessarily mean that the biocatalyst has been dried and is then directly added to the reactor. It is rather sufficient that the biocatalyst has undergone a drying step at any time before it is added to the reactor, independently of whether further steps between the drying and the addition are performed or not. As non-limiting examples, such further steps between the drying step and the addition to the reactor may be storage or reconstitution. However, it is also possible to add the biocatalyst to the reactor directly after drying. According to any one of the methods of the present invention a dried biocatalyst may be added to the reactor. This means that the biocatalyst is added to the reactor in a dried form. In particular, the biocatalyst may have the form of a powder or a granule. As an alternative to adding a dried biocatalyst to the reactor, the dried biocatalyst may be reconstituted before being added to the reactor. For example, the biocatalyst may be reconstituted by suspending in an aqueous composition. With this respect, the aqueous composition may be water or a buffer. As a further alternative, a biocatalyst in form of a matrix bound microorganism may be added to the reactor. The conversion of (meth-) acrylonitrile to ammonium (meth-) acrylate may be carried out by any of a batch process and a continuous process, and the conversion may be carried out by selecting its reaction system from reaction systems such as suspended bed, a fixed bed, a fluidized bed and the like or by combining different reaction systems according to the form of the catalyst. Particularly, the method of the present invention may be carried out using a semi-batch process. In particular, the term "semi-batch process" as used herein may comprise that an aqueous ammonium (meth-) acrylate solution is produced in a discontinuous manner. In yet another embodiment, the biocatalyst is recovered from the reaction mixture after the bioconversion and re-used in a subsequent bioconversion reaction.

According to a non-limiting example for carrying out such a semi-batch process water, a certain amount of (meth-) acrylonitrile and the biocatalyst are placed in the bioconversion unit. Further (meth-) acrylonitrile is then added during the bioconversion until a desired content of ammonium (meth-) acrylate of the composition is reached. After such desired content of ammonium (meth-) acrylate is reached, the obtained composition is for example partly or entirely recovered from the reactor, before new reactants are placed therein. In particular, in any one of the methods of the present invention the (meth-) acrylonitrile may be fed such that the content of (meth-) acrylonitrile during step (b) is maintained substantially constant at a predetermined value. In general, in any one of the methods of the present invention the (meth-) acrylonitrile content and/or the ammonium (meth-) acrylate content during step (b) may be monitored. Methods of monitoring the contents are not limited and include Fourier Transform Infrared Spectroscopy (FTIR). In another embodiment, the heat-balance of the reaction may be used for monitoring the process. This means that monitoring via heat-balance method takes place by measuring the heat energy of the system during bioconversion and by calculating the loss of heat energy during the reaction in order to monitor the process.

Although the conversion of (meth-) acrylonitrile to the ammonium (meth-) acrylate may preferably be carried out at atmospheric pressure, it may be carried out under pressure in order to increase solubility of acrylonitrile in the aqueous medium. Because biocatalysts are temperature sensitive and the hydrolysis is an exothermic reaction temperature control is important. The reaction temperature is not specifically restricted provided that it is not lower than the freezing point of the aqueous medium. However, it is desirable to carry out the bioconversion at a temperature of usually 0 to 50°C, preferably 10 to 40°C, more preferably 15 to 30°C. It is possible that the temperature may vary over time during the bioconversion reaction. Further suitable conditions for the bioconversion according to the present invention are for example at least 15°C, at least 20°C, at least 24°C or at least 28°C. Preferably the aqueous medium with the composition for bioconversion is incubated between including 27°C and 33°C, more preferably the aqueous medium is incubated between including 28°C and 30°C. Most preferably the aqueous medium is incubated at 28°C. The aqueous medium may also be incubated at 38°C, 39°C, 40°C, 41 °C, 42°C, 43°C, 44°C, 45°C, 46°C, 47°C, 48°C, 49°C or 50°C.

At the start of the process of the invention, the aqueous medium may comprise at least 0.05% (meth-) acrylonitrile, preferably at least 0.1 % (meth-) acrylonitrile, more preferably at least 0.5% (meth-) acrylonitrile, most preferably at least 1.0% (meth-) acrylonitrile (w/w). Throughout the bioconversion (incubation) the concentration of (meth-) acrylonitrile may be kept at a concentration of about 0.5% to 1.5%, preferably about 1.0% (meth-) acrylonitrile by continuous feeding of (meth-) acrylonitrile.

Alternatively, the concentration of (meth-) acrylonitrile in the aqueous medium may be 5% or 6% at the start of the incubation and might be kept at that concentration or no further (meth-) acrylonitrile may be added during bioconversion (incubation).

It is preferred, that the concentration of (meth-) acrylonitrile during the bioconversion should not exceed 6 % by wt. and may for example be in the range from 0.1 % by wt. to 6 % by wt., preferably from 0.2 % by wt. to 5 % by wt., more preferably from 0.3 % by wt. to 4 % by wt., even more preferably from 0.5 % by wt. to 3 % by wt., still more preferably from 0.8 % by wt. to 2 % by wt. and most preferably from 1 % by wt. to 1.5 % by wt., relating to the total of all components of the aqueous mixture. It is possible that the concentration may vary over time during the bioconversion reaction. In order to obtain more concentrated solutions of ammonium (meth-) acrylate the total amount of (meth-) acrylonitrile should not be added all at once but it should be added stepwise or even continuously keeping the abovementioned concentration limits in mind.

The concentration of ammonium (meth-) acrylate in the obtained solution (aqueous medium) is in the range from 10% to 80%, preferably in the range from 20% to 70%, more preferably in the range from 30% to 65%, even more preferably in the range from 40% to 60%, most preferably in the range from 45% to 55% by weight, based on the complete weight of the reaction solution. The reaction should be carried out in such a manner that the final concentration of (meth-) acrylonitrile in the final ammonium (meth- ) acrylate solution obtained does not exceed 0.1 % by weight relating to the total of all components of the aqueous solution.

Typical reaction times may be from 2 h to 20 h, in particular 4 h to 12 h, for example 6 h to 10 h. After completion of the addition of (meth-) acrylonitrile, the reactor contents are allowed to further circulate for some time to complete the reaction, for example for 1 hour to 3 hours. The remaining contents of (meth-) acrylonitrile should preferably be less than 100 ppm, based on the complete weight of the reaction solution. Further preferred bioconversion times (incubation times) of the aqueous medium may be at least 5h, at least 10h or at least 12h. Preferably the bioconversion (incubation) time is at least 18h, for example about 24h or about 30h. More preferably the bioconversion (incubation) time is about 36h or about 42h. Most preferably, the bioconversion (incubation) time is about 48h. Depending on the nitrilase used and the reaction rate of said nitrilase, the bioconversion (incubation) time may also exceed 48h.

The present invention further relates to aqueous ammonium (meth-) acrylate solutions obtainable or being obtained by any one of the methods described and provided herein. An aqueous ammonium (meth-) acrylate solution, in particular an aqueous ammonium (meth-) acrylate solution obtainable or being obtained by any one of the methods described herein, may have a concentration of ammonium (meth-) acrylate at the end of the bioconversion of at least 10% (w/w), at least 15% (w/w), at least 20% (w/w), at least 25% (w/w), at least 30% (w/w), at least 35% (w/w), preferably at least 40% (w/w), at least 45% (w/w), more preferably at least 50% (w/w), more preferably at least 51 % (w/w), more preferably at least 52% (w/w), more preferably at least 53% (w/w), even more preferably at least 54% (w/w), most preferably at least 55% (w/w) by weight of the ammonium (meth-) acrylate monomers in the aqueous medium.

In any one of the aqueous ammonium (meth-) acrylate solutions, the ammonium (meth-) acrylate content concentration may be determined using HPLC.

Bioconversion unit

The hydrolysis of (meth-) acrylonitrile to ammonium (meth-) acrylate by means of a biocatalyst is performed in a suitable bioconversion unit (also called reactor). Suitable reactors for performing the bioconversion are known to the skilled artisan. Examples comprise vessels of any shape, for example cylindrical or spherical vessels, or tube reactors. Such reactors comprise particularly a pumping circuit comprising a heat- exchanger.

The bioconversion unit comprises a reaction vessel. The volume of the reaction vessel is not specifically limited and may range from 10 m ³ to 150 m ³ , for example it may be from about 20 m ³ to about 120 m ³ , suitably from about 20 m ³ to about 100 m ³ , preferably about 20 m ³ to 50 m ³ . Preferably, the reaction vessel should be double walled and should be horizontal. Such a construction avoids installing a pit for the collection of any leakage thereby ensuring an easier and quicker relocation of the reaction unit.

The bioconversion unit furthermore comprises means for controlling the temperature of the contents of the vessel. The hydrolysis of (meth-) acrylonitrile to ammonium (meth-) acrylate is an exothermal reaction and therefore heat generated in course of the reaction should be removed in order to maintain an optimum temperature for bioconversion. The bioconversion unit furthermore usually comprises means for measurement and control, for example means for controlling the temperature or for controlling the pressure in the vessel.

For temperature control, the preferred bioconversion unit comprises an external temperature control circuit comprising a pump which pumps the aqueous reactor contents from the storage vessel through a heat exchanger and back into the storage vessel, preferably via an injection nozzle.

In one embodiment, a separate, relocatable temperature control unit is used comprising pump and heat exchanger and which is connected with the bioconversion unit by pipes or flexible tubes. In a preferred embodiment, the temperature control circuit is integrated into the bioconversion unit. It may -for example- be located at one end of the unit next to the reaction vessel.

It has been found, that the external temperature control circuit described above may also be used as means for mixing. The stream of the aqueous reaction mixture which passes through the temperature control circuit and which is injected back into the reaction vessel causes a circulation of the aqueous reaction mixture within the reaction vessel which is sufficient to mix the aqueous reaction mixture.

Preferably, no stirrer is used for the mobile bioconversion unit (i.e. reaction vessel). A stirrer is an additional mechanical device, which increases the technical complexity. When using the external temperature control cycle for mixing instead of a stirrer, the technical complexity can be reduced while still sufficient mixing during bioconversion can be ensured. Advantageously, without a stirrer a transportation step is easier, since no stirrer as additional technical component has to be removed before transportation of the mobile bioconversion unit. Further, a bioconversion unit without a stirrer offers more flexibility in form, shape, mechanical stability requirements and size for the

bioconversion unit. In particular, a horizontal set-up for the relocatable bioconversion unit can be realized easier without a stirrer and with mixing just via the external temperature control cycle.

Having no stirrer in the bioconversion reactor offers the advantage of reduced engineering costs and less effort in process control. A further advantage is that with having difficult construction requirements for constructing a bio ammonium (meth-) acrylate production unit, with the present invention the bioconversion manufacturing unit can be built much simpler, with less effort and leads to a less complex

bioconversion reactor construction. Based on the state of the art, if bioconversion reactors are not vertical designed but horizontal, this would require more stirrer.

Advantageously, with the present invention and mixing by the external cooling circuit, stirrers are no longer needed. Unexpectedly, the external cooling circuit is sufficient also with horizontal and/or vertical reactors to obtain a satisfactory mixture of the reaction composition / reaction mixture. It is possible to do mixing without a stirrer when producing ammonium (meth-) acrylate from (meth-) acrylonitrile by a biocatalyst method. Additionally, the reduced equipment complexity offers the possibility to conduct the bioconversion in a relocatable unit.

Adding (meth-) acrylonitrile to the contents of the bioconversion unit may be performed in various ways. It may be added into the reaction vessel or it may be added into the temperature control circuit, for example after the pump and before the heat exchanger or after the heat exchanger. Injecting (meth-) acrylonitrile into the temperature control circuit ensures good mixing of the reaction mixture with freshly added (meth-) acrylonitrile. Preferably, (meth-) acrylonitrile is added between pump and heat exchanger.

The amount of reaction mixture cycled per hour through the temperature control circuit is chosen such that sufficient mixing to the contents of the reactor as well as sufficient temperature control is achieved. In one embodiment, the amount of reaction mixture cycled per hour through the temperature control circuit may be from 100 % to 1000 % of the total volume of the reaction mixture in the bioconversion unit, in particular from 200 % to 1000 % and for example from 500% to 800%. Further possible is that the amount of reaction mixture cycled per hour through the temperature control circuit is from 100 % to 10000 %, preferably from 100 % to 5000 %.

Off-gases of the bioconversion unit may comprise acrylonitrile, acrylic acid and acrylamide. If necessary, according to the applicable rules such off-gases may be treated in a manner known in the art. For example, it may be possible to combust the off-gases.

In one embodiment, all off-gases containing acrylonitrile, acrylic acid and acrylamide may be washed in a scrubber. The scrubber vessel may have a volume of 1 m ³ to 100 m ³ , preferably a volume of 5 m ³ to 100 m ³ , more preferably a volume of 10 m ³ to 100 m ³ . It may be for example an ISOtank or relocatable storage vessel, preferably a double walled vessel. The scrubber water may preferably be collected in a tank and it may be re-used for next bio-conversion batch.

In another embodiment of the invention, for temperature control an external temperature control circuit, for example a cooling circuit is used, which comprises a pump which pumps the monomer from the storage vessel through a heat exchanger and back into the storage vessel.

The temperature control circuit may be a separate, relocatable temperature control unit comprising pump and heat exchanger and which is connected with the storage vessel by pipes or flexible tubes. Modular, relocatable units

In one embodiment of the invention, aqueous solutions of bio ammonium (meth-) acrylate for use in the method according to the present invention may be manufactured at a fixed chemical plant, and may be shipped to another location for further

processing. However, in another preferred embodiment of the present invention the manufacture of bio ammonium (meth-) acrylate may be performed in a modular, relocatable plant. Further preferred is for example a relocatable bioconversion unit, which can be combined with installations and/or units of a fixed chemical plant. Such combination of an existing plant with a modular, relocatable bioconversion unit offers flexibility in building a production line based on case specific needs. Such production line at a certain plant can be adjusted easily in case the production requirements change. The existing plant for example may be a fixed polymerization plant for homopolymers of (meth-) acrylic acid and/or copolymers of for example (meth-) acrylic acid and acrylamide. So, the combination of a relocatable bioconversion unit offers the possibility of combining the manufacturing of bio ammonium (meth-) acrylate with units for further processing the ammonium (meth-) acrylate obtained from a relocatable bioconversion unit.

Particularly, in the light of the present invention it is possible to reduce the food print and complexity of the bio ammonium (meth-) acrylate manufacturing site. Having a bioconversion reactor without a stirrer / no agitating element reduces the engineering and processing control significantly. Further, no drying, cleaning and/or separation (e.g. centrifugation) facility for ammonium (meth-) acrylate is needed. The obtained aqueous ammonium (meth-) acrylate solution can be used directly for further processing.

Therefore, in a preferred embodiment of the invention, the bioconversion unit / bioconversion reactor is a relocatable bioconversion unit. In one embodiment, the relocatable bioconversion unit is similar to the storage unit for (meth-) acrylonitrile, which also may be relocatable. Therefore, it is possible to using largely the same equipment for storing the (meth-) acrylonitrile and for the bioconversion step. This contributes to an economic process for manufacturing aqueous ammonium (meth-) acrylate solutions.

Due to the flexibility of having a relocatable bioconversion unit / bioconversion reactor without a mechanical stirrer / agitating device and without installations for cleaning and/or drying, it is possible to conduct the method for production of an aqueous ammonium (meth-) acrylate solution at the location where the further processing for example to a polymer takes place.

Manufacturing bio ammonium (meth-) acrylate directly at the site of further processing the ammonium (meth-) acrylate to for example polyacrylic acids saves significant transport costs. (Meth-) acrylonitrile is a liquid and may be transported as pure compound to the site of further processing. The molecular weight of ammonium (meth-) acrylate is about 30 to 40 % higher than that of (meth-) acrylonitrile and ammonium (meth-) acrylate is typically provided as about 50 % aqueous solution. So, for a 50 % aqueous solution of ammonium (meth-) acrylate the mass to be transported is about 2.5-fold as much as compared to transporting pure (meth-) acrylonitrile. Transporting pure, solid acrylic acid means transporting only about 30 to 40 % more mass as compared to transporting pure (meth-) acrylonitrile, however, additional equipment for handling and dissolving the solid (meth-) acrylic acid is necessary at the location where further processing takes place.

Furthermore, (meth-) acrylic acid is caustic and it is therefore an advantage to reduce the transportation distance or amount of (meth-) acrylic acid to be transported in order to reduce the risk of accidents when transporting acrylic acid. A bioconversion according to the present invention in a relocatable bioconversion unit enables that advantage.

(Meth-) acrylonitrile for bio-catalysis may be stored in one or more than one relocatable storage units. The storage unit comprises a storage vessel. The volume of the storage vessel is not specifically limited and may range from 50 m ³ to 150 m ³ , for example it may be about 100 m ³ . Preferably, the storage vessel should be single walled or double walled and should be horizontal. Such a construction avoids installing a pit for the collection of any leakage thereby ensuring an easier and quicker relocation of the storage unit. Single walled or double-walled vessels may be placed on every good bearing soil. The storage unit furthermore comprises means for charging and discharging the vessel, means for controlling the pressure in the vessel, for example a valve for settling low-pressure or overpressure,

and means for controlling the temperature of the (meth-) acrylonitrile which preferably should not exceed 25°C. It furthermore may comprise means for measurement and control to the extent necessary.

Examples of relocatable storage units comprise relocatable cuboid, storage tanks, preferably double-walled tanks or single walled tanks. Further, any considerable form, shape and size of container is suitable and applicable for the storage and/or provision of acrylonitrile in the sense of the present invention. Particularly, standard iso-tanks are applicable for the storage and/or provision of (meth-) acrylonitrile. Other examples comprise tank containers having a cuboid frame, preferably a frame according to the ISO 668 norm mentioned above and one or more storage vessels mounted into the frame. Such normed tank containers may be stacked and transported on trucks, railcars or ships in the same manner closed intermodal containers.

Several different relocatable units may be bundled together to have a relocatable plant. Each relocatable unit may have certain functions. Examples of such relocatable units comprise units for storing and optionally cooling monomers and/or other raw materials, hydrolyzing (meth-) acrylonitrile, mixing monomers, further processing the ammonium (meth-) acrylate to for example an aqueous solution of a copolymer of (meth-) acrylic acid and acrylamide. For performing different processes, individual units may be connected with each other in a suitable manner thereby obtaining a production line. Also bundling a relocatable bioconversion unit with non-relocatable units is possible.

“Relocatable unit” means that the unit is transportable basically as a whole and that is it not necessary to disassemble the entire unit into individual parts for transport.

Transport may happen on trucks, railcars or ships.

In one embodiment, such modular, relocatable units are containerized units which may be transported in the same manner as closed intermodal containers for example on trucks, railcars or ships. Intermodal containers are large standardized (according to ISO 668) shipping containers, in particular designed and built for intermodal freight transport. Such containers are also known as ISO containers. Such ISO containers may have external dimensions of a height of ~ 2.59 m, a width of ~ 2.44 m and a length of ~ 6.05 m. Larger ISO containers have external dimensions of a height of ~ 2.59 m, a width of ~ 2.44 m and a length of -12.19 m.

In another embodiment, the relocatable units are combined, thereby obtaining modular production plants for performing different processes according to the present invention. Such a modular construction using relocatable units provides the advantage, that the plants may be easily relocated if aqueous ammonium (meth-) acrylate solutions are no longer needed at one location but at another location.

At the site of manufacturing the aqueous ammonium (meth-) acrylate solution, at the site of further processing the ammonium (meth-) acrylate to obtain subsequent further products (e.g. poly (meth-) acrylate) and/or at the site of applying / using for example aqueous solutions of (meth-) acrylic acid / acrylamide copolymers (e.g. for oilfield or mining applications) different relocatable units according to the present invention may be used and combined, for example:

o a relocatable storage unit for (meth-) acrylonitrile,

o a relocatable bioconversion unit for hydrolyzing (meth-) acrylonitrile in water in the presence of a biocatalyst capable of converting (meth-) acrylonitrile to ammonium (meth-) acrylate,

o a relocatable unit for removing the biocatalyst from an aqueous ammonium

(meth-) acrylate solution,

o a relocatable storage unit for an aqueous ammonium (meth-) acrylate solution, o relocatable units for further processing ammonium (meth-) acrylate with other water-soluble, monoethylenically unsaturated monomers different from (meth-) acrylic acid,

o a relocatable unit for polymerization to obtain aqueous solutions of (meth-) acrylic acid homo- or copolymers, and/or

o a relocatable unit for subsequent applications.

Further processing of ammonium (meth-) acrylate

After having obtained the aqueous ammonium (meth-) acrylate solution further processing is possible. Further processing steps are mixing the aqueous ammonium (meth-) acrylate solution with other monomers in order to prepare a monomer solution which is suitable for a subsequent polymerization step to obtain homopolymers or copolymers deriving from ammonium (meth-) acrylate. Further processing also comprises processing the obtained ammonium (meth-) acrylate to other acrylic monomers or to produce acrylic acid or salts thereof (e.g. sodium acrylate) to be used for instance as a polymerizable monomer. Due to the benefits of a bioconversion reaction (particularly, without a stirrer or without mechanical agitation device) it is in particular possible to use the bioconversion reactor as make-up and/or storage device for a monomer solution, which could subsequently be used for a polymerization reaction. The different further processing steps may be performed at different locations. For example, each further processing step may be performed at a different location. Alternatively, all or some of the further processing steps may be performed at the same location, in particular at the location of use of either the aqueous ammonium (meth-) acrylate solution or at the location of use of the resulting polymer solution. If performed at the same location, it is possible to connect the different modular units / modular reactors with each other as needed to perform for example the different steps comprising the bioconversion of (meth-) acrylonitrile to ammonium (meth-) acrylate and subsequent preparation of a monomer solution and polymerization to obtain homo- or copolymers of (meth-) acrylic acid directly after another.

Biomass removal

After bioconversion, the reaction vessel comprises an aqueous solution of ammonium (meth-) acrylate, which still comprises the biocatalyst suspended therein. The biocatalyst preferably becomes removed completely, essentially completely, or partially before polymerization, however, removing the biocatalyst may not be absolutely necessary in every case. Whether it is necessary to remove the biocatalyst

substantially depends on two factors, namely whether remaining biocatalyst negatively affects polymerization and/or the properties of the polymer obtained and/or the biocatalyst negatively affects the application of the obtained polymer solution. In one embodiment, at least 75 %, preferably at least 90 % by weight of the biomass -relating to the total of the biomass present- should be removed.

The method for removing the biocatalyst is not specifically limited. Separation of the biocatalyst may take place by for example filtration or centrifugation. In other embodiments, active carbon may be used for separation purpose.

Procedurally, for removing the biocatalyst there are several options.

In one embodiment, the aqueous ammonium (meth-) acrylate solution comprising the biocatalyst is removed from the bioconversion unit, passed through a unit for removing the biocatalyst, and thereafter the aqueous ammonium (meth-) acrylate solution is filled into a suitable storage unit for ammonium (meth-) acrylate, for example a relocatable storage unit for ammonium (meth-) acrylate as described above.

In another embodiment, the aqueous ammonium (meth-) acrylate solution comprising the biocatalyst is removed from the bioconversion unit, passed through a unit for removing the biocatalyst and thereafter the aqueous ammonium (meth-) acrylate solution is filled directly into a monomer make-up unit for further processing, i.e. without intermediate storing in an ammonium (meth-) acrylate storage unit.

In another embodiment, the aqueous ammonium (meth-) acrylate solution comprising the biocatalyst is removed from the bioconversion unit and is filled directly, i.e. without removing the biocatalyst, into the monomer make-up unit. In said embodiment, the biocatalyst is still present in course of monomer make-up for further processing and is removed after preparing an aqueous monomer solution.

In another embodiment it is even possible that the biocatalyst is not removed from the aqueous monomer solution and the biocatalyst is present during further processing. This non-removal of the biocatalyst is of advantage, because the processing step of removing the biocatalyst can be avoided which therefore leads to less process steps and makes the overall process simpler.

In another embodiment, the aqueous ammonium (meth-) acrylate solution comprising the biocatalyst is removed from the bioconversion unit, passed through a unit for removing the biocatalyst and thereafter filled back into the bioconversion unit. In order to ensure complete discharge of the bioconversion unit before re-filling it, the unit for removing the biocatalyst should comprise a buffer vessel having a volume sufficient for absorbing the contents of the bioconversion unit. The above-mentioned methods for biocatalyst removal are for example applicable for partwise and/or complete removal of the biocatalyst. Further, it is preferred, that the completely or partly removed biocatalyst may be reused for a subsequent

bioconversion reaction.

In a preferred embodiment, the aqueous ammonium (meth-) acrylate solution does no longer comprise the biocatalyst. However, in another embodiment the ammonium (meth-) acrylate solution still comprises the biomass. In said embodiment, the biocatalyst may be removed after preparing an aqueous monomer solution for further processing in the same manner as described above or it may not be removed. Criteria for deciding in which cases it may not be necessary to remove the biocatalyst have already been mentioned above.

Provision of acrylamide

In the context of the present invention, acrylamide may be used as comonomer besides (meth-) acrylic acid. Basically, any kind of acrylamide may be used for the process according to the present invention, for example acrylamide obtained by catalytic oxidation of propene. It is also possible to use crude acrylamide, which has not been purified. In one embodiment of the invention acrylamide available by enzymatic hydrolysis of acrylonitrile may be used for carrying out the process according of the present invention (hereinafter also“bio acrylamide”). In a preferred embodiment of the present invention the manufacture of acrylamide by enzymatic hydrolysis of acrylonitrile is also performed in a modular / relocatable bioconversion unit. Suitable enzymes have been disclosed in the literature (e.g. WO 2005054456, WO 2005054489), and the publications describes also suitable conditions for carrying out the reaction. The manufacture of bio acrylamide may be carried out using stirred tank reactors or loop reactors, and in particular, the relocatable bioconversion unit described above may also be used. Manufacturing bio-acrylamide at the same location as manufacturing ammonium (meth-) acrylate also saves transport costs. Further beneficial is that for enzymatic production of acrylamide and ammonium (meth-) acrylate the same starting material, namely (meth-) acrylonitrile, can be used, which offers advantages regarding sourcing and transportation.

Aqueous monomer solution

In course of further processing, an aqueous monomer solution comprising at least water, ammonium (meth-) acrylate and optionally further water-soluble,

monoethylenically unsaturated monomers is prepared. Basically, the kind and amount of water-soluble, monoethylenically unsaturated comonomers to be used besides acrylic acid is not limited and depends on the desired properties and the desired use of the aqueous solutions of poly (meth-) acrylates to be manufactured. Typical monomers fall under the definitions of neutral comonomers, anionic comonomers, cationic comonomers and/or associative comonomers, which an artisan knows from the state of the art and is also applicable in the context of the present invention.

Examples of neutral comonomers are comprising hydroxyl and/or ether groups, for example hydroxyethyl(meth)acrylate, hydroxypropyl(meth)acrylate, allyl alcohol, hydroxyvinylethylether, hydroxyvinylpropylether, hydroxyvinylbutylether, polyethylene glycol (meth)acrylate, N-vinylformamide, N-vinylacetamide, N-vinylpyrrolidone or N- vinylcaprolactam, and vinyl esters, for example vinylformate or vinyl acetate. Examples of neutral comonomers also comprise acrylamide, methacrylamide, N- methyl(meth)acrylamide, N,N’-dimethyl(meth)acrylamide, N-methylol(meth)acrylamide. Preference is given to acrylamide, methacrylamide, N-vinylpyrrolidone.

Examples of anionic comonomers may be selected from water-soluble,

monoethylenically unsaturated monomers comprising at least one acidic group, or salts thereof. The acidic groups are preferably selected from the group of

-COOH, -SO3H and -PO3H2 or salts thereof. Preference is given to monomers comprising COOH groups and/or -SO3H groups or salts thereof. Suitable counterions include especially alkali metal ions such as Li ⁺ , Na ⁺ or K ⁺ , and also ammonium ions such as NH ₄ ⁺ or ammonium ions having organic radicals. Examples of ammonium ions having organic radicals include [NH(CH ₃ ) ₃ ] ⁺ , [NH ₂ (CH ₃ ) ₂ ] ⁺ , [NH ₃ (CH ₃ )] ⁺ , [NH(C ₂ H ₅ ) ₃ ] ⁺ , [NH ₂ (C ₂ H ₅ ) ₂ ] ⁺ , [NH ₃ (C ₂ H ₅ )] ⁺ , [NH ₃ (CH ₂ CH ₂ OH)] ⁺ , [H ₃ N-CH ₂ CH ₂ -NH ₃ ] ²⁺ or [H(H ₃ C) ₂ N- CH ₂ CH ₂ CH ₂ NH ₃ ] ²⁺ .

Examples of anionic comonomers comprising -COOH groups include crotonic acid, itaconic acid, maleic acid or fumaric acid or salts thereof. Examples of comonomers comprising -SO ₃ H groups or salts thereof include vinylsulfonic acid, allylsulfonic acid, 2- acrylamido-2-methylpropanesulfonic acid (ATBS), 2-methacrylamido-2- methylpropanesulfonic acid, 2-acrylamidobutanesulfonic acid, 3-acrylamido-3- methylbutanesulfonic acid or 2-acrylamido-2,4,4-trimethylpentanesulfonic acid.

Preference is given to 2-acrylamido-2-methylpropanesulfonic acid (ATBS) or salts thereof. Examples of monomers comprising -P03H ₂ groups or salts thereof include vinylphosphonic acid, allylphosphonic acid, N-(meth)acrylamidoalkylphosphonic acids or (meth)acryloyloxyalkylphosphonic acids, preferably vinylphosphonic acid.

Examples of cationic comonomers may be selected from water-soluble,

monoethylenically unsaturated monomers comprising cationic groups. Suitable cationic monomers include especially monomers having ammonium groups, especially ammonium derivatives of N-(co-aminoalkyl)(meth)acrylamides or co-aminoalkyl(meth)- acrylates such as 2-trimethylammonioethyl acrylate chloride H ₂ C=CH-CO- CH ₂ CH ₂ N ⁺ (CH ₃ )3 CI- (DMA3Q). Further examples have been mentioned in

WO 2015/158517 A1 page 8, lines 15 to 37. Preference is given to DMA3Q.

Associative monomers impart hydrophobically associating properties to polyacrylates and/or polyacrylamides. Associative monomers to be used in the context of this invention are water-soluble, monoethylenically unsaturated monomers having at least one hydrophilic group and at least one, preferably terminal, hydrophobic group.

Examples of associative monomers have been described for example in WO

2010/133527, WO 2012/069478, WO 2015/086468 or WO 2015/158517.

“Hydrophobically associating copolymers” are understood by a person skilled in the art to mean water-soluble copolymers which, as well as hydrophilic units (in a sufficient amount to assure water solubility), have hydrophobic groups in lateral or terminal positions. In aqueous solution, the hydrophobic groups can associate with one another. Because of this associative interaction, there is an increase in the viscosity of the aqueous polymer solution compared to a polymer of the same kind that merely does not have any associative groups.

Examples of suitable associative monomers comprise monomers having the general formula H ₂ C=C(R ¹ )-R ² -R ³ (I) wherein R ¹ is H or methyl, R ² is a linking hydrophilic group and R ³ is a terminal hydrophobic group. Further examples comprise having the general formula H ₂ C=C(R ¹ )-R ² -R ³ -R ⁴ (II) wherein R ¹ , R ² and R ³ are each as defined above, and R ⁴ is a hydrophilic group.

The linking hydrophilic R ² group may be a group comprising ethylene oxide units, for example a group comprising 5 to 80 ethylene oxide units, which is joined to the

H ₂ C=C(R ¹ )- group in a suitable manner, for example by means of a single bond or of a suitable linking group. In another embodiment, the hydrophilic linking group R ² may be a group comprising quaternary ammonium groups.

In one embodiment, the associative monomers are monomers of the general formula H ₂ C=C(R ¹ )-0-(CH ₂ CH ₂ 0)k-R ^3a (III) or H ₂ C=C(R ⁵ )-(C=0)-0-(CH ₂ CH ₂ 0) _k -R ^3a (IV), wherein R ¹ has the meaning defined above and k is a number from 10 to 80, for example, 20 to 40. R ^3a is an aliphatic and/or aromatic, straight-chain or branched hydrocarbyl radical having 8 to 40 carbon atoms, preferably 12 to 32 carbon atoms. Examples of such groups include n-octyl, n-decyl, n-dodecyl, n-tetradecyl, n-hexadecyl or n-octadecyl groups. In a further embodiment, the groups are aromatic groups, especially substituted phenyl radicals, especially distyrylphenyl groups and/or tristyrylphenyl groups.

In another embodiment, the associative monomers are monomers of the general formula H ₂ C=C(R ¹ )-0-(CH ₂ ) _n -0-(CH ₂ CH ₂ 0) _x -(CH ₂ -CH(R ⁵ )0) _y -(CH ₂ CH ₂ 0) _z H (V), wherein R ¹ is defined as above and the R ⁵ radicals are each independently selected from hydrocarbyl radicals comprising at least 2 carbon atoms, preferably from ethyl or propyl groups. In formula (V) n is a natural number from 2 to 6, for example 4, x is a number from 10 to 50, preferably from 12 to 40, and for example, from 20 to 30 and y is a number from 5 to 30, preferably 8 to 25. In formula (V), z is a number from 0 to 5, for example 1 to 4, i.e. the terminal block of ethylene oxide units is thus merely optionally present. In an embodiment of the invention, it is possible to use at least two monomers (V), wherein the R ¹ and R ⁵ radicals and indices n, x and y are each the same, but in one of the monomers z = 0 while z > 0 in the other, preferably 1 to 4.

In another embodiment, the associative monomers are cationic monomers. Examples of cationic associative monomers have been disclosed in WO 2015/158517 A1 , page 11 , line 20 to page 12, lines 14 to 42. In one embodiment, the cationic monomers having the general formula H ₂ C=C(R ¹ )-C(=0)0-(CH2)k-N ⁺ (CH3)(CH ₃ )(R ⁶ ) X- (VI) or H ₂ C=C(R ¹ )-C(=0)N(R ¹ )-(CH2)k-N ⁺ (CH3)(CH3)(R ⁶ ) X- (VII) may be used, wherein R ¹ has the meaning as defined above, k is 2 or 3, R ⁶ is a hydrocarbyl group, preferably an aliphatic hydrocarbyl group, having 8 to 18 carbon atoms, and X- is a negatively charged counterion, preferably Ch and/or Br.

Besides water-soluble monoethylenically unsaturated monomers, also water-soluble, ethylenically unsaturated monomers having more than one ethylenic group may be used as further comonomers. Monomers of this kind can be used in special cases in order to achieve easy crosslinking of the polymers. The amount thereof should generally not exceed 2% by weight, preferably 1 % by weight and especially 0.5% by weight, based on the sum total of all the monomers. More preferably, the monomers to be used in the present invention are only monoethylenically unsaturated monomers.

Besides the monomers, further additives and auxiliaries may be added to the aqueous monomer solution. Furthermore, before polymerization also suitable initiators for radical polymerization may be added. Examples of such further additives and auxiliaries comprise complexing agents, defoamers, surfactants, stabilizers, and bases or acids for adjusting the pH value. In certain embodiments of the invention, the pH-value of the aqueous monomer solution is adjusted to values from pH 5 to pH 7, for example pH 6 to pH 7. Preferably, it is also possible that the pH adjustment takes place in-situ, which means that via adjusting the acrylic acid content in the aqueous monomer solutions the pH can be adjusted. This adjustment can take place directly without addition of further pH adjusting additives during the reaction. This adjustment can also take place directly during the reaction by addition of for example a suitable buffer.

In one embodiment, the aqueous monomer solution comprises at least one stabilizer for the prevention of polymer degradation. Such stabilizers for the prevention of polymer degradation are what are called“free-radical scavengers”, i.e. compounds which can react with free radicals (for example free radicals formed by heat, light, redox processes), such that said radicals can no longer attack and hence degrade the polymer. Using such kind of stabilizers for the stabilization of aqueous solutions of polyacrylates and/or polyacrylamides basically is known in the art, as disclosed for example in WO 2015/158517 A1 , WO 2016/131940 A1 , or WO 2016/131941 A1.

The stabilizers may be selected from the group of non-polymerizable stabilizers and polymerizable stabilizers. Polymerizable stabilizers comprise a monoethylenically unsaturated group and become incorporated into the polymer chain in course of polymerization. Non-polymerizable stabilizers don’t comprise such monoethylenically unsaturated groups and are not incorporated into the polymer chain.

In one embodiment of the invention, stabilizers are non-polymerizable stabilizers selected from the group of sulfur compounds, steri cally hindered amines, N-oxides, nitroso compounds, aromatic hydroxyl compounds or ketones. Examples of sulfur compounds include thiourea, substituted thioureas such as N,N‘-dimethylthiourea, N,N‘-diethylthiourea, N,N‘-diphenylthiourea, thiocyanates, for example ammonium thiocyanate or potassium thiocyanate, tetramethylthiuram disulfide, and mercaptans such as 2-mercaptobenzothiazole or 2-mercaptobenzimidazole or salts thereof, for example the sodium salts, sodium dimethyldithiocarbamate, 2,2‘-dithiobis(benzo- thiazole), 4,4‘-thiobis(6-t-butyl-m-cresol). Further examples include dicyandiamide, guanidine, cyanamide, paramethoxyphenol, 2,6-di-t-butyl-4-methylphenol,

butylhydroxyanisole, 8-hydroxyquinoline, 2,5-di(t-amyl)-hydroquinone, 5-hydroxy- 1 ,4- naphthoquinone, 2,5-di(t-amyl)hydroquinone, dimedone, propyl 3, 4, 5-tri hydroxy- benzoate, ammonium N-nitrosophenylhydroxylamine, 4-hydroxy-2,2,6,6-tetramethy- oxylpiperidine, (N-(1 ,3-dimethylbutyl)-N'-phenyl-p-phenylenediamine and 1 , 2, 2,6,6- pentamethyl-4-piperidinol. Preference is given to sterically hindered amines such as

1.2.2.6.6-pentamethyl-4-piperidinol and sulfur compounds, preferably mercapto compounds, especially 2-mercaptobenzothiazole or 2-mercaptobenzimidazole or the respective salts thereof, for example the sodium salts, and particular preference is given to 2-mercaptobenzothiazole or salts thereof, for example the sodium salts. The amount of such non-polymerizable stabilizers -if present- may be from 0.1 % to 2.0 % by weight, relating to the total of all monomers in the aqueous monomer solution, preferably from 0.15 % to 1.0 % by weight and more preferably from 0.2 % to 0.75 % by weight.

In another embodiment of the invention, the stabilizers are polymerizable stabilizers substituted by a monoethylenically unsaturated group. With other words, such stabilizers are also monomers (C). Examples of stabilizers comprising

monoethylenically unsaturated groups comprise (meth)acrylic acid esters of 1 , 2,2,6, - pentamethyl-4-piperidinol or other monoethylenically unsaturated groups comprising

1.2.2.6.6-pentamethyl-piperidin-4-yl groups. Specific examples of suitable

polymerizable stabilizers are disclosed in WO 2015/024865 A1 , page 22, lines 9 to 19. In one embodiment of the invention, the stabilizer is a (meth)acrylic acid ester of 1 ,2,2,6,6-pentamethyl-4-piperidinol. The amount of polymerizable stabilizers -if present- may be from 0.01 to 2% by weight, based on the sum total of all the monomers in the aqueous monomer solution, preferably from 0.02 % to 1 % by weight, more preferably from 0.05 % to 0.5 % by weight.

In one embodiment, the aqueous monomer solution comprises at least one non- polymerizable surfactant. Examples of suitable surfactants including preferred amounts have been disclosed in WO 2015/158517 A1 , page 19, line, 23 to page 20, line 27. In the manufacture of hydrophobically associating polyacrylamides, the surfactants lead to a distinct improvement of the product properties. If present, such non-polymerizable surfactant may be used in an amount of 0.1 to 5% by weight, for example 0.5 to 3 % by weight based on the amount of all the monomers used.

As used herein, the term“water-soluble monomers” in the context of this invention means that the monomers are to be soluble in the aqueous monomer solution to be used for polymerization in the desired use concentration. It is thus not absolutely necessary that the monomers to be used are miscible with water without any gap; instead, it is sufficient if they meet the minimum requirement mentioned. It is to be noted that the presence of acrylamide and/or acrylic acid in the monomer solution might enhance the solubility of other monomers as compared to water only. In general, the solubility of the water-soluble monomers in water at room temperature should be at least 50 g/l, preferably at least 100 g/l.

Besides water, the aqueous monomer solution may also comprise additionally water- miscible organic solvents. However, as a rule the amount of water should be at least 70 % by wt. relating to the total of all solvents used, preferably at least 85 % by wt. and more preferably at least 95 % by wt.. In one embodiment, only water is used as solvent.

Depending on the chemical nature, the water-soluble, monoethylenically unsaturated monomers to be used may be provided as pure monomers or as aqueous solutions for further processing. It is also possible to provide a mixture of two or more water-soluble, monoethylenically unsaturated monomers, in aqueous solution or as pure monomers for further processing. Acrylic acid, acrylamide and other water-soluble,

monoethylenically unsaturated monomers such as 2-acrylamido-2-methylpropane- sulfonic acid (ATBS), or 2-trimethylammonioethyl acrylate chloride H ₂ C=CHCO- CH ₂ CH ₂ N+(CH ₃ )3 Ch (DMA3Q), or mixtures thereof preferably may be stored in suitable storage units. The monomers may be provided by road tankers, ISO tanks, or rail cars and pumped into relocatable storage units. The aqueous monomer solution for polymerization comprises water and 5 % to 45 % by weight, preferably 15 % to 45 % by weight of water-soluble, monoethylenically unsaturated monomers, relating to the total of all components of the aqueous monomer solution. The water-soluble, monoethylenically unsaturated monomers comprise at least ammonium (meth-) acrylate, which preferably is manufactured as described above.

In one embodiment of the invention, the monomer concentration is from 8 % by weight to 24.9 % by weight, preferably from 15 % by weight to 24.9 % by weight, for example from 20 to 24.9 % by weight, relating to the total of all components of the aqueous monomer solution. The monomer concentration may be selected by the skilled artisan according to his/her needs. For preparing the aqueous monomer solution, the water- soluble, monoethylenically unsaturated monomers to be used are mixed with each other. All monomers and optionally additives may be mixed with each other in a single step but it may also be possible to mix some monomers and add further monomers in a second step. Also, water for adjusting the concentration of the monomers may be added. Water eventually used for rinsing lines in course of transferring the monomer solution into the polymerization unit, needs to be taken into consideration when adjusting the concentration.

Preferably, the preparation of the aqueous monomer solution is performed in a relocatable monomer make-up unit. In one embodiment, the monomer make-up may be the unit which is similar to the bioconversion unit as described above. Using largely the same equipment for storing (meth-) acrylonitrile, for the bioconversion step and for further processing ammonium (meth-) acrylate contributes to an economic process for manufacturing aqueous ammonium (meth-) acrylate solutions. It is possible that the bioconversion unit may also be used for monomer make-up.

If the monomer make-up vessel is different to the bioconversion unit, it may be equipped with a stirrer for mixing the components of the aqueous monomer solution with each other. However, in the same manner as with the bioreactor, the external temperature control circuit may be used as means for mixing. The stream of the aqueous monomer mixture which passes through the temperature control circuit and which is injected back into the monomer make-up vessel causes a circulation of the aqueous reaction mixture within the reaction vessel which is sufficient to mix the aqueous reaction mixture.

Furthermore, the present invention relates to an (meth-) acrylic acid homopolymer or copolymer obtainable or being obtained by polymerizing the ammonium (meth-) acrylate of the aqueous solution as described herein. With this respect, in case of a homopolymer the term“polymerizing” refers to a homopolymerization reaction, while in case of a copolymer the term“polymerizing” refers to a copolymerization reaction. The homopolymerization or copolymerization may be performed using an aqueous ammonium (meth-) acrylate solution obtainable or being obtained by any one of the methods described herein. Preferably, an aqueous ammonium (meth-) acrylate solution may be used, from which the biocatalyst has been separated prior to the

polymerization.

As used herein, the term“poly (meth-) acrylates” and/or“poly (meth-) acrylic acid” as used herein means water-soluble homopolymers of (meth-) acrylic acid, or water- soluble copolymers comprising at least 10 %, preferably at least 20 %, and more preferably at least 30 % by weight of (meth-) acrylic acid and at least one additional water-soluble, monoethylenically unsaturated monomer different from (meth-) acrylic acid, wherein the amounts relate to the total amount of all monomers in the polymer. Copolymers are preferred. Copolymers may for example also comprise terpolymers of three different monomers.

(Meth-) acrylic acid homopolymers are, for example, used as surface coatings, adhesives, sealants, etc. In particular, use of (meth-) acrylic acid / acrylamide copolymers is made in tertiary oil recovery, which is also denoted as enhanced oil recovery. With this respect, in methods of tertiary oil recovery an aqueous solution of the polymer may be injected into the rock in order to promote oil displacement and thus increase the yield of crude oil. The present invention is therefore also related to an aqueous solution of any (meth-) acrylic acid / acrylamide copolymer described herein. As water for the aqueous solution seawater may be used.

Although the invention has been described with respect to specific embodiments and examples, it should be appreciated that other embodiments utilizing the concept of the present invention are possible without departing from the scope of the invention. The present invention is defined by the claimed elements, and any and all modifications, variations, or equivalents that fall within the true spirit and scope of the underlying principles.

FIGURES

The invention is further described by the figures. These are not intended to limit the scope of the invention

Brief description of the figure

Figure 1 : Schematic representation of a bio ammonium (meth-) acrylate reactor Figure 2: Schematic representation of a bio ammonium (meth-) acrylate reactor having eight single walled reaction vessel.

Detailed description of the figure

Figure 1 schematically represents an embodiment of the relocatable bioconversion unit with an integrated temperature control circuit. The bioconversion unit comprises a frame (10), a double-walled reaction vessel mounted into the frame comprising an outer wall (11 ) and an inner wall (12). Preferred volumes of the reaction vessel have already been mentioned. In other embodiments, the reaction vessel is self-supporting and there is no frame (10). The reaction vessel is filled with the reaction mixture. The bioconversion unit furthermore comprises an external temperature control circuit comprising at least a pump (13) and a temperature control unit (14). The reaction mixture is circulated by means of a pump (13) from the reaction vessel to the temperature control unit (14) and is injected back into the storage vessel, preferably via an injection nozzle (16). In the depicted embodiment, (meth-) acrylonitrile is injected into the temperature control circuit thereby ensuring good mixing (15). It may be added before or after the temperature control unit. Figure 1 shows an embodiment in which (meth-) acrylonitrile is added into the temperature control circuit between the pump and the heat exchanger. The stream of reaction mixture injected back into the reaction vessel causes a circulation of the reaction mixture in the reaction vessel which ensures sufficient mixing of the contents of the reaction mixture. No stirrer is installed.

Figure 2 schematically represents an embodiment of the relocatable bioconversion unit with an integrated temperature control circuit. The bioconversion unit comprises a frame (10), a reaction vessel mounted into the frame comprising a single wall (11 ). Preferred volumes of the reaction vessel have already been mentioned. In other embodiments, the reaction vessel is self-supporting and there is no frame (10). The reaction vessel is filled with the reaction mixture. The bioconversion unit, furthermore, comprises an external temperature control circuit comprising at least a pump (12) and a temperature control circuit (13). The reaction mixture is circulated by means of a pump (12) from the reaction vessel to the temperature control unit (13) and is injected back into the storage vessel, preferably via an injection nozzle (15). In the depicted embodiment, (meth-) acrylonitrile is injected into the temperature control circuit thereby ensuring good mixing (14). It may be added before or after the temperature control unit. No stirrer is installed.

EXAMPLES

The invention is further described by the following examples. The examples relate to practical and in some cases preferred embodiments of the invention that do not limit the scope of the invention.

Example 1 (comparative)

Copolymer of purified ammonium acrylate and acrylamide (NhUAA/AM):

Copolymer comprising 70.54 wt.% (75.0 mol%) of acrylamide and 29.46 wt.%

(25 mol%) of ammonium acrylate, stabilized with 0.25 wt.% Na-MBT (relating to polymer).

A 5 L beaker with magnetic stirrer, pH meter and thermometer was initially charged with 550.14 g of a 43% aqueous solution of ammonium acrylate (purified /

centrifugated), and then the following were added successively: 1800 g of distilled water, 1089.29 g of acrylamide (52% by weight in water, bio acrylamide) 10.5 g of a 5% aqueous solution of diethylenetriaminepentaacetic acid pentasodium salt, and 4 g of a 50% aqueous solution of the stabilizer sodium 2- mercaptobenzothiazole (Na-MBT).

After adjustment to pH 6.4 with a 20% by weight solution of sulfuric acid and addition of the rest of the water to attain the desired monomer concentration of 23% by weight (total amount of water 1824.37 g minus the amount of water already added, minus the amount of acid required), the monomer solution was adjusted to the initiation temperature of 0 °C. The solution was transferred to a Dewar vessel, the temperature sensor for the temperature recording was inserted, and the flask was purged with nitrogen for 45 minutes. The polymerization was initiated with 21 g of a 10% aqueous solution of the water-soluble azo initiator 2, 2 ^, -azobis(2-methylpropionamidine) dihydrochloride (Wako V-50; 10h t1/2 in water 56°C), 1.75 g of a 1 % t-butyl

hydroperoxide solution and 1 .05 g of a 1 % sodium sulfite solution. With the onset of the polymerization, the temperature rose to 60°C within about 50 min. A solid polymer gel was obtained.

After the polymerization, the gel was incubated overnight at 60 °C and the gel block was comminuted with the aid of a meat grinder. The comminuted aqueous

polyacrylamide gel was kept for further testing without drying.

Example 2 (inventive)

Copolymer of crude (unpurified) ammonium acrylate and acrylamide (cNI-UAA/AM):

Copolymer comprising 70.54 wt.% (75.0 mol%) of acrylamide and 29.46 wt.%

(25 mol %) of crude (unpurified / non-centrifugated) ammonium acrylate (ammonium acrylate is used directly after synthesis without a cleaning step), stabilized with 0.25 wt.% Na-MBT (relating to polymer) A 1 L screw glass bottle with magnetic stirrer, pH meter and thermometer was initially charged with 62.87 g of a 43% aqueous solution of crude ammonium acrylate, and then the following were added successively: 200 g of distilled water, 124.49 g of acrylamide (52% by weight in water, bio acrylamide) 1.2 g of a 5% aqueous solution of diethylenetriaminepentaacetic acid pentasodium salt, and 0.46 g of a 50% aqueous solution of the stabilizer sodium 2-mercaptobenzothiazole (Na-MBT).

After adjustment to pH 6.4 with a 10% by weight solution of sulfuric acid and addition of the rest of the water to attain the desired monomer concentration of 23 % by weight (total amount of water 208.50 g minus the amount of water already added, minus the amount of acid required), the monomer solution was adjusted to the initiation temperature of 0 °C. The solution was transferred to Dewar vessel, the temperature sensor for the temperature recording was inserted, and the flask was purged with nitrogen for 45 minutes. The polymerization was initiated with 2.40 g of a 10% aqueous solution of the water-soluble azo initiator 2, 2 ^, -azobis(2-methylpropionamidine) dihydrochloride (Wako V-50; 10h t1/2 in water 56 °C), 0.20 g of a 1 % t-BHP solution and 0.12 g of a 1 % sodium sulfite solution. With the onset of the polymerization, the temperature rose to 55 °C within about 120 min. A solid polymer gel was obtained.

After the polymerization, the gel was incubated 3 hours at 60 °C. The comminuted aqueous polyacrylamide gel was kept for further testing without drying.

Testing

Gel fraction / Solid content

A 5000 ppm polymer solution in pH 7 buffer is diluted to 1000 ppm with pH 7 buffer. The gel fraction is given as ml. of gel residue on the sieve when 250 g 1000 ppm polymer solution are filtered over 200 pm sieve and consequently washed with 2 I of tab water.

Viscosity of the polymers in aqueous solution

Measurements were performed in“pH 7 buffer”: For 10 I of pH 7 buffer fully dissolve 583.3 ± 0.1 g sodium chloride, 161.3 ± 0.1 g disodium hydrogenphosphate · 12 H ₂ 0 and 7.80 ± 0.01 g sodium dihydrogenphosphate · 2 H ₂ 0 in 10 I dist. or deionized water. A 5000 ppm polymer solution was obtained by dissolving the appropriate amount of aqueous polymer gel in pH 7 buffer until being fully dissolved. Viscosity measurements were performed at a Brookfield RS rheometer with single gap geometry.

Filtration ratio

Determination of MPFR (Millipore Filtration Ratio)

The filterability of the polymer solutions was characterized using the MPFR value (Millipore filtration ratio). The MPFR value characterizes the deviation of a polymer solution from ideal filtration characteristics, i.e. when there is no reduction of the filtration rate with increasing filtration. Such a reduction of the filtration rate may result from the blockage of the filter in course of filtration.

To determine the MPFR values, about 200 g of the relevant polyacrylamide solution having a concentration of 1000 ppm were filtered through a polycarbonate filter have a pore size of 5 pm at a pressure of 2 bar and the amount of filtrate was recorded as a function of time.

The MPFR value was calculated by the following formula

MPFR - (tl 80 g - tl 60 g) / (teo g - t60 g) .

T _{x g} is the time at which the amount solution specified passed the filter, i.e. tiso _g is the time at which 180 g of the polyacrylamide solution passed the filter. According to API RP 63 (“Recommended Practices for Evaluation of Polymers Used in Enhanced Oil Recovery Operations”, American Petroleum Institute), values of less than 1 .3 are acceptable.

Long-term storage

100 g of the gel was sealed under vacuum in a plastic bag and stored at 60 °C for one week. Subsequently, the gel was cooled tor room temperature and used for further testing.

Results

Table 1 :

¹⁾ @5000 ppm; pH=7 buffer, rt; 100 s ¹

²⁾ @1000 ppm; pH=7 buffer Conclusion:

From table 1 it becomes obvious that the polymer of the inventive example shows similar properties and performance as the polymer of the comparative example.

Unexpectedly, it is possible to produce a polymer, a copolymer of acrylamide and ammonium (meth-) acrylate, wherein the ammonium (meth-) acrylate is obtained in form of an aqueous ammonium (meth-) acrylate solution from the process of the present invention. From the MPFR value is become clear that the inventive polymer and the comparative polymer show similar properties. Both MPFR values are below 1.3 and with that in the acceptable range. Consequently, it is a surprise that with the process of the present invention for examples aqueous ammonium (meth-) acrylate solutions can be produced, which are suitable for further processing to polymers without a cleaning and/or drying step. Surprisingly, the resulting polymers of the present invention do not degrade during storage for one week at 60°C