TECHNICAL FIELD

[1] The present invention relates to a process for purifying carbon blacks, and more specifically makes use of supercritical fluid extraction (SFE), particularly with an extraction agent comprising carbon dioxide in a supercritical state, for producing carbon blacks that have a reduced content of oxy-polycyclic aromatic hydrocarbons and optionally other polycyclic aromatic hydrocarbon impurities. The invention further relates to purified carbon blacks obtainable by this process, and applications and uses of such purified carbon blacks.

TECHNICAL BACKGROUND

[2] Carbon blacks are widely employed in industry as an additive for various different applications, for example as a coloring agent or pigment, reinforcing filler or conductive agent in the manufacture of paints, coatings, inks, electrodes or plastic or rubber articles. Depending on the respective application, carbon blacks with different properties are required, which can be controlled by the carbon black production process and possible aftertreatment. Carbon blacks are produced by controlled thermal or thermal-oxidative decomposition of hydrocarbon precursors such as oils, natural gas or acetylene. Established carbon black production processes include the furnace black process, the gas black process, originally developed by Degussa, the channel black process, the lamp black process, the acetylene process or the thermal black process.

[3] Depending on the carbon black production process, used hydrocarbon precursor materials and process conditions, impurities such as metals, sulfur and organic compounds can contaminate the obtained carbon blacks. Such impurities, particularly when present in relatively high amounts, may adversely affect the carbon black performance and therefore be undesirable in certain applications. [4] Carbon blacks can in particular contain as impurities organic compounds that have a polycyclic aromatic structure, which are commonly referred to as polycyclic aromatic hydrocarbons (PAHs). PAHs are believed to be harmful to the health and environment as for example discussed in Sudip K. Samanta, Om V. Singh and Rakesh K. Jain: “Polycyclic aromatic hydrocarbons: environmental pollution and bioremediation”, TRENDS in Biotechnology, Vol. 20, No. 6, Jun. 2002, pages 243-248. Therefore, the PAH content of carbon blacks is subject to increasingly demanding customer needs and official regulations for applications such as use in food or beverage contact situations, pharmaceuticals, cosmetics, or the manufacture of toys and articles for children. For instance, the American Food and Drug Administration (FDA) has limited the total PAH content of high purity furnace blacks in goods with food contact to 0.5 ppm (cf. U.S. Code of Federal Regulations (CFR) 21 Sec.178.3297), whereby the PAH content is defined as the sum of 22 PAH compounds.

[5] Similarly, oxygenated derivatives of PAH compounds may contaminate carbon blacks. Polycyclic aromatic hydrocarbon derivatives that consist not only of carbon and hydrogen, but contain in addition oxygen are commonly referred to as oxygenated PAHs or oxy-PAHs. Oxy-PAHs include for example polycyclic aromatic ketones, polycyclic aromatic quinones, hydroxylated PAHs, polycyclic aromatic carboxaldehydes, polycyclic aromatic carboxylic acids and anhydrides, and polycyclic aromatic lactones. Oxy-PAHs are for example frequently found in carbon blacks oxidized with certain oxidizing agents such as ozone as they may form during such an oxidative treatment of carbon blacks. Oxy-PAH compounds are likewise believed to be hazardous to health especially due to their ascribed mutagenicity (cf. e.g. A. Clerge, J. Le Goff, C. Lopez, J. Ledauphin, R. Delepee (2019): "Oxy-PAHs: occurrence in the environment and potential genotoxic/mutagenic risk assessment for human health", Critical Reviews in Toxicology, DOI:10.1080/10408444.2019.1605333). Therefore, there is a desire for reducing the amount of oxy-PAHs in carbon blacks. [6] Accordingly, it is an objective of the present invention to provide a process for effectively removing oxy-PAHs, and if possible also PAHs, from carbon blacks and to provide carbon blacks having a reduced content of such impurities, ideally without adversely affecting other properties of the carbon black and/or making use of harmful or costly substances in an economic and environmental-friendly manner.

SUMMARY OF INVENTION

[7] This objective and additional advantages as described herein have unexpectedly been achieved by providing a process as defined in appended independent claim 1.

[8] The present invention accordingly relates to a process for producing a purified carbon black with a reduced content of oxy-polycyclic aromatic hydrocarbons (oxy-PAHs). The process comprises:

(a) providing a carbon black comprising an initial content of oxy- polycyclic aromatic hydrocarbons of 1 ppm or more,

(b) treating the carbon black comprising an initial content of oxy- polycyclic aromatic hydrocarbons with an extraction agent comprising carbon dioxide in a supercritical state to extract at least a portion of the oxy-polycyclic aromatic hydrocarbons from the carbon black, and

(c) removing the extraction agent comprising the extracted oxy- polycyclic aromatic hydrocarbons from the carbon black to obtain a purified carbon black with a lower content of oxy-polycyclic aromatic hydrocarbons than the initial content of oxy-polycyclic aromatic hydrocarbons.

[9] The present invention is also drawn to a purified carbon black obtained by the process according to the present invention as disclosed above and described in more detail below.

[10] The present invention furthermore relates to the use of such purified carbon black as pigment, reinforcing filler or conductive agent, for example for the manufacture of plastic or rubber articles, paints, inks, coatings, electrodes or energy storage devices. [11] Moreover, the present invention is directed towards the use of supercritical carbon dioxide for removing oxy-polycyclic aromatic hydrocarbons from carbon black.

[12] The process of the present invention involving a treatment of carbon black with an extraction agent comprising carbon dioxide in a supercritical state provides several advantages. Thus, it is flexible and applicable to various kinds of carbon blacks, independent of their production process. The process of the invention enables effectively purifying carbon blacks and obtaining carbon blacks with a low oxy-PAH content and optionally PAH content, substantially without adversely affecting other properties of the carbon black or the use of purifying agents which are expensive, harmful or difficult to remove from the carbon black product. Use of an extraction agent in the supercritical state beneficially combines densities similar to those of a liquid with solute diffusivities and viscosities closer to those of a gas, which enables high mass transfer rates and rapid and efficient extraction of oxy-PAHs and PAHs from carbon blacks. Moreover, the solvent strength can be varied herein by a simple variation of the applied pressure and/or temperature or the addition of suitable modifiers. Furthermore, carbon dioxide has the benefit of being non-toxic, nonflammable and inexpensive. It has a critical temperature as low as 304.2 K (31 °C) in combination with a critical pressure of 72.8 atm (7,380 kPa). The extraction with an extraction agent comprising carbon dioxide can thus be carried out at relatively mild conditions thereby reducing the tendency of undesirable changes to the carbon black by the purification treatment. Furthermore, supercritical carbon dioxide can easily be separated from the carbon black for example via pressure release, which leads to vaporization of the carbon dioxide. Thus, no dedicated step of drying or solvent removal after the extraction is required.

[13] These and other optional features and advantages of the present invention will be described in more detail in the following description. DETAILED DESCRIPTION

[14] As used herein, the term "comprising" is understood to be open-ended and to not exclude the presence of additional undescribed or unrecited elements, materials, ingredients or method steps etc. The terms "including", "containing" and like terms are understood to be synonymous with "comprising". As used herein, the term "consisting of is understood to exclude the presence of any unspecified element, ingredient or method step etc.

[15] As used herein, the singular form of “a”, “an”, and “the” include plural referents unless the context clearly dictates otherwise.

[16] Unless indicated to the contrary, the numerical parameters and ranges set forth in the following specification and appended claims are approximations. Notwithstanding that the numerical ranges and parameters setting forth the broad scope of the invention are approximations, the numerical values set forth in the specific examples are reported as precisely as possible. Any numerical values, however, contain errors necessarily resulting from the standard deviation in their respective measurement.

[17] Also, it should be understood that any numerical range recited herein is intended to include all subranges subsumed therein. For example, a range of “1 to 10” is intended to include any and all sub-ranges between and including the recited minimum value of 1 and the recited maximum value of 10, that is, all subranges beginning with a minimum value equal to or greater than 1 and ending with a maximum value equal to or less than 10, and all subranges in between, e.g. 1 to 6.3, or 5.5 to 10, or 2.7 to 6.1.

[18] All parts, amounts, concentrations etc. referred to herein are by weight, unless specified otherwise.

[19] As mentioned above, the present invention relates to a process for producing a purified carbon black with a reduced content of oxy-polycyclic aromatic hydrocarbons. The process comprises (a) providing a carbon black comprising an initial content of oxy-polycyclic aromatic hydrocarbons of 1 ppm or more, (b) treating the carbon black comprising an initial content of oxy-polycyclic aromatic hydrocarbons with an extraction agent comprising carbon dioxide in a supercritical state to extract at least a portion of the oxy-polycyclic aromatic hydrocarbons from the carbon black, and (c) removing the extraction agent comprising the extracted oxy- polycyclic aromatic hydrocarbons from the carbon black to obtain a purified carbon black with a lower content of oxy-polycyclic aromatic hydrocarbons than the initial content of oxy-polycyclic aromatic hydrocarbons.

[20] The term “polycyclic aromatic hydrocarbons (PAHs)” as used herein refers to organic compounds having a skeleton with two or more, such as two to seven, fused aromatic rings, i.e. a polycyclic aromatic structure. Hydrocarbon groups such as alkyl groups can optionally be bound to the skeleton of fused aromatic rings. As used herein, “polycyclic aromatic hydrocarbons (PAHs)” are non-substituted compounds having such a polycyclic aromatic structure, that is respective compounds consisting of carbon and hydrogen atoms only. On the contrary, “oxy-polycyclic aromatic hydrocarbons”, also referred to shortly as “oxy-PAHs”, as used herein refer to oxygenated derivatives of PAHs that consist not only of carbon and hydrogen, but contain in addition oxygen. In other words, oxy-PAHs represent organic compounds, which have a skeleton with two or more, such as two to seven, fused aromatic rings and which consist of carbon, hydrogen and oxygen atoms. For instance, oxy-PAHs can be derived from unsubstituted PAHs by substituting one or more hydrogen atom(s) by an oxygen-containing functional group, such as a carboxyl, aldo, hydroxyl or keto group. Oxy-PAHs include for example polycyclic aromatic ketones, polycyclic aromatic quinones, hydroxylated PAHs, polycyclic aromatic carboxaldehydes, polycyclic aromatic carboxylic acids and anhydrides, and polycyclic aromatic lactones. According to the present invention, the oxy- PAHs may in particular include one or more keto group, that is the oxy- PAHs can be polycyclic aromatic ketones.

[21] For the purpose of the present invention, the content of oxy-polycyclic aromatic hydrocarbons (oxy-PAHs) or of polycyclic aromatic hydrocarbons (PAHs) of a carbon black can more specifically refer to the content of one or more than one specific (group(s) of) oxy-PAH compounds or PAH compounds, such as 9,10-phenantrenedione, the oxy-PAH6 or the PAH22 group, as defined infra. Accordingly, a content of oxy-polycyclic aromatic hydrocarbons of a carbon black indicated herein can in particular mean a content of the compounds of the oxy-PAH6 group (also referred to as oxy- PAH6 content) or a content of 9,10-phenantrenedione. Likewise, a content of polycyclic aromatic hydrocarbons (PAHs) of a carbon black indicated herein can in particular mean a content of the compounds of the PAH22 group (also referred to as PAH22 content).

[22] “PAH22” as used herein refers to the group of 22 PAH compounds as specified by the American Food and Drug Administration (FDA) in the U.S. Code of Federal Regulations (CFR) 21 Sec.178.3297 and the method entitled “Determination of PAH content of Carbon Black”, dated July 8, 1994, as developed by Cabot Corp., mentioned therein: naphthalene (CAS no. 91-20-3), acenaphthylene (CAS no. 208-96-8), acenaphthene (CAS no. 83-32-9), fluorene (CAS no. 86-73-7), phenanthrene (CAS no. 85-01-8), anthracene (CAS no. 120-12-7), fluoranthene (CAS no. 206-44-0), pyrene (CAS no. 129-00-0), benzo(g,h,i)fluoranthene (CAS no. 203-12-3), benz(a)anthracene (CAS no. 56-55-3), cyclopenta(c,d)pyrene (CAS no. 27208-37-3), chrysene (CAS no. 218-01-9), benzo(b)fluoranthene (CAS no. 205-99-2), benzo(k)fluoranthene (CAS no. 207-08-9), benzo(e)pyrene (CAS no. 192-97-2), benzo(a)pyrene (CAS no. 50-32-8), perylene (CAS no. 198-55-0), dibenzo(a,h)anthracene (CAS no. 53-70-3), benzo(g,h,i)perylene (CAS no. 191-24-2), indeno(1 ,2,3-cd)pyrene (CAS no. 193-39-5), anthanthrene (CAS no. 191-26-4), and coronene (CAS no. 191- 07-1 ). The PAH22 content is thus determined as the total amount of these 22 compounds based on the total weight of a carbon black sample. The PAH22 content can be determined by analyzing a toluene extract obtained by Soxhlet extraction of the carbon black sample using GC-MS utilizing deuterated forms of PAH22 compounds for calibration following the above- mentioned method entitled “Determination of PAH content of Carbon Black”, dated July 8, 1994 as described in the examples. [23] “Oxy-PAH6” as used herein refers to the group of the following six oxy-PAH compounds: 9,10-phenanthrendione (CAS no. 84-11-7), 6H- benzo[cd]pyren-6-one (CAS no. 3074-00-8), benzanthrone (CAS no. 82- 05-3), benzo[b]fluoren-11-one (CAS no. 3074-03-01), 9-fluorenone (CAS no. 486-25-9) and 4H-cyclopenta[def]phenanthren-4-one (CAS no. 5737- 13-3). Accordingly, the oxy-PAH6 content is determined as the sum of the amounts of these six compounds based on the total weight of a carbon black sample. The oxy-PAH6 content of a carbon black sample can be determined analogously to the determination of the PAH22 content by analyzing a toluene extract obtained by Soxhlet extraction of the carbon black sample by GC-MS utilizing deuterated forms of oxy-PAH6 compounds for calibration. Alternatively, the content of oxy-polycyclic aromatic hydrocarbons of a carbon black can be determined as a content of 9,10-phenantrenedione of the carbon black. The content of 9,10- phenantrenedione can be determined as set forth in the Examples.

[24] According to the present invention a carbon black comprising an initial content of oxy-polycyclic aromatic hydrocarbons of 1 ppm or more is provided as starting material to be purified. For the sake of clarity, as will be apparent to the skilled reader, “carbon black” is different from “soot” or “black carbon”. Soot or black carbon are used to designate generally unwanted carbonaceous by-products resulting from an incomplete combustion of carbon-containing materials, such as oil, fuel, diesel or gasoline, coal, paper or waste material. Soot and black carbon contain large quantities of organic and inorganic impurities typically containing less than 60% of elemental carbon, based on the total mass, and are composed of rather coarse particles having hardly a well-defined structure or order. On the contrary, carbon black is deliberately produced by incomplete combustion or thermal decomposition of gaseous or liquid hydrocarbons under controlled conditions, and typically has a higher carbon content such as 80 wt.% or more, based on the total mass, and is composed of particles, which have a well-defined structure and high degree of order including graphene-like arrangement of carbon atoms, and high surface area-to- volume ratio. [25] This initial carbon black provided as starting material to be purified in the process of the present invention can in principle be based on any process for the production of carbon black. Different industrial processes for the production of carbon blacks are available and include e.g. the furnace process, gas black process, acetylene black process, thermal black process or lamp black process, as for example described in J.-B. Donnet et aL, "Carbon Black: Science and Technology", 2 ^nd edition. The carbon black comprising an initial content of oxy-polycyclic aromatic hydrocarbons used in the practice of the present invention can accordingly for example comprise or be a furnace black, a thermal black, a lamp black, a channel black, a gas black, an acetylene black, a recycled black or a combination of any of the foregoing. Recycled blacks are carbon blacks obtained from end-of-use carbon black-containing products, such as waste tires, and obtainable by recycling processes, typically involving two steps, a pyrolysis step for the decomposition of organic components such as rubbers or plastics and a demineralization step for dissolving inorganic additives or impurities. A wide variety of carbon blacks with different properties that can be used in the present invention are commercially available from carbon black manufacturers such as for example Cabot Corporation, Mitsubishi Chemical Company, Tokai Carbon, Denka, Birla Carbon or Orion Engineered Carbons GmbH. Non-limiting examples thereof include carbon blacks marketed under the ECORAX®, PUREX®, CORAX®, PRINTEX®, AROSPERSE®, HIBLACK®, COLOUR BLACK, SPECIAL BLACK, or NEROX® brands by ORION Engineered Carbons GmbH.

[26] The carbon black used as starting material in the process of the present invention may have been subjected to an optional aftertreatment or not. Typically, the carbon black comprising an initial content of oxy-polycyclic aromatic hydrocarbons used in the practice of the present invention comprises a carbon black which has been subjected to an oxidative treatment. Carbon blacks that have been subjected to an oxidative treatment, also referred to as "oxidized carbon blacks", comprise oxygencontaining functional groups in particular at the surface of the carbon black particles. The oxygen-containing functional groups can be exemplified, but are not limited to, alcohol, quinone, carboxyl, phenol, lactol, lactone, anhydride, chinone, peroxidic, ether, and ketone groups. Oxidative treatment can for example be accomplished by treatment with oxidizing agents including oxygen gas, ozone, peroxides such as hydrogen peroxide, persulfates such as sodium and potassium persulfates, hypohalites such as sodium hypochlorite, and transition metal-containing oxidants such as permanganate salts, osmium tetroxide, chromium oxides, ceric ammonium nitrates; and mixtures thereof. In particular, the carbon black comprising an initial content of oxy-polycyclic aromatic hydrocarbons used in the practice of the present invention can be an ozone-oxidized carbon black. Oxidized carbon blacks typically have a notable oxygen content. For example, oxidized carbon blacks that can be used according to the present invention can have an oxygen content of 0.5 wt.% or more, such as 1 wt.% or more, or 2 wt.% or more, or 5 wt.% or more, or 10 wt.% or more, based on the total weight of the oxidized carbon black. Typically, the oxygen content does not exceed 20 wt.%, based on the total weight of the oxidized carbon black material. For example, the oxidized carbon black can contain from 0.5 wt.% to 20 wt.%, or from 1 wt.% to 15 wt.%, or from 2 wt.% to 10 wt.%, or from 5 wt.% to 15 wt.% of oxygen, based on the total weight of the oxidized carbon black material. An oxidized carbon black used as starting material according to the present invention may have an oxygen content in a range between any of the above-mentioned values.

[27] The carbon black to be purified in the process of the present invention has an initial oxy-PAH content of 1 ppm or more. For instance, the carbon black to be purified in the process of the present invention may have an initial oxy-PAH6 content of 1 ppm or more. The carbon black may for example have an initial content of oxy-polycyclic aromatic hydrocarbons, such as an initial oxy-PAH6 content, of 2 ppm or more, or 3 ppm or more, or 4 ppm or more, or 5 ppm or more, or 10 ppm or more, such as 20 ppm or more, or 30 ppm or more, or 40 ppm or more, or 50 ppm or more, or 80 ppm or more, or 100 ppm or more, or 150 ppm or more, or 200 ppm or more, or 250 ppm or more, or 300 ppm or more. The carbon black can for example have an initial oxy-PAH content, such as an initial oxy-PAH6 content, of 5,000 ppm or less, such as 2,000 ppm or less, or 1 ,000 ppm or less, or 800 ppm or less, or 600 ppm or less, or 500 ppm or less. The carbon black to be purified in the process of the present invention may have an initial oxy-PAH content, such as an initial oxy-PAH6 content, in a range between any of the recited values, such as in a range from 1 ppm to 1,000 ppm, or from 5 ppm to 500 ppm or a range from 10 ppm to 100 ppm. The carbon black to be purified in the process of the present invention may have an initial content of 9,10-phenantrenedione of 1 ppm or more, such as of 2 ppm or more, or 3 ppm or more, or 4 ppm or more, or 5 ppm or more, or 10 ppm or more, or 20 ppm or more, or 30 ppm or more, or 40 ppm or more, or 50 ppm or more. The carbon black can for example have an initial content of 9,10-phenantrenedione of 500 ppm or less, such as 300 ppm or less, or 100 ppm or less, or 80 ppm or less, or 60 ppm or less, or 50 ppm or less. The carbon black to be purified in the process of the present invention may have an initial content of 9,10-phenantrenedione in a range between any of the recited values, such as in a range from 1 ppm to 500 ppm, or from 2 ppm to 300 ppm, or from 5 ppm to 80 ppm.

[28] The carbon black provided for purification according to the process of the present invention can further have an initial content of polycyclic aromatic hydrocarbons (PAHs). The initial content of polycyclic aromatic hydrocarbons can vary significantly, depending on the type of carbon black employed and its production method. For example, the initial content of polycyclic aromatic hydrocarbons can vary from as low as a few ppm to 10,000 ppm or even more. For instance, the carbon black to be purified in the process of the present invention may have an initial content of polycyclic aromatic hydrocarbons of 10 ppm or more, or 20 ppm or more, or 50 ppm or more, such as 100 ppm or more, 250 ppm or more, 500 ppm or more, 800 ppm or more, or 1 ,000 ppm or more. The carbon black can have an initial content of polycyclic aromatic hydrocarbons of 10,000 ppm or less, such as 5,000 ppm or less, or 3,000 ppm or less, or 2,000 ppm or less, or 1 ,000 ppm or less, or 800 ppm or less, or 500 ppm or less, or 400 ppm or less, or 300 ppm or less, or 200 ppm or less, or 100 ppm or less. The carbon black to be purified in the process of the present invention may have an initial content of polycyclic aromatic hydrocarbons in a range between any of the recited values, such as in a range from 10 ppm to 10,000 ppm, or a range from 50 ppm to 5,000 ppm, or a range from 200 ppm to 800 ppm.

[29] For example, the carbon black to be purified in the process of the present invention may have an initial PAH22 content of 10 ppm or more, such as 20 ppm or more, or 30 ppm or more, or 50 ppm or more, or 80 ppm or more, or 100 ppm or more, or 250 ppm or more, or 500 ppm or more, or 800 ppm or more, or 1 ,000 ppm or more. The carbon black can have an initial PAH22 content of 10,000 ppm or less, such as 5,000 ppm or less, or 3,000 ppm or less, or 2,000 ppm or less, or 1 ,000 ppm or less, or 800 ppm or less, or 500 ppm or less, or 400 ppm or less, or 300 ppm or less, or 200 ppm or less, or 100 ppm or less, or 50 ppm or less. The carbon black to be purified in the process of the present invention may have an initial PAH22 content in a range between any of the recited values, such as in a range from 10 ppm to 10,000 ppm, or from 500 ppm to 3,000 ppm or a range from 10 ppm to 200 ppm.

[30] The carbon black can have any combination of the initial PAH content, such as PAH22 content, and initial oxy-PAH content, such as oxy-PAH6 or 9,10-phenantrenedione content specified above.

[31] The carbon black comprising an initial content of oxy-polycyclic aromatic hydrocarbons and optionally PAHs provided in step (a) of the process can furthermore be characterized by one or more than one or all of the following properties.

[32] Thus, the carbon black comprising an initial content of oxy-polycyclic aromatic hydrocarbons and optionally PAHs provided in step (a) of the process be characterized by its ash content. The carbon black can for example have an ash content of 20 wt.% or less, such as 15 wt.% or less, or 10 wt.% or less, or 5 wt.% or less, or 3 wt.% or less, or 1 wt.% or less, or 0.5 wt.% or less, or 0.1 wt.% or less, based on the total weight of the carbon black. The carbon black can for example have an ash content of 0.001 wt.% or more, such as 0.005 wt.% or more, or 0.01 wt.% or more, or 0.05 wt.% or more, or 0.1 wt.% or more, or 0.2 wt.% or more, or 0.3 wt.% or more, or 0.5 wt.% or more, or 1 wt.% or more, or 2 wt.% or more, or 3 wt.% or more, based on the total weight of the carbon black. The carbon black to be purified in the process of the present invention may have an ash content in a range between any of the recited values, such as in a range from 0.001 wt.% to 20 wt.%, or from 0.005 wt.% to 5 wt.%, or from 0.1 to 1 wt.%. The ash content of the carbon black can be determined according to ASTM D1506-15.

[33] Further, the carbon black comprising an initial content of oxy-polycyclic aromatic hydrocarbons and optionally PAHs can be characterized by a content of volatiles. The content of volatiles can be determined by heating to 950°C according to DIN 53552:1977. The carbon black can for example have a volatile content of 20 wt.% or less, such as 15 wt.% or less, or 10 wt.% or less, or 5 wt.% or less, or 3 wt.% or less, or 1 wt.% or less, based on the total weight of the carbon black. The carbon black can for example have a volatile content of 0.1 wt.% or more, such as 0.2 wt.% or more, or 0.3 wt.% or more, or 0.5 wt.% or more, or 1 wt.% or more, or 2 wt.% or more, or 3 wt.% or more, based on the total weight of the carbon black. The carbon black to be purified in the process of the present invention may have a volatile content in a range between any of the recited values, such as in a range from 0.1 wt.% to 20 wt.%, or from 0.2 wt.% to 15 wt.%, or from 1 to 10 wt.%.

[34] Moreover, the carbon black comprising an initial content of oxy-polycyclic aromatic hydrocarbons and optionally PAHs can be characterized by its moisture content. For example, the carbon black can have a moisture content of 15 wt.% or less, such as 10 wt.% or less, or 5 wt.% or less, or 3 wt.% or less, or 1 wt.% or less, based on the total weight of the carbon black. The carbon black can for example have a moisture content of 0.1 wt.% or more, such as 0.2 wt.% or more, or 0.3 wt.% or more, or 0.5 wt.% or more, or 1 wt.% or more, based on the total weight of the carbon black. The carbon black to be purified in the process of the present invention may have a moisture content in a range between any of the recited values, such as in a range from 0.1 wt.% to 15 wt.%, or from 0.2 wt.% to 10 wt.%, or from 0.3 to 3 wt.%. The moisture content of the carbon black can be determined according to ASTM D1509-18.

[35] The carbon black comprising an initial content of oxy-polycyclic aromatic hydrocarbons and optionally PAHs can further be characterized by its carbon content. For example, the carbon black can have a carbon content of 80 wt.% or more, such as 85 wt.% or more, or 90 wt.% or more, or 95 wt.% or more, or 97 wt.% or more, or 98 wt.% or more, based on the total weight of the carbon black. The carbon black can for example have a carbon content of up to 99.9 wt.%, such as 99.5 wt.% or less, or 99 wt.% or less, or 98 wt.% or less, or 97 wt.% or less, or 95 wt.% or less. The carbon black to be purified in the process of the present invention may have a carbon content in a range between any of the recited values, such as in a range from 80 wt.% to 99.9 wt.%, or from 80 wt.% to 97 wt.%, or from 85 to 95 wt.%. The carbon content can be determined by elemental analysis.

[36] The carbon black comprising an initial content of oxy-polycyclic aromatic hydrocarbons and optionally PAHs can further be characterized by a specific surface area. For example, the carbon black can have a BET surface area of 10 m ² /g or more, such as 20 m ² /g or more, or 30 m ² /g or more, or 50 m ² /g or more, or 80 m ² /g or more, or 100 m ² /g or more, or 150 m ² /g or more, or 200 m ² /g or more, or 300 m ² /g or more, or 500 m ² /g or more, or 1 ,000 m ² /g or more. The carbon black can for example have a BET surface area of 2,000 m ² /g or less, such as 1 ,500 m ² /g or less, or 1 ,000 m ² /g or less, or 800 m ² /g or less, or 500 m ² /g or less, or 300 m ² /g or less, or 200 m ² /g or less. The carbon black to be purified in the process of the present invention may have a BET surface area in a range between any of the recited values, such as in a range from 10 to 2,000 m ² /g, or from 30 to 500 m ² /g, or from 50 to 300 m ² /g. The BET surface area can be measured by nitrogen adsorption according to ASTM D6556-19a.

[37] In the process according to the present invention a single carbon black or a mixture of two or more different carbon blacks, which may each be as described above, can be used as carbon black material to be purified. [38] As set forth above, in the process according to the present invention, the provided carbon black with the initial content of oxy-polycyclic aromatic hydrocarbons and optionally PAHs is treated with an extraction agent to extract at least a portion of the oxy-polycyclic aromatic hydrocarbons and optionally at least a portion of the polycyclic aromatic hydrocarbons from the carbon black. Herein, the extraction agent comprises carbon dioxide in a supercritical state. “Supercritical state” means that the extraction agent is in the state of a supercritical fluid. A supercritical fluid is obtained at a temperature and pressure above the critical temperature and pressure (critical point), i.e. in the supercritical region of the respective phase diagram. The critical point represents the highest temperature and pressure at which the respective substance can exist as a gas and liquid in equilibrium. A supercritical fluid exhibits intermediate properties between that of a gas and of a liquid. Use of an extraction agent in the supercritical state can for example advantageously combine liquid-like densities with gas-like diffusivities and viscosities, which promotes high mass transfer rates and rapid and efficient extraction of oxy-PAHs and PAHs from the carbon black. Specifically, carbon dioxide has a relatively low critical temperature of 304.2 K (31 °C) and a relatively low critical pressure of about 74 bar (7,380 kPa). The extraction with an extraction agent comprising carbon dioxide can thus be carried out at relatively mild conditions thereby reducing the tendency of undesirable changes to the carbon black by the purification treatment. Furthermore, supercritical carbon dioxide can easily be separated from the carbon black for example via pressure release, which leads to vaporization of the carbon dioxide. Thus, no dedicated step of drying or solvent removal after the extraction is required. Additionally, carbon dioxide has the benefit of being non-toxic, nonflammable and inexpensive.

[39] The extraction agent used according to the present invention can comprise for example at least 50 wt.% carbon dioxide, such as at least 70 wt.% carbon dioxide, such as at least 80 wt.% carbon dioxide, or at least 90 wt.% carbon dioxide, or at least 95 wt.% carbon dioxide, or at least 99 wt.% carbon dioxide, or at least 99.5 wt.% carbon dioxide, based on the total weight of the extraction agent. In a preferred variant, the extraction agent can consist of supercritical carbon dioxide, i.e. be substantially free of any other constituent than carbon dioxide. “Substantially free” means that substances other than carbon dioxide are included in the extraction agent, if present at all, only as impurities in small amounts of generally not more than 0.2 wt.%, such as 0.1 wt.% or less, or 0.005 wt.% or less, based on the total weight of the extraction agent. Alternatively, the extraction agent can comprise one or more auxiliary agents in addition to carbon dioxide. Such auxiliary agents may for example be used in order to control or change the chemical and/or physical properties of the extraction agent such as the viscosity, polarity or solvent strength of the extraction agent. Useful auxiliary agents include for example, without being limited thereto, air, oxygen, nitrogen, methane, water, and organic solvents like methanol, toluene, and dichloromethane or a combination of any of the foregoing. The auxiliary agent(s) can be used in any amount in the extraction agent according to the respective needs. For example, the one or more auxiliary agents can be used in a total amount of 50 wt.% or less, such as 30 wt.% or less, 20 wt.% or less or 10 wt.% or less, or 5 wt.% or less, or 1 wt.% or less, or 0.5 wt.% or less, based on the total weight of the extraction agent. The amount of auxiliary agent within the extraction agent can also be varied over time during the treatment of the carbon black in step (b). Preferably, however, the extraction agent used in the practice of the present does not include any auxiliary agents.

[40] According to the process disclosed herein, the carbon black comprising an initial content of oxy-polycyclic aromatic hydrocarbons and optionally PAHs is treated with the extraction agent comprising carbon dioxide in a supercritical state to extract at least a portion of the oxy-polycyclic aromatic hydrocarbons and optionally at least a portion of the polycyclic aromatic hydrocarbons from the carbon black. The treatment with the extraction agent is accordingly carried out at conditions under which the extraction agent is in a supercritical state. The carbon black is therefore treated with the extraction agent at a temperature and a pressure above the critical temperature and above the critical pressure of the extraction agent, respectively. The critical temperature and critical pressure can be derived from a phase diagram of the respective extraction agent, corresponding to the temperature and pressure at the critical point. A treatment of the carbon black with carbon dioxide as extraction agent can for example be carried out at any temperature at or above the critical temperature of carbon dioxide (31 °C) and a pressure at or above the critical pressure of carbon dioxide (73.8 bar). According to the present invention, treating the carbon black with the extraction agent can for example be conducted at a temperature of 31 °C or more, or 50°C or more, or 75°C or more, such as 100°C or more, or 150°C or more, or 200°C or more, or 250°C or more. The treatment can for example be conducted at a temperature of 500°C or less, such as 400°C or less, or 350°C or less, or 300°C or less. Treating the carbon black with the extraction agent can be carried out at a temperature in a range between any of the recited values, such as at a temperature in a range from 75°C to 400°C, preferably from 100°C to 350°C, such as from 100°C to 300°C. Moreover, treating the carbon black with the extraction agent can for example be conducted at a pressure of 73.8 bar or more, such as 75 bar or more, or 100 bar or more, or 120 bar or more, or 150 bar or more, or 200 bar or more. The treatment can for example be carried out at a pressure or 700 bar or less, such as 500 bar or less, or 400 bar or less, or 300 bar or less, or 250 bar or less. Treating the carbon black with the extraction agent can be carried out at a pressure in a range between any of the recited values, such as at a pressure in a range from 75 bar to 700 bar, preferably from 100 bar to 500 bar, such as from 150 bar to 400 bar. For example, treating the carbon black with the extraction agent in the process according to the invention can be carried out at a temperature in a range from 75 to 350°C, preferably from 120 to 300°C, more preferably from 150 to 280°C, and a pressure in a range from 150 to 400 bar, preferably from 180 to 350 bar, more preferably from 200 to 320 bar.

[41] Treating of the carbon black with the extraction agent in the process of the present invention can comprise exposing the carbon black to a flow of the extraction agent. The average flow rate can vary widely, e.g. depending on the size of the reactor used and/or the amount of carbon black that is treated therein with the extraction agent. The average flow rate of the extraction agent can for example be 5 NL/h or more, such as 10 NL/h or more, or 20 NL/h or more, or 50 NL/h or more, or 100 NL/h or more, or 150 NL/h or more, or 200 NL/h or more, or 250 NL/h or more, or 500 NL/h or more, or 1,000 NL/h or more, or 5,000 NL/h or more, or 10,000 NL/h or more, or 50,000 NL/h or more, or 100,000 NL/h or more, or 500,000 NL/h or more, or 1 ,000,000 NL/h or more, or 5,000,000 NL/h or more. For example, the average flow rate of the extraction agent can be 20,000,000 NL/h or less, such as 10,000,000 NL/h or less, or 5,000,000 NL/h or less, or 1 ,000,000 NL/h or less, or 500,000 NL/h or less, or 100,000 NL/h or less, 50,000 NL/h or less, or 10,000 NL/h or less, or 5,000 NL/h or less, or 1 ,000 NL/h or less, or 500 NL/h or less, such as 400 NL/h or less, or 300 NL/h or less, or 250 NL/h or less, or 200 NL/h or less or 150 NL/h or less, or 100 NL/h or less. The average flow rate can be in a range between any of the recited values, such as in a range from 5 NL/h to 10,000,000 NL/h, or from 50 NL/h to 500,000 NL/h, or from 100 NL/h to 10,000 NL/h or from 150 NL/h to 300 NL/h, or from 200 NL/h to 250 NL/h. Typically in a reactor with a comparatively small volume of the extraction chamber as employed in the examples described infra, the average flow rate is in a range from 50 NL/h to 250 NL/h. The average flow rate of the extraction agent is calculated based on the total volume which the supplied amount of the extraction agent would have under standard conditions (101.325 kPa, 0°C) and the overall extraction time. The volume of extraction agent can be measured for example by a mass flow meter, for instance positioned downstream of the extraction chamber, which measures the amount of extraction agent in the gaseous state per unit time at a certain temperature and pressure, e.g. at room temperature and atmospheric pressure. Integration over time yields then the total volume of extraction agent. The measured total volume of extraction agent can then be converted to a total volume of extraction agent under standard conditions by using the ideal gas law. The total volume of extraction agent under standard conditions expressed in norm liters [NL] is divided by the overall extraction time to calculate the average flow rate under standard conditions. [42] The average flow rate of the extraction agent (in NL/h) per unit volume of the extraction chamber of the reactor (in L) can for example be 50 NL h' ¹ L' 1 or more, such as 100 NL h' ¹ L' ¹ or more, or 200 NL h' ¹ L' ¹ or more, or 500 NL h' ¹ L' ¹ or more, or 1 ,000 NL h' ¹ L' ¹ or more, or 2,000 NL h' ¹ L' ¹ or more, or 2,500 NL h' ¹ L' ¹ or more, or 3,000 NL h' ¹ L' ¹ or more. For example, the average flow rate of the extraction agent per unit volume of the extraction chamber of the reactor (in L) can be 6,000 NL h' ¹ L' ¹ or less, such as 5,000 NL h' ¹ L' ¹ or less, or 4,000 NL h' ¹ L' ¹ or less, or 3,000 NL-h' 1 L' ¹ or less, or 2,500 NL h' ¹ L' ¹ or less or 2,000 NL h' ¹ L' ¹ or less, or 1 ,000 NL h' ¹ L' ¹ or less. The average flow rate of the extraction agent per unit volume of the extraction chamber can be in a range between any of the recited values, such as in a range from 50 NL h' ¹ L' ¹ to 6,000 NL h' ¹ L' ¹ , or from 500 NL-h' ¹ -L' ¹ to 5,000 NL-h' ¹ -L' ¹ , or from 1 ,000 NL-h' ¹ -L' ¹ to 4,000 NL-h' ¹ -L' ¹ , or from 2,000 NL-h' ¹ -L' ¹ to 3,000 NL-h' ¹ -L' ¹ . Typically, the average flow rate per unit volume of the extraction chamber of the reactor (in L) is in a range from 500 NL h' ¹ L' ¹ to 3,000 NL h' ¹ L' ¹ .

[43] The average flow rate of the extraction agent (in NL/h) per mass unit of the amount of treated carbon black (in kg) can for example be 100 NL-h' ¹ -kg' ¹ or more, such as 500 NL-h' ¹ -kg' ¹ or more, or 1 ,000 NL-h' ¹ -kg' ¹ or more, or 5,000 NL-h' ¹ - kg ^-1 or more, or 10,000 NL-h' ¹ - kg ^-1 or more, or 20,000 NL-h' ¹ -kg' ¹ or more, or 50,000 NL-h' ¹ -kg' ¹ or more. For example, the average flow rate of the extraction agent per mass unit of the amount of treated carbon black (in kg) can be 100,000 NL-h' ¹ -kg' ¹ or less, such as 80,000 NL-h' ¹ -kg' ¹ or less, 50,000 NL-h' ¹ -kg' ¹ or less, or 20,000 NL-h' ¹ -kg' ¹ or less, or 10,000 NL-h' ¹ -kg' ¹ or less, or 5,000 NL-h' ¹ -kg' ¹ or less or 2,000 NL-h' ¹ -kg' ¹ or less, or 1 ,000 NL-h' ¹ -kg' ¹ or less. The average flow rate of the extraction agent per mass unit of the amount of treated carbon black (in kg) can be in a range between any of the recited values, such as in a range from 100 NL-h' ¹ -kg' ¹ to 100,000 NL-h' ¹ -kg' ¹ , or from 1 ,000 NL-h' ¹ -kg' ¹ to 50,000 NL-h' ¹ -kg' ¹ , or from 5,000 NL-h' ¹ -kg' ¹ to 20,000 NL-h' ¹ -kg' ¹ . Typically, the average flow rate per mass unit of the amount of treated carbon black (in kg) is in a range from 5,000 NL-h' ¹ -kg' ¹ to 100,000 NL-h' ¹ , such as from 5,000 NL-h' ¹ -kg' ¹ to 20,000 NL-h' ¹ -kg' ¹ . [44] The carbon black can be treated with the extraction agent in the process according to the present invention for any desirable time. The treatment time will generally be determined by applied extraction conditions and the desired degree of purification on the one hand and economic considerations on the other hand. For example, the carbon black can be treated with the extraction agent in the process according to the present invention for a time of at least one second, such as at least 10 seconds, or at least 30 seconds, or at least 1 minute, or at least 2 minutes, or at least 5 minutes, or at least 10 minutes, or at least 20 minutes, or at least 30 minutes, or at least 40 minutes, or at least 50 minutes, or at least 1 hour, or at least 2 hours, or at least 4 hours, or at least 6 hours, or at least 10 hours, or at least 15 hours. The treatment of the carbon black with the extraction agent in the process according to the present invention can for example be conducted for a time of up to 48 hours, such as 24 hours or less, or 20 hours or less, or 16 hours or less, or 10 hours or less, or 6 hours or less, or 4 hours or less, or 2 hours or less, or 1 hour or less, or 50 minutes or less, or 40 minutes or less, or 30 minutes or less, or 20 minutes or less, or 10 minutes or less, or 5 min or less, or 2 minutes or less or 1 minute or less, or 30 seconds or less, or 10 seconds or less. The time period can for example be in the range of 10 minutes to 45 minutes. The carbon black can be treated with the extraction agent for a time in a range between any of the recited values, for example from 1 minute to 48 hours, or from 5 minutes to 24 hours, or from 10 minutes to 4 hours, or from 20 minutes to 1 hour.

[45] The conditions such as pressure, temperature and flow rate of the treatment of the carbon black with the extraction agent in the process according to the invention can be held substantially constant during the treatment or be varied in a controlled manner over time. This can be advantageous since on the one hand the solvent properties of the supercritical extraction agent such as solute diffusivities, viscosity and mass transfer rate and on the other hand the solubilities and vapor pressures of the oxy-polycyclic aromatic hydrocarbons and PAHs each depend on the pressure and/or the temperature. Thus, changing the temperature, the pressure and/or the flow rate of the extraction agent in the treatment step over time can contribute to optimize the extraction efficiency. Temperature and/or pressure during the treatment step can for example be changed in a stepwise manner, i.e. the carbon black can be treated with the extraction agent for a predetermined first time at a first temperature and a first pressure, subsequently for a predetermined second time at a second temperature and a second pressure and so on. This is however only one example, and the extraction conditions can be changed during the treatment step in any possible manner, e.g. according to a customized predetermined program. A change of the conditions during the treatment step can for example be accomplished by changing the conditions within an extraction chamber and/or by transferring the carbon black between different zones of the extraction chamber and/or between different extraction chambers.

[46] The conditions of the treatment step in the process according to the invention can be chosen such that treating the carbon black with the extraction agent comprises extracting at least 50 wt.%, or at least 70 wt.%, or at least 80 wt.%, or at least 90 wt.%, or at least 95 wt.% or at least 99 wt.%, of the oxy-polycyclic aromatic hydrocarbons, from the carbon black, based on the initial content of oxy-polycyclic aromatic hydrocarbons. More specifically, treating the carbon black with the extraction agent can comprise extracting at least 50 wt.%, or at least 70 wt.%, or at least 80 wt.%, or at least 90 wt.%, or at least 95 wt.% or at least 99 wt.%, of the initial oxy-PAH6 content or of the initial content of 9,10-phenantrenedione from the carbon black. Moreover, treating the carbon black with the extraction agent can comprise extracting at least 30 wt.%, such as at least 40 wt.%, or at least 50 wt.%, or at least 70 wt.%, or at least 80 wt.%, or at least 90 wt.%, or at least 95 wt.% or at least 99 wt.%, or at least 99.5 wt.%, or at least 99.8 wt.%, or at least 99.9 wt.%, or at least 99.95 wt.% of the initial PAH content, such as of the initial PAH22 content, from the carbon black. [47] It is noted that the PAHs and oxy-PAHs may be present on the surface of and/or within the carbon black particles, whereby the distribution depends on the conditions of the production process and possible aftertreatment steps. (Oxy-)PAH molecules residing on the surface of a particle may typically be more easily removed during the supercritical fluid extraction than molecules being incorporated within a carbon black particle. Therefore, for instance (oxy-)PAHs residing predominantly on the surface of the particle may be removed more completely compared to (oxy-)PAHs being more evenly distributed between the particle surface and the particle volume.

[48] The process of the present invention further comprises removing the extraction agent comprising the extracted oxy-polycyclic aromatic hydrocarbons and optionally extracted PAHs from the carbon black to obtain a purified carbon black with a lower content of oxy-polycyclic aromatic hydrocarbons than the initial content of oxy-polycyclic aromatic hydrocarbons and optionally a lower content of polycyclic aromatic hydrocarbons than the initial content of polycyclic aromatic hydrocarbons. For example, the carbon black can be treated as set forth above with a flow of extraction agent such that the extraction agent comprising the extracted oxy-polycyclic aromatic hydrocarbons and optionally extracted PAHs is continuously removed from the treated carbon black, which is accordingly increasingly purified with progressing treatment time. A precipitation of the extracted oxy-polycyclic aromatic hydrocarbons and optionally extracted PAHs within the extraction chamber or periphery such as pressure lines connected thereto is generally to be avoided as this may lead to recontamination of the carbon black and/or plugging of the pressure lines. Precipitation of the extracted oxy-polycyclic aromatic hydrocarbons and optionally extracted PAHs in the extraction chamber and the pressure lines connected thereto can for example be prevented by heating them to a temperature high enough to keep the oxy-polycyclic aromatic hydrocarbons and optionally extracted PAHs dissolved in the extraction agent. [49] The process disclosed herein may optionally further comprise a step of separating at least a portion of the oxy-polycyclic aromatic hydrocarbons and optionally the PAHs from the extraction agent comprising the extracted oxy-polycyclic aromatic hydrocarbons and optionally PAHs removed from the carbon black. This can for example be accomplished by phase separation or reducing the solubility of the oxy-polycyclic aromatic hydrocarbons and PAHs in the extraction agent. For example, the temperature and/or pressure of the extraction agent comprising the extracted oxy-polycyclic aromatic hydrocarbons and optionally PAHs can be adjusted such that the extraction agent transforms into a gaseous state and the extracted oxy-polycyclic aromatic hydrocarbons and optionally PAHs can be separated from the gaseous extraction agent e.g. as a liquid and/or solid phase. Alternatively, the temperature and/or pressure of the extraction agent comprising the extracted oxy-polycyclic aromatic hydrocarbons and optionally PAHs can be adjusted such that the extracted oxy-polycyclic aromatic hydrocarbons and optionally PAHs condense and/or precipitate but the extraction agent remains in the supercritical state. The oxy-polycyclic aromatic hydrocarbons and optionally PAHs could also be separated from the extraction agent by passing the extraction agent comprising the extracted oxy-polycyclic aromatic hydrocarbons and optionally PAHs through a suitable filter such as an oxy-PAH/PAH adsorbing or absorbing medium. For instance, the extraction agent comprising the extracted oxy-polycyclic aromatic hydrocarbons and optionally PAHs can be passed through a liquid absorber medium, which can for example comprise one or more organic solvent, to absorb at least a portion of the oxy-polycyclic aromatic hydrocarbons and optionally PAHs by the liquid phase and yield an extraction agent depleted of oxy-PAHs and optionally PAHs. A suitable absorber medium is for example acetonitrile. The extraction agent comprising the extracted oxy-polycyclic aromatic hydrocarbons and optionally PAHs can be contacted with the absorber medium with the extraction agent in the supercritical state or after being transformed to a non-supercritical state, for example gaseous state. In the latter case, temperature and pressure conditions can be chosen such that only part or essentially none of the oxy-polycyclic aromatic hydrocarbons and optionally PAHs condense or precipitate prior to passing through the absorbing medium. Separating at least a portion of the oxy-polycyclic aromatic hydrocarbons and optionally PAHs from the extraction agent can also comprise transforming the extraction agent into a gaseous state and separating part of the extracted oxy-polycyclic aromatic hydrocarbons and optionally PAHs from the gaseous extraction agent as a liquid and/or solid phase by means of condensation and/or precipitation and further separating at least part of the remaining oxy-polycyclic aromatic hydrocarbons and optionally PAHs from the extracting agent by passing through an absorber medium.

[50] The process of the present invention may further comprise after the separation of at least a portion of the extracted oxy-polycyclic aromatic hydrocarbons and optionally PAHs from the extraction agent, recycling the thus obtained extraction agent for use in the step of treating the carbon black comprising an initial content of oxy-polycyclic aromatic hydrocarbons and optionally PAHs described above. Preferably, the recycled extraction agent is substantially free or completely free of oxy-polycyclic aromatic hydrocarbons and PAHs. “Substantially free” means in this respect that the recycled extraction agent contains less than 0.5 wt.%, such as less than 0.1 wt.% of oxy-polycyclic aromatic hydrocarbons and PAHs. “Completely free” means the recycled extraction agent contains no oxy-polycyclic aromatic hydrocarbons and PAHs, except for traces that may be present as omnipresent impurities.

[51] Optionally the process disclosed herein can further comprise detecting the amount of oxy-polycyclic aromatic hydrocarbons and/or PAHs extracted by the treatment of the carbon black with the extraction agent. To this end, for instance the extraction agent comprising the extracted oxy-aromatic hydrocarbons and optionally PAHs that has been removed from the carbon black as set forth above, e.g. a continuous effluent flow from an extraction chamber, can be analyzed for its content of extracted oxy-polycyclic aromatic hydrocarbons and/or PAHs. The analysis can be conducted continuously or discontinuously, e.g. as an online measurement, i.e. while the extraction treatment is ongoing, and make use of any analysis technique that provides a measurement allowing to draw quantitative or qualitative inferences regarding the contemporary or accumulated amount of oxy-PAHs and/or PAHs extracted from the carbon black. For example, in case the extracted oxy-polycyclic aromatic hydrocarbons and optionally PAHs are at least partially separated from the extraction agent by passing through a liquid absorber medium as mentioned above, the absorbance or absorbance change of the absorber medium at one or more characteristic wavelengths within the electromagnetic spectrum, e.g. in the UV or visible range of the electromagnetic spectrum, can be measured over time. From such measurement, a measure for the contemporary extracted amount and/or the overall amount of extracted oxy-polycyclic aromatic hydrocarbons and/or PAHs can be deduced. Such information related to a detection of the amount of oxy-polycyclic aromatic hydrocarbons and/or PAHs extracted by the treatment of the carbon black with the extraction agent can furthermore be used to control the treatment of the carbon black with the extraction agent. Thus, it can for instance be used to control the extraction time such as for example to terminate the treatment of the carbon black with the extraction agent when a certain amount of oxy- polycyclic aromatic hydrocarbons and/or PAHs extracted over time is indicated by the analysis. Furthermore, the detected information could be used in a feedback mechanism to control the extraction conditions such as pressure and/or temperature in the treatment of the carbon black with the extraction agent. For example, the carbon black comprising an initial content of oxy-polycyclic aromatic hydrocarbons and optionally PAHs can at first be exposed to the extraction agent at a first temperature and a first pressure. Subsequently, for example when the contemporary extracted amount of oxy-PAHs and/or PAHs or the extraction rate, as indicated by the detected information, drops below a threshold value, pressure and/or temperature can be adjusted to treat the carbon black with the extraction agent at a second temperature and a second pressure. In this way, the extraction parameters could be tailored to optimize for an extraction of the different oxy-PAH and PAH species from an increasingly purified carbon black. This may for example allow to define different conditions for extracting oxy-PAHs and optionally PAHs from a carbon black at an initial extraction stage or a carbon black at a later extraction stage already purified to some extent from oxy-PAHs and optionally PAHs, and/or to extract oxy-PAHs and/or PAHs being located at or near the surface of the carbon black particles or oxy-PAHs and/or PAHs being located within the carbon black particles as these may have different extraction characteristics. This can enhance extraction efficiencies while concomitantly minimizing the influence on other properties of the carbon black such as for example on surface oxygen-containing groups.

[52] Optionally the process according to the present invention can further comprise drying the carbon black comprising an initial content of oxy- polycyclic aromatic hydrocarbons and optionally PAHs prior to treating it with the extraction agent. The drying step can be conducted such that moisture is removed from the provided carbon black sample to an extent such that residual moisture, if any, does not exceed a predetermined level considered to be tolerable, such as for example 0.5 wt.% or 0.1 wt.%, if possible without substantially altering the surface chemistry of the carbon black particles. Drying is typically carried out at elevated temperatures such as at a temperature of 50°C or more, or 100°C or more, or 150°C or more, for example heating the carbon black sample to a temperature in a range from 100°C to 200°C, such as from 120°C to 180°C, for a time period of 1 minute or more such as 10 minutes or more, or 30 minutes or more, or 60 minutes or more, or 90 minutes or more. Heating can be achieved by any conventional means. The drying can be carried out in a gas atmosphere, e.g. a flow of a gaseous medium, which can be preheated to elevated temperatures. The gaseous medium can for example be air or nitrogen. The gaseous medium can however in particular comprise one or more components used in the extraction agent utilized later during the supercritical fluid extraction, however, in a gaseous state. As such, the gaseous medium can for example comprise or consist of carbon dioxide. In one implementation, the drying step is carried out at a temperature of about 150°C in gaseous carbon dioxide at a pressure of about 10 bar for about 1.5 hours. For instance, the provided carbon black can have an initial moisture content as described above, which can be reduced by the drying of the carbon black, for example removing thereby 80% or more, such as 90% or more, or 95% or more of the initial moisture content from the carbon black. During the drying step, the carbon black can reside in a reactor subsequently utilized for supercritical fluid extraction as described infra, such as for example within an extraction chamber of such reactor, or the drying may be carried out outside of such reactor or in a separate unit.

[53] The process according to the present invention can be carried out in a pressure-resistant reactor. Reactors for supercritical fluid extraction are commercially offered for example by Uhde High Pressure Technologies GmbH, Hagen, Germany and THAR Process Inc., PA, USA. The reactor is generally constructed to withstand the temperatures and pressures required for supercritical fluid extraction. The reactor can be made of suitable metallic construction materials such as e.g. stainless steel. The reactor generally comprises heating means for controlling the temperature in the treatment step with the extraction agent. The heating means can be any conventional heating means. The reactor may comprise an extraction volume, such as an extraction chamber, in which the carbon black is provided for treatment with the extraction agent. The extraction chamber can for example have a volume of 0.01 L or more, such as 0.05 L or more, or 0.1 L or more, or 0.5 L or more, or 1 L or more, or 5 L or more, or 10 L or more, or 50 L or more, or 100 L or more, or 200 L or more, or 500 L or more, or 1 ,000 L or more. The extraction chamber can for example have a volume of 10,000 L or less, such as 5,000 L or less, or 2,000 L or less, or 1,000 L or less, or 500 L or less, or 200 L or less, or 100 L or less, or 50 L or less, or 20 L or less, or 10 L or less, or 5 L or less, or 2 L or less, or 1 L or less, or 0.5 L or less, or 0.2 L or less, or 0.1 L or less. The volume of the extraction chamber can be in a range between any of the recited values such as in a range from 0.01 L to 5,000 L, or from 0.05 L to 0.5 L, or from 1 L to 2,000 L, or from 10 L to 1,000 L. A reactor can comprise a single extraction chamber or two or more extraction chambers. For instance, a reactor with two or more extraction chambers can be used, which may allow for a quasi-continuous operation also in batch mode wherein one or more of the extraction chambers are charged with the initial carbon black to be treated or treated carbon black is discharged therefrom while carbon black is extracted in one or more other extraction chamber(s) of the reactor. Thus, providing a carbon black comprising an initial content of oxy- polycyclic aromatic hydrocarbons and optionally PAHs can comprise introducing an amount of said carbon black into the extraction chamber(s) of the reactor. Typically, the extraction chamber(s) is fed with extraction agent through an inlet connected to a feeding line from one or more sources of the extraction agent. The extraction agent comprising oxy- polycyclic aromatic hydrocarbons and optionally PAHs can be withdrawn from the extraction chamber(s) through an outlet and connected effluent line. The reactor typically further comprises conventional means for flow and process control such as sensors, pressure or flow regulation means, valves, pumps and controllers. Typically, the one or more than one extraction chamber is designed such that a flow of the extraction agent may be forced through the carbon black material rather than flowing for example above the carbon black material. In this way, the contact time of the extraction agent with the carbon particles may be increased thus enhancing extraction efficacy.

[54] For example, carbon dioxide may be supplied as extraction agent in a pressurized container. The carbon dioxide can be withdrawn from the container e.g. to establish a continuous flow with at a predetermined flow rate, e.g. regulated by one or more pumps and/or flow control means connected to the feeding line. Pressure and temperature of the extraction agent can be regulated by pressure regulating and heating means to provide the extraction agent in a supercritical state. Pressure regulation can for example be accomplished by control of the pump(s), valves and back-pressure regulators in the system, whereas heating can for example be accomplished by heating the feeding line e.g. by providing the same with electrical heating jackets, heating tapes or alike, and/or by one or more heating elements that heat the extraction chamber, which can e.g. be of a resistive electrical heater type. The obtained flow of supercritical carbon dioxide extraction agent contacts the carbon black in the extraction chamber to extract oxy-PAHs and optionally PAHs therefrom. Optionally, auxiliary agents such as those mentioned above can be supplied to the flow of carbon dioxide at a predetermined constant or variable ratio at any stage of the reactor such as upstream of the extraction chamber.

[55] The process can further comprise retrieving and/or collecting the purified carbon black. This can involve stopping a feed of the extraction agent, withdrawing the extraction agent or the purified carbon black from the extraction chamber, or otherwise separating the purified carbon black and the extraction agent. Generally, the process according to the present invention can be conducted as a continuous process, as a semi-batch or as a batch process. In case of a continuous process, carbon black comprising an initial content of oxy-polycyclic aromatic hydrocarbons and optionally PAHs can for example be continuously fed to an extraction chamber where it is treated with the extraction agent, e.g. using a continuous flow of the extraction agent, and the purified carbon black be continuously withdrawn from the extraction chamber. Preferably, such continuous process can be carried out in a manner with no substantial mixing of the carbon black particles fed at different times into the extraction chamber such that the residence time in the extraction chamber and thus the extraction time is approximately the same. Moreover, a flow of extraction agent from the inlet to the outlet may be in an opposite direction, the same direction, a perpendicular direction or any other angular configuration to the conveying direction of the carbon black particles.

[56] In case of a batch or semi-batch process, a batch of carbon black comprising an initial content of oxy-polycyclic aromatic hydrocarbons and optionally PAHs can be loaded to an extraction chamber and treated with the extraction agent for a desired time under controlled conditions to extract oxy-PAHs and optionally PAHs and produce the purified carbon black having a reduced content of oxy-PAHs and optionally a reduced content of PAHs. After the desired time, the treatment can be stopped and the purified carbon black be retrieved, for example by releasing the pressure and removing the purified carbon black from the extraction chamber. Prior to removing the purified carbon black from the extraction chamber, the extraction agent can optionally be removed from the extraction chamber and replaced with a gaseous medium such as for example nitrogen or air, and then reducing the temperature or pressure, e.g. to ambient conditions. In this way, condensation or precipitation of extracted oxy-polycyclic aromatic hydrocarbons and optionally PAHs comprised in the extraction agent can be avoided. Separation of any residual extraction agent from the purified carbon black can be effectuated by reducing the pressure and/or the temperature below the respective critical value(s) for the extraction agent, thereby transforming the extraction agent to the gaseous state. Since carbon dioxide is a gas at ambient conditions, separation from the purified carbon black can be accomplished according to the present invention in a straightforward manner without the need of any further drying or purification steps, which may be required for example when organic solvents or steam is employed for extraction.

[57] The process of the present invention can generally be carried out independently of carbon black production or treatment processes. It can accordingly be applied to a wide variety of different carbon black grades. The process can nevertheless advantageously be implemented in a carbon black production plant and be carried out e.g. after a carbon black production or treatment process. For example, the process disclosed herein can be implemented downstream of a carbon black production, such as for example downstream of a furnace reactor, and upstream or downstream of other carbon black aftertreatment processes such as for example an oxidative treatment.

[58] The purified carbon black obtainable by the process according to the present invention has a lower content of oxy-polycyclic aromatic hydrocarbons than the initial content of oxy-polycyclic aromatic hydrocarbons of the carbon black provided for purification. The purified carbon black can for example have a content of oxy-polycyclic aromatic hydrocarbons, which corresponds to 50 wt.% or less, or 30 wt.% or less, or 20 wt.% or less, or 10 wt.% or less, or 5 wt.% or less, or 1 wt.% or less, or 0.5 wt.% or less, or 0.2 wt.% or less, or 0.1 wt.% or less, or 0.05 wt.% or less of the initial content of oxy-polycyclic aromatic hydrocarbons. For instance, the purified carbon black can have a oxy-PAH6 content or content of 9,10-phenantrenedione, which corresponds to 50 wt.% or less, or 30 wt.% or less, or 20 wt.% or less, or 10 wt.% or less, or 5 wt.% or less, or 1 wt.% or less, or 0.5 wt.% or less, or 0.2 wt.% or less, or 0.1 wt.% or less, or 0.05 wt.% or less of the initial oxy-PAH6 content or of the content of 9,10-phenantrenedione, respectively. Moreover, the purified carbon black obtainable by the process according to the present invention may optionally further have a lower content of PAHs than the initial content of PAHs of the carbon black provided for purification. For instance, the purified carbon black can have a PAH content, such as PAH22 content, which corresponds to 60 wt.% or less, or 50 wt.% or less, or 30 wt.% or less, or 20 wt.% or less, or 10 wt.% or less, or 5 wt.% or less, or 1 wt.% or less, or 0.5 wt.% or less, or 0.2 wt.% or less, or 0.1 wt.% or less, or 0.05 wt.% or less of the initial PAH content, such as of the initial PAH22 content.

[59] The purified carbon black obtainable by the process according to the present invention may for example have a PAH22 content of less than 1,500 ppm, such as less than 1,000 ppm, or less than 700 ppm, or less than 500 ppm, or less than 200 ppm, or less than 150 ppm, or less than 100 ppm, or less than 50 ppm, or less than 20 ppm, or less than 10 ppm, or less than 5 ppm, or less than 3 ppm, or less than 2 ppm, or less than 1 ppm, or less than 0.5 ppm.

[60] The purified carbon black obtainable by the process according to the present invention may moreover for example have an oxy-PAH6 content of less than 200 ppm, such as less than 100 ppm, or less than 50 ppm, or less than 25 ppm, or less than 10 ppm, or less than 5 ppm, or less than 3 ppm, or less than 1 ppm. The purified carbon black obtainable by the process according to the present invention can in particular have a content of 9,10-phenantrenedione of less than 1 ppm.

[61] The purified carbon black can have any combination of the PAH22 and oxy-PAH6 and/or 9,10-phenantrenedione contents specified above. The purified carbon blacks obtainable according to the process according to the present invention can have an oxy-PAH content and/or a PAH content such as PAH22 content that ensures compliance with official regulations for applications of the purified carbon blacks in areas such as use in food or beverage contact situations, pharmaceuticals, cosmetics, or the manufacture of toys and articles for children, e.g. compliance with FDA regulations.

[62] The purified carbon black can further have any of the other characteristics and properties described above for the carbon black provided as starting material to be purified, such as carbon content, oxygen content, volatile content, ash content, moisture content, and BET surface area. These properties may remain substantially unaffected by the purification process disclosed herein. Thus, the purified carbon black may apart from the content of oxy-PAHs and optionally PAHs substantially correspond to the carbon black provided as starting material to be purified. For instance, the carbon content, oxygen content, volatile content, ash content, moisture content, and/or BET surface area of the purified carbon black can correspond to the respective value of the carbon black provided as starting material, as described above, ±30%, or ±20%, or ±10%, or ±5%.

[63] The purified carbon blacks obtained according to the present invention can be used in any application, where carbon blacks are conventionally employed or useful. The purified carbon blacks according to the present invention can for example be employed as pigment, reinforcing filler or conductive agent, such as for the manufacture of plastic or rubber articles, paints, inks, coatings, electrodes or energy storage devices. The purified carbon blacks according to the present invention are particularly useful in applications, where there is an increased awareness or concern regarding oxy-PAHs and/or PAHs or where PAH-related official regulations exist, such as in food or beverage contact situations, pharmaceuticals, cosmetics, or the manufacture of toys and articles for children.

[64] Having generally described the present invention above, a further understanding can be obtained by reference to the following specific examples. These examples are provided herein for purposes of illustration only, and are not intended to limit the present invention, which is rather to be given the full scope of the appended claims including any equivalents thereof.

EXAMPLES

[65] All parts and percentages indicated throughout the Examples refer to weight, unless specified otherwise. materials:

[66] Carbon blacks:

[67] Carbon Black A: Printex U, a commercially available gas black from Orion Engineered Carbon GmbH, as an example of a carbon black having a negligible initial oxy-PAH content (Comparative Example).

[68] Carbon Black B: Ozone-oxidized Carbon Black A, as an example of a carbon black having a considerable initial oxy-PAH content.

[69] Extraction agent: Carbon dioxide with a purity of 99.995 volume-%, supplied in pressurized liquid form in a 50 L dip tube bottle, commercially available from Westfalen AG.

[70] Supercritical fluid extraction of samples of the above-identified investigated carbon blacks was carried out in a custom-made high-temperature, high- pressure supercritical fluid extraction setup using supercritical carbon dioxide as extraction agent. The setup comprises a tube-shaped extraction chamber (inner diameter: 1.43 cm, length: 50 cm, volume: 0.080 L) made of stainless steel (Swagelok IPT series 316/316L) with an inlet at one end and an outlet at its opposite end. The extraction chamber was mounted in an aluminum block equipped with four heating cartridges (Horst Heizpatronen 230 V, diameter 12.5 mm, length 160 mm, nominal power 500 W) for heating the extraction chamber. Two thermocouples (type K) were mounted within the aluminum block and used in combination with heating controllers (Eurotherm Universalregler 818 and 808) for measurement and regulation of the temperature of the aluminum block. The dip tube bottle containing carbon dioxide was connected via conventional " tubes to the inlet of a pump (Knauer 80 P with an 100 mL pump head equipped with a cooling unit utilizing a Huber Ministat 125w cc1 cryostat) and from the outlet of the pump via a pressure line (Swagelok IPT series, outer diameter ") to the inlet of the extraction chamber for feeding the extraction agent to the extraction chamber. An exhaust pressure line (Swagelok IPT series, outer diameter %") connected to the outlet of the extraction chamber leads via a back-pressure regulator (customized Equilibar blockage resistant BPR equipped with a polyimide membrane and Kalrez® membranes) for reducing the pressure below the critical value into an absorption chamber located downstream of the extraction chamber to pass the (then gaseous) extraction agent laden with oxy-PAHs and PAHs through a volume of acetonitrile provided as absorbing medium in the absorption chamber and releasing the purified extraction medium into the atmosphere by passing it through a mass flow meter (Bronkhorst F-201 CV) and a valve. Two filters (Swagelok IPT high pressure filters with each a 2 pm pore and a 0.5 pm pore filter element) were placed in the pressure lines upstream of and downstream of the extraction chamber, respectively, to avoid contamination of the pressure lines. The feed and exhaust pressure lines were moreover mantled with heating tapes (Horst Heizleitungen HS 450°C controlled by Eurotherm Universalregler) for heating of the extraction agent upstream and downstream of the extraction chamber to avoid precipitation and plugging of the lines. Flow rate and pressure of the continuous flow of extraction agent through the extraction chamber were controllable independently on the one hand by the pump connected to the feeding pressure line and on the other hand by the backpressure regulator located downstream of the extraction chamber. The reference pressure applied to the dome of the BPR was delivered by a bypass line branching off from the feeding pressure line between the pump and the inlet of the extraction chamber. fluid extraction:

[71] For supercritical fluid extraction, the extraction chamber was filled with about 5 g of the carbon black to be extracted. The carbon black was fixed between two glass wool plugs. The extraction chamber was then heated to the extraction temperature of 250°C and a continuous flow of the extraction agent through the extraction chamber provided, controlling the flow rate and pressure of the extraction agent by the pump and back-pressure regulator. The sample was then subjected to continuous supercritical fluid extraction using supercritical carbon dioxide as extraction agent at a pressure of 300 bar, a temperature of 250°C and an estimated average flow rate of the extraction agent through the extraction chamber corresponding to 150 or 60 NL/h (average flow rate per unit volume of the extraction chamber: 1 ,866 or 746 NL h' ¹ L' ¹ ) for a time of 4-5 h, respectively. Thereafter the flow of the extraction agent was stopped, the pressure released from the system and the sample allowed to cool to ambient temperature.

The thus obtained extracted carbon black samples were analyzed for their PAH22 and oxy-PAH content as described below.

Determination of PAH22 and oxy-PAH content:

[72] The investigated carbon blacks were analyzed for their PAH22 content after supercritical fluid extraction and compared to the initial PAH22 content determined for a reference sample of the respective pristine carbon black that has not been subjected to supercritical fluid extraction. The PAH22 content was each determined following the method entitled “Determination of PAH content of Carbon Black”, dated July 8, 1994, as developed by Cabot Corp., and incorporated by the American Food and Drug Administration (FDA) in the U.S. Code of Federal Regulations (CFR) 21 Sec.178.3297, as follows:

[73] The carbon black material was crushed in a mortar with a pestle until a homogenous powder was obtained. A suitable amount (up to 10 g) of the powder was precisely weighed in a cellulose extraction thimble (MN 645, Macherey-Nagel, Duren, Germany). A glass wool plug and cellulose pieces from an extraction thimble were put on top of the carbon black and the filled thimble then loaded in the extraction chamber of a 100 mL Soxhlet apparatus with a 250 mL round bottom flask. Toluene was added to the flask and the condenser of the apparatus was gently flushed with nitrogen. The sample was then subjected to Soxhlet extraction with toluene in the Soxhlet apparatus for 48 h under light protection at a rate of approx. 10 cycles per hour. The obtained raw extract was then concentrated to slightly over 5 mL by means of a rotary evaporator operated at 40°C and a pressure reduction of 5 kPa as a minimum (Buchi Rotavapor R-200, Buchi Labortechnik AG, 9230 Flawil, Switzerland). The extract was then transferred to a 10 mL volumetric flask and brought to the mark by adding fresh toluene. To an aliquot of the extract were added 17 deuterated PAH standards (Ds-Naphthalene, Ds-Acenaphthylene, Dio-Acenaphthene, D10- Fluorene, Dw-Phenanthrene, Dw-Anthracene, Dio-Fluoranthene, D10- Pyrene, Di2-Benzo[a]anthracene, Di2-Chrysene, Di2-Benzo[b]fluoranthene, Di2-Benzo[k]fluoranthene, Di2-Benzo[a]pyrene, Di4-Dibenz[a,h]anthracene, Di2-Benzo[g,h,i]perylene, Di2-lndeno[1 ,2,3-c,d]pyrene and Di2-Coronene, each in an amount of 200 ng). Then, the extract aliquot was cleaned-up by treatment with a silica gel column (1 g silica gel/13% H2O, 8 to 10 mm inner diameter and 5 cm ³ capacity). Subsequently, a further deuterated compound, D-12-Perylene, was added to the cleaned-up extract as recovery standard in an amount of 200 ng. The thus obtained solution was then used for HRGC/LRMS analysis (Capillary gas chromatography coupled with low resolution mass spectrometry) for PAH identification and quantification using the following instrumentation and conditions: Gas chromatograph: Thermo Scientific GC-Ultra with PTV injector, GC-column: 60 m DB5-MS, 0.25 mm ID, 0.25 pm film thickness; temperature program GC oven: preheating oven to 80°C, sample injection, holding for 2 min at 80°C, heating with a rate of 25°C/min to 180°C, heating with a rate of 8°C/min to 220°C, heating with a rate of 2°C/min to 250°C, heating with a rate of 3°C/min to 280°C, heating with a rate of 5°C/min to 320°C, hold at 320°C for 21 min and 18 seconds; Mass spectrometer: Thermo Scientific Trace DSQ LRMS, operated in the electron impact mode (El) and Selected Ion Monitoring (SIM Mode); mass resolution: 1 amu; monitoring of molecular and fragment ions for the individual PAH compounds. Calibration check of the instrument was performed for each analysis sequence by injection of mixtures containing all native PAHs of interest and the above- mentioned deuterated standards. Identification of the PAH species was achieved by analysis of the relative retention time, the molecular and fragment ions, and the fragmentation ratio. Quantification was performed using the instrumentation software via the deuterated internal PAHs using the isotope dilution and internal standard method. The PAH22 content was calculated by summing up the individual determined concentrations of the 22 PAH compounds, whereby for compounds, whose concentration were below the limit of quantification (LOQ), the LOQ was adopted as the respective concentration. The co-eluting isomer dibenz(a,h)anthracene and dibenz(a,c)anthracene could not be separated by the GC column and where thus taken as one substance, reported herein as “dibenz(a,h)anthracene”.

[74] The investigated carbon black samples were also analyzed for their content of 9,10-phenantrenedione, which served as an indicator of the oxy-PAH content, after supercritical fluid extraction and compared to the initial content of 9,10-phenantrenedione determined for a reference sample of the pristine carbon black that has not been subjected to supercritical fluid extraction. The determination of the oxy-PAH content was carried out in analogy to the determination of the PAH22 content as described above, based on the same analytical methods. In particular, the extraction of the carbon black, the volume reduction of the raw extract and the adjustment of a defined volume were performed exactly in the same manner as described above. The further steps were carried out as described above with the following oxy-PAH specific adaptations: To an aliquot of the extract was added as internal standard a deuterated nitro-PAH (D9-3-Nitrofluoranthene in an amount of 250 ng) instead of the above-mentioned 17 deuterated PAH standards. The oxy-PAH extract aliquot containing the deuterated internal standard was directly subjected to High Resolution Mass Spectrometry (HRGC/HRMS) without further treatment. The following instrumentation and conditions were applied: Thermo Scientific GC-Ultra 2000 with PTV injector, GC-column: 30 m DB5-MS, 0.25 mm ID, 0.1 pm film thickness, temperature program GO oven: preheating oven to 80°C, sample injection, holding for 3 min and 42 seconds at 80°C, heating with a rate of 35°C/min to 180°C, heating with a rate of 6°C/min to 290°C, hold at 290°C for 37 seconds; mass spectrometer: Thermo Scientific MAT 95 HRMS, operated in the electron impact mode (El) and Selected Ion Monitoring (SIM Mode); mass resolution: <8.000 amu, monitoring of molecular and fragment ions for the oxy-PAH compound. Calibration check of the HRMS instrument was performed for each analysis sequence by injection of mixtures containing 9,10-phenantrenedione, 9- Nitrofluoranthene and the above-mentioned deuterated standard. Identification of the oxy-PAH species was achieved by analysis of the relative retention time, the molecular and fragment ions, and the fragmentation ratio. Quantification was performed using the instrumentation software via the deuterated internal nitro-PAH using the standard method.

[75] The PAH22 content and content of 9,10-phenantrenedione of the extracted Carbon Black A and Carbon Black B samples was each determined as described above. The results are summarized in Table 1 below in comparison to the initial PAH22 content and content of 9,10- phenantrenedione determined for the pristine carbon blacks A and B that have not been subjected to SFE as a reference. The reported relative extracted amount has been calculated according to the formula 1- (x(example)/x(reference)), wherein x(example) and x(reference) represent the detected amount of the indicated compound or detected total amount of the indicated group of compounds for the given extracted carbon black and the respective pristine reference carbon black, respectively. P54583WO APPL filed_130623.doc

39

[76] As illustrated by Example 1 in Table 1 , conventional carbon blacks not oxidatively aftertreated typically have a negligible content of oxy-PAHs, but may contain significant amounts of PAHs (Reference 1). Purified carbon blacks with a significantly reduced content of polycyclic aromatic hydrocarbons compared to the starting material (Reference 1) can be obtained through the supercritical fluid extraction with carbon dioxide as extraction agent (Example 1). On the other hand, as illustrated by Example 2, oxidation with an oxidation agent as ozone, can yield carbon blacks, which have a significantly reduced PAH content, but a considerable amount of oxy-PAHs (Reference 2). As demonstrated by Example 2, supercritical fluid extraction with carbon dioxide as extraction agent allows however to effectively remove also the oxy-PAHs from the carbon black. Thus, purified carbon blacks with a significantly reduced content of oxy- PAHs (as well as PAHs) compared to the starting material (Reference 2) can be obtained through the supercritical fluid extraction with carbon dioxide as extraction agent (Example 2).