Process To Produce Oil With Low Polyaromatic Hydrocarbon Content

Abstract

Process for TDAE-1 and TDAE-2 production is initiated with production of DAE Feeds which have kinematic viscosity at 100 C. ranges 24-67 cSt, followed by mixing them with solvent to yield Mixture of DAE Feed with density ranges 0.75-0.85 kg/liter and further contacting the Mixture of DAE Feed with solvent, like furfural, NMP and DMSO to facilitate a counter current liquid-liquid extraction, wherein the TDAE-1 and TDAE-2 are produced at ratio of polar solvent to Mixture of DAE Feed ranges 1.7-2.0 and 0.5-1.7, respectively. The PCA content of TDAE-1 and TDAE-2 are less than 3% weight and 3-20% weight. The amount of 8 Grimmer polyaromatics hydrocarbon content in the TDAE-1 and TDAE-2 are the same, that is, less than 10 mg/kg including Benzo (a) pyrene substance as much as less than 1 mg/kg.

Claims

1. A treated distillated aromatic obtained by a process comprising the following the steps: a. preparing a distillate aromatic extract (DAE) Feed by mixing one, two, or three different DAE having different kinematic viscosities, b. mixing the DAE Feed obtained at the step a above with a diluent to obtain a mixture of DAE Feed having a density of 0.75-0.85 kg/liter, wherein the diluent is selected from n-pentane, isopentane, n-hexane, n-heptane, n-octane and isooctane, c. directing the mixture of DAE Feed to an extractor that has an isothermic temperature, ranges 22-35 C., d. contacting the mixture of DAE Feed with a furfural solvent so that a liquid-liquid extraction process with counter current technique take place at an isothermic temperature, ranges 22-35 C., e. adjusting a process of separation of interface layers in the extractor thereby transporting a mixture of raffinate and a mixture of extract through a control equipment placed at the lower portion of the column, and f. directing the mixture of raffinate to a solvent recovery unit to separate out the solvent and the diluent from the mixture of raffinate to yield an end product.

2. The process of claim 1, wherein in preparing the DAE Feed, the process for producing the DAE comprises a furfural solvent extraction.

3. The Process of claim 2, wherein the DAE Feed is produced by means of mixing DAE-1, DAE-2, and DAE-3, or combinations thereof.

4. The process of claim 3, wherein the ratio of mixing of DAE-1, DAE-2, DAE-3 ranges 25%-35%, 14%-35% and 41%-51%, respectively.

5. The process according to claim 1, wherein the kinematic viscosity is at 100 C., ranges 24-67 cSt.

6. The process according to claim 1, wherein the process further comprises a step of: g. collecting the solvent and the diluent separated out at the step f above into a container for reutilization at a next extraction process.

7. The process according to claim 1, wherein the ratio of diluent to DAE Feed is 1.

8. The process according to claim 1, wherein the treated distillated aromatic extract is characterized by comprising polycyclic aromatic (PCA) less than 3%, the sum of eight types of polyaromatic hydrocarbon (8 Grimmer PAH) less than mg/kg, benzo(a)pyrene (BaP) less than 1 mg/kg, and aromatic content of more than 25% weight calculated based on ASTM D2140.

9. The processes according to claim 8, wherein the treated distillated aromatic extract contains aromatic compound ranges 25-31% weight and kinematic viscosity at 100 C. ranges 16-24 cSt.

10. The process according to claim 1, wherein the treated distillated aromatic extract contains aromatic compounds in the range of 31%-37%.

11. The process according to claim 1, wherein the treated distillated aromatic extract is characterized by comprising polycyclic aromatic (PCA) 3%-20%, the sum of eight types of polyaromatic hydrocarbon (8 Grimmer PAH) less than 10 mg/kg, ben-zo(a)pyrene (BaP) less than 1 mg/kg, and aromatic content of more than 25% weight calculated based on ASTM D2140.

12. The processes according to claim 11 to obtain the treated distillated aromatic extract product with yield of 50% to 70% weight.

13. A treated distillated aromatic extract-1 (TDAE-1), characterized by comprising polycyclic aromatic (PCA) less than 3%, the sum of eight types of polyaromatic hydrocarbon (8 Grimmer PAH) less than 10 mg/kg, benzo(a)pyrene (BaP) less than 1 mg/kg, and aromatic content of more than 25% weight calculated based on ASTM D2140.

14. A treated distillated aromatic extract-2 (TDEA-2), characterized by comprising polycyclic aromatic (PCA) 30-20%, the sum of eight types of polyaromatic hydrocarbon (8 Grimmer PAH) less than 10 mg/kg, ben-zo(a)pyrene (BaP) less than 1 mg/kg, and aromatic content of more than 25% weight calculated based on ASTM D2140.

Description

BRIEF SUMMARY OF THE FIGURE

[0015] The following drawing forms part of the present specification and is included to further demonstrate certain aspects of the present invention. The invention may be better understood by reference to this drawing in combination with the detailed description of specific embodiments presented herein.

[0016] FIG. 1 is diagram flow of process on Blending of DAE Feed, Mixture of DAE Feed and TDAE-1 and TDAE-2 productions.

DETAILED DESCRIPTION OF THE INVENTION

[0017] While the present invention is described related to the embodiments as illustrated herein after, as well as the accompanied drawing, it has to be understood that they are not intended to represent the only form of the invention in regard to the details of the process and manner of operation. In fact, it will be evident to one skill in the art that modifications and variations may be made without departing from the spirit and the scope of the invention. Although specific terms have been employed, they are intended in a generic and descriptive sense only and not for the purpose of limitation.

[0018] FIG. 1 explains the flow diagram of TDAE-1 and TDAE-2 production. Flows (1, 2, and 3) illustrate the mixing process of one, two or three types of DAE to yield the DAE Feed (4). The mixing process are conducted at the kinematic viscosity desired, at temperature of 100 C., that is, 24-67 cSt and density 0.98-1.20 kg/liter. The formula determinations are based on the kinematic viscosities at temperature of 100 C. for each component of DAE-1, DAE-2 and DAE-3, respectively. Mixing process are conducted in in-line or off-line and completed with stirring in a container. After the DAE Feeds are available, the process continued with making Mixture of DAE Feed (6) by dissolving diluents (5) into the flow of Mixture of DAE Feed to yield density of Mixture of DAE Feed 0.75-0.85 kg/liter and further guided into the extractor (7). At the same time, the flow of polar solvent (8) is being contacted with the Mixture of DAE Feed (6) with the counter current method so that it forms a separate mixture of raffinate phase (9) and mixture of extract phase (12). The mixture of raffinate phase and mixture of extract phase then are guided to the Recovery Unit (10 and 13), respectively, to yield TDAE-1 and TDAE-2 and HACE (14) products, at the same time recovering all the solvent and diluents for continues reutilization.

[0019] The process for TDAE-1 and TDAE-2 production in the present invention is started with DAE feed making by mixing the components of DAE-1, DAE-2 and DAE-3; or using a single type of DAE. The mixing manner can be applied to two or three types of the DAE. The formula determination is based on the kinematic viscosities at temperature of 100 C. for each component of DAE-1, DAE-2 and DAE-3 so that they yield DAE Feed with the kinematic viscosity at 100 C. between 24 to 67 with density of 0.98-1.20 kg/liter. The mixing process are conducted in-line or off-line and completed with stirring them in a container.

[0020] The next process is mixing the DAE feed and diluent of alkane compound/paraffin that have chain of carbon atom range C5-C8. The ratio of the mixing between the diluent and the DAE Feed is 0.3-3.0, preferably at 1.0. This is done using an equipment that can control and that arrange the amount of diluent flow into the flow of DAE Feed, so that yield Mixture of DAE Feed with density between 0.75 to 0.80 kg/liter.

[0021] This flow of Mixture of DAE Feed then become next feed at liquid-liquid extraction process in the extractor (7). Uniquely, this extractor consist of some compartments, wherein each compartment provided with one static disc and one turbine agitator which is revolvable in accordance with the desired operation condition. The turbine agitator function to disperse each of flow to become droplet so that a perfect extraction process may take place at a minimum density difference of 0.05 kg/liter.

[0022] The extraction process of Mixture of DAE feed in the extractor is carried out using certain solvent, such as furfural, NMP and DMSO as polar solvent. The operation condition is arranged in a manner such that the isothermic temperature at upper and lower extractor are at 22-35 C. achieved, with rotational speed of agitator 75-100 RPM, and the ratios of certain solvent such as furfural, NMP and DMSO and the DAE mixture feed range 0.5-2.0. With the ratio of polar solvent to DAE mixture feed ranges 1.7-2.0 a TDAE-1 containing PAH less than 10 mg/kg and BaP less than 1 mg/kg with PCA less than 3% weight will be yielded. In addition, when the ratio of polar solvent to DAE mixture feed ranges 0.5-1.7 a TDAE-2 containing PAH less than 10 mg/kg and BaP less than 1 mg/kg with PCA less than 3% weight will be yielded.

[0023] The extraction process requires 15-30 minute time for retention of Mixture of DAE Feed so that the layers of mixture of raffinate and mixture of extract are formed. During this process no pseudo raffinate is present such that occurs in the other regular extraction processes.

[0024] The interface layer of the two mixtures (mixture of raffinate and mixture of extract) can be set through a control equipment disposed at the lower portion of the extractor. The placement of the equipment at the lower portion is to prevent the undesirables extract flow (entrainment) from entering the flow of raffinate which may lower the quality of the raffinate.

[0025] The mixture of raffinate is led into the solvent recovery unit for separation of raffinate from its certain solvent components, like furfural, NMP and DMSO and diluent.

[0026] From this process an end product will yielded, that is TDAE-1 or TDAE-2, which have the kinematic viscosities at temperature of 100 C. (ASTM D445-06) above 16 cSt, the aromatic component analysed using the method of ASTM D 2140-97 ranges 25-38% weight, specific gravity at 15.6 C. ranges 0.966-0.988, aniline point ranges 43.0-75.0 C., refraction index at 20 C. ranges 1.5379-1.5546.

[0027] The mixture of extract is led into the recovery unit for extract separation process from its certain solvent component, like furfural, NMP and DMSO. From this process an end product, that is, HACE will be obtained.

[0028] Flow of certain solvents, like furfural, NMP and DMSO and the diluent from solvent recovery unit are collected at one particular decanter (container) henceforth conducted separation process between diluent and the certain solvent, like furfural, NMP and DMSO. Both of the flow is returned back into the extraction process that run continuously.

[0029] The TDAE-1 and TDAE-2 being produced will be utilized as process oil in the tyre manufacturing and in the printing ink replacing the DAE that will be totally eliminated from its application due to its poor health effects due to the content of carcinogen substances.

EXAMPLES

Example 1

Preparation of DAE Feed

[0030] The extract of DAE-1, DAE-2, and DAE-3 are prepared according to their properties as can be seen in the Table 1, respectively. The mixing process of the two or three DAE are conducted at the kinematic viscosity desired, that is, at temperature of 100 C., is 24 to 60 cSt. The formula determination is based on the kinematic viscosities of each component of DAE-1, DAE-2 and DAE-3, respectively, so that they can yield the desired. DAE Feed Mixing process are conducted in-line or off-line and completed with stirring them in a container.

TABLE-US-00001 TABLE 1 The properties of DAE Feed Parameter DAE-1 DAE-2 DAE-3 Refraction index at 70 C. 1.4585-1.4640 1.488-1.489 1.476-1.481 Specific gravity at 70 C. 0.8200-0.8235 0.8600-0.8700 0.770-0.9000 Flash point, C. Minimum 240 Minimum 240 Minimum 240 Kinematic viscosity at 100 C. 14-17 19-35 52-95 Kinematic viscosity at 60 C. 17.3-20 Kinematic viscosity at 40 C. 449 2555 11664 Furfural content, mg/kg Maximum 100 Maximum 100 Maximum 100

TABLE-US-00002 TABLE 2 The physical analysis of DAE Feeds. Result of DAE Feed Test DAE DAE DAE Parameter Feed 1 Feed 2 Feed 3 Specific gravity API 4.43 Aniline Point, C. 31.8 Color ASTM 2.0 Density at 15.6 C., kg/m3 1.040 Flash point, C. 243 Pour point, C. 15 Refraction index at 20 C. 1.5988 Refractive Intercept 1.0802 Specific gravity at 15.6 C. 1.0410 Viscosity gravity constant 0.9989 Kinematics Viscosity at 100 C., cSt 32.35 22.68 32.57 Viscosity Saybolt at 98.9 C., SUS 160.6 Sulphur, % weight 5.37 Carbon atom Type C.sub.A, % weight 48.0 49.0 C.sub.N, % weight 21.0 18.0 C.sub.P, % weight 31.0 33.0 PCA, % weight 28.8 25.9 26.2

TABLE-US-00003 TABLE 3 The composition of Polyaromatic Hydrocarbon DAE Feeds. DAE-Feed 1 DAE-Feed 2 Unit EC (mg/kg)*** (mg/kg) Phenantrene 4.410 6.263 Antracene <0.001 0.060 Fluoranthene 0.226 0.303 Pyrene 1.960 3.075 Benzo(b)nafto(2,1-d)tiofena 51.128 74.846 Benzo(g,h,i)fluoranthene 1.042 1.661 Benzo(c)phenantrene 0.918 1.458 Benzo(a)antracene 1.724 2.345 Cyclopenta(c,d)pyrene <0.001 <0.001 Tripenilene/chrysene 34.376 44.763 Chrysene 12.186 15.577 Benzo(b)fluoranthene 18.500 20.668 Benzo(j)fluoranthene 1.482 2.577 Benzo(k)fluoranthene 2.764 3.321 Benzo(b + j + k)fluoranthene 22.746 26.566 Benzo(e)Pyrene 64.848 66.933 Benzo(a) pyrene 4.058 4.658 Perylene 0.994 3.321 Indeno (1,2,3-cd)pyrene 1.100 1.347 Dibenzo(a,h)antracene 1.328 0.637 Benzo (g,h,i)perylene 19.726 15.373 Antracene 1.174 1.207 Coronene 4.978 2.759 PAH* 251.668 299.718 EC** 106.890 116.716 PCA 28.8 25.9 Note: * PAH is the sum of all individual polyaromatic hydrocarbon compounds. ** EC is the sum of 8 types of individual polyaromatic hydrocarbon compound (8 Grimmer PAH) that are restricted according to European Legislation No. 2005/69/EC. ***Calculated from PAH of DAE Feed Mixture 1, which is a mixture of DAE Feed 1 and Diluent at ratio of 1:1.

[0031] For example, the amount of 8 Grimmer PAH content disclosed at Table 3 is 106,890 mg/kg. In the process of the present invention, it is found that TDAE product can be lowered to 10 mg/kg, including the Benzo(a) pyrene with the amount of less than 1 mg/kg.

Example 2

Preparation of the Mixture of Feeds

[0032] DAE Feed is mixed with a non polar aliphatic diluent with the chain of carbon from C5 to C8 and with ratio of diluent to the DAE Feed between 0.3 to 3.0. The process of feed mixing is executed at temperature of 25 to 70 C. The data on the density after the mixing process is shown at Table 4.

TABLE-US-00004 TABLES 4 The density of diluents. Carbon atom Type of Diluent Amount Density (kg/liter) n-pentane 5 0.63 isopentane 5 0.62 n-hexane 6 0.66 n-heptane 7 0.68 n-octane 8 0.70 isooctane 8 0.69 Note: DAE Feed Mixture 1 resulted from mixing DAE Feed 1 with n-hexane at a ratio of 1 resulted density of 0.81 kg/liter.

Example 3

Process of Liquid-Liquid Extraction

[0033] The process of liquid-liquid extraction to produce process oil is conducted using counter current method in an extraction column at temperature of 22 to 50 C.

[0034] From the result of liquid-liquid extraction process above, the yield of TDAE-1 and TDAE-2 products between 40 to 50% weight and 50% to 70% weight are obtained, respectively, as shown in Table 5 for the operation condition, Table 6 for chemical propertis , and Table 7 for physical properties.

TABLE-US-00005 TABLE 5 The operation conditions. TDAE-1 TDAE-2 Example Example Example Example Example Example Parameters 10 11 7 8 9 13 Flow of Mixture 10.80 10.80 15.80 15.80 15.80 16.80 of DAE Feed, kg/hour Flow of solvent, 20.00 20.00 15.00 10.00 15.00 8.00 kg/hour Flow of Mixture 6.17 6.26 11.80 12.70 11.67 14.51 of raffinate phase, kg/hour Flow of Mixture 24.62 24.37 19.20 13.00 19.12 10.52 of extract phase, kg/hour Ratio DAE 1:2 1:2 1:1 1:0.67 1:1 2:1 Mix/Furfural Temperature, C. 25 35 25 25 25 25 PCA , % weight 2.2 2.3 8.0 10.4 5.9 13.2 Yield, % weight 43.2 42.8 56.4 63.6 55.8 65.7 EC, mg/kg **** 0.001 0.014 Trace 0.017 0.003 0.273 BaP, mg/kg **** <0.001 <0.001 <0.001 0.005 <0.001 0.033 **** Result of TDAE Mixture (Raffinate) test.

TABLE-US-00006 TABLE 6 The chemical properties of TDAE products. TDAE Mix-1 TDAE Mix-2 Example Example Example Example Example Example Unit (mg/kg) 10 11 7 8 9 13 Phenantrene 0.016 0.082 0.012 0.015 0.017 0.102 Antracene 0.001 0.005 <0.001 <0.001 0.001 <0.001 Fluoranthene 0.002 0.0013 0.002 0.003 0.003 0.013 Pyrene 0.002 0.008 0.002 0.007 0.003 0.028 Benzo (b) nafto (2, 1-d) tiofene 0.001 0.004 0.010 0.038 0.007 0.484 Benzo (g, h, i) fluoranthene <0.001 <0.001 <0.001 0.004 0.001 0.046 Benzo (c) phenantrene <0.001 <0.001 <0.001 0.002 0.001 0.040 Benzo (a) antracene * <0.001 <0.001 <0.001 0.005 <0.001 0.026 Cyclopenta (c, d) pyrene <0.001 <0.001 <0.001 <0.001 <0.001 <0.001 Tripenilena/chrysene 0.001 0.005 <0.001 0.011 0.001 0.083 Chrysene * <0.001 0.002 <0.001 0.004 <0.001 0.024 Benzo (b) fluoranthene * <0.001 0.003 <0.001 <0.001 0.001 0.021 Benzo (j) fluoranthene * <0.001 <0.001 <0.001 <0.001 <0.001 0.040 Benzo (k) fluorantena * <0.001 <0.001 <0.001 <0.001 <0.001 0.035 Benzo (b + j + k) fluoranthene 0.003 <0.001 0.001 0.096 Benzo (e) Pyrene * 0.001 0.009 <0.001 0.003 0.002 0.094 Benzo (a) pyrene * <0.001 <0.001 <0.001 0.005 <0.001 0.033 Perylene <0.001 <0.001 <0.001 0.002 <0.001 0.011 Indeno (1, 2, 3-cd) pyrene <0.001 <0.001 <0.001 <0.001 <0.001 0.018 Dibenzo (a, h) Antracene * <0.001 <0.001 <0.001 <0.001 <0.001 <0.001 Benzo (g, h, i) perylene <0.001 0.004 <0.001 0.001 0.006 0.028 Antracene <0.001 <0.001 0.002 <0.001 <0.001 0.023 Coronene <0.001 0.003 0.004 <0.001 <0.001 0.017 PAH 0.026 0.004 0.101 0.025 0.135 1.142 EC * 0.01 0.014 0.017 0.003 0.273 Benzo (a) pyrene <0.001 <0.001 <0.001 0.005 <0.001 0.033 PCA 2.2 2.3 8.0 10.4 5.9 13.2

[0035] For example, Table 6 discloses the amount of 8 Grimmer PAH content is 0.001-0.273 mg/kg, which is considered far below the limit of PAH allowed by the European legislation (10 mg/kg), whereas it is found that the highest content of Benzo(a)pyrene is 0.033 mg/kg which is still below the allowable limit of the European Legislation (1 mg/kg). In some experiments of the present invention, it is found that TDAE product can fulfill the PAHs allowable limit of the European Legislation at the same time met the PCA limit of less than 3% weight. However, on other experiments the TDAE can meet the same PAH limit although the PCA content is higher than 3% weight, even as high as 13.2% weight. This fact will be very useful for the European Legislation that will limit the amount of 8 Grimmers PAH content substantially less than 10 mg/kg, where one of them is Benzo(a)pyrene at amount of less than 1 mg/kg. Besides it will be useful for the European Legislation, the present invention will give new benefits for rubber industry for providing TDAE product with better quality compared to other TDAE products, which is aromatic component content more than 25%, even can reach 30-35% by using ASTM D 2140-97 method.

TABLE-US-00007 TABLE 7 The physical analysis of TDAE products. No Parameter Method TDAE-1 TDAE-2 1 Specific gravity at 15.6/15.6 C. ASTM D1298 0.9661 0.9885 2 Kinematic viscosity at 100 C., cSt ASTM D445 16.58 19.73 3 Kinematic viscosity at 40 C., cSt ASTM D445 327.2 519.8 4 Refraction index at 20 C. ASTM D1218-02(07) 1.5379 1.5546 5 Viscosity Gravity Constant ASTM D2501-91 (05) 0.915 0.944 6 Sulphur % weight ASTM D4294-08a 3.75 4.35 7 Flash point, C. ASTM D92-05a 262 248 8 Aniline Point, C. ASTM D611-07 54.9 43.0 9 Carbon atom Type C.sub.A, % weight ASTM D2140 31.0 37 10 C.sub.N, % weight ASTM D2140 34.0 33 11 C.sub.P, % weight ASTM D2140 35.0 30 12 Polycyclic aromatics, % weight IP 346 2.7 8.0

Example 4

AMES Test on DAE Feed, TDAE-1 and TDAE-2

[0036] The mutagenity test was conducted using AMES Test based on OECD Guidelines for Testing of Chemicals No. 471 (1997). In this test Salmonella typhimurium TA 1535 was used as microbe material which was very sensitive to mutagenic compound. The number of colony which grew was an indicator of mutagenic activity of the PAH compound in the DAE Feed, TDAE-1 and TDAE-2, respectively. Based on the AMES Test as shown in Table 8, the following conclusions are drawn: [0037] 1. The bacteria colony in the DAE Feed grew four (4) times than that grew in the control (spontaneous reversion of the colony). This indicates that DAE Feed product can be classified as mutagenic or carcinogenic compound. [0038] 2. The number of bacteria colony in the TDAE-1 and TDAE-2 was similar to that in the control (spontaneous reversion of the colony). This indicates that TDAE-1 and TDAE-2 products can be classified as non-mutagenic or non-carcinogenic compound.

TABLE-US-00008 TABLE 8 The result of Mutagenic Test (Ames test). Average Number of Colony Koloni Without With No Type of Test S-9 Mix S-9 Mix 1 Spontaneous Reversion (Colony 330 430 Control) 2 Mutagenicity Test a. DAE Umpan (without dilution)* 1865 b. TDAE-1 (without dilution)* 324 351 c. TDAE-2 (without dilution)* 335 417 d. DMSO 314 377 3 Mutagenicity Test a. DAE Umpan (dilution 1:1) 495 529 b. TDAE-1 (dilution 1:1) 163 200 c. TDAE-2 (dilution 1:1) 155 217 4 Mutagenicity Test a. DAE Umpan (dilution 1:10) 378 427 b. TDAE-1 (dilution 1:10) 43 107 c. TDAE-2 (dilution 1:10) 17 91 5 Toxicity Test a. DAE Feed No Not b. TDAE-1 inhibitory Conducted c. TDAE-2 zone (no d. DMSO toxic to microorganism tested) Too many colonies were present so that it was uncountable. [0039] The table below indicate the level of PCA, B(a)P and PAH contained in the respective product as mentioned above:

TABLE-US-00009 PCA B(a)P 8 Grimmer PAH % weight mg/kg mg/kg a. DAE feed (without 28.8% 4,058 106,890 dilution) b. TDAE-1 (without dilution) 2.2% <0.001 0.001 c. TDAE-2 (without dilution) 8% <0.001 trace
<Term and Definition Used in the Specification of this Application>

[0040] In the specification of this application, Liquid-liquid extraction is a technological process which based on method of operation of mass transfer to a feed that is contacted with a solvent for extracting dissolvable substances (solute) from feed materials. Feed materials, which consist of carrier and solute must have a property, that is, cannot be mixed (immiscible) or can be mixed partially (miscible) with the solvent, so that only solute that have higher solvability than the diluents can move into the solvent.

[0041] Diluent is an alkane compound that used to lower the density of feed materials.

[0042] Extractor is a type of agitation column extractor used in the experiments of the present invention, hereinafter referred to as extractor. The main part of this extractor is a turbine agitator which can be operated on the hydrodynamic conditions and serves as a stirrer to generate droplets spread.

[0043] PCA or Polycyclic Aromatic, is organic compound that consist of 3 or more rings of aromatic compound with or without branch chain, where in the PCA are contained PAH (Polycyclic Aromatic Hydrocarbon) compound and organic compound that contain hetero-atom like Nitrogen (N), Sulphur (S) and Oxygen (O). Not all compound that grouped as PAH have the property of carcinogenic.

[0044] PAH or Polycyclic Aromatic Hydrocarbon is chemical compound that consist of aromatic ring bonding and does not contain hetero-atom or other substituent, consist of carbon and hydrogen molecules. There are 23 types individual PAH compounds in DAE Feed where 8 types of them stated as carcinogenic substances or called 8 Grimmer PAH.

[0045] Process Oil is oil which is rich in aromatic compound, used as solvent in the tire making or may also be used as a solvent at the printing ink industry.

[0046] IP 346 is the standard method to determine PCA in lubricating oil or petroleum fraction that does not contain asphaltene.

[0047] While the present invention is described related to the embodiments as illustrated herein after, as well as the accompanied drawing, it has to be understood that they are not intended to represent the only form of the invention in regard to the details of the process and manner of operation. In fact, it will be evident to one skill in the art that modifications and variations may be made without departing from the spirit and the scope of the invention. Although specific terms have been employed, they are intended in a generic and descriptive sense only and not for the purpose of limitation.