The present invention relates to an eccentric polymer pipe, suitable for transporting fluids, particularly for transporting pressurized fluids. The present invention also relates to a process for producing an eccentric polymer pipe.

BACKGROUND OF THE INVENTION

Polymer pipes such as polyoiefin pipes are inter alia used to transport fluids. The fluid inside the pipe creates internal pressure which leads to hoop stress on the pipe wall. Therefore the pipe has to be designed to withstand the occurring hoop stress. Moreover, the transported fluid may have varying temperatures, usually within the temperature range from about 0 °C to about 50 °C. Such pressure pipes maybe made of polyoiefin plastics such as medium density polyethylene (MDPE; density: 0.930- 0.942 g/cm ³ ), high density polyethylene (HOPE; density: 0.945-0.965 g em ⁵ ) and polypropylene (PP; density: 0.890-0.915 g/cm ³ ). By the expression "pressure pipe" herein is meant a pi e which, when used, is subjected to a posit ive pressure, i.e. the pressure inside the pipe is higher than the pressure outside the pipe.

Polymer pipes are general ly manufactured by extrusion, or to a smal ler extent, by in ject ion moulding. The properties of such conventional poly mer pipes produced by extrusion or injection moulding are sufficient for many purposes, although enhanced properties may be desired, for instance in applications requiring high pressure resistance, i.e. pipes that are subjected to an internal fluid pressure for a long and/or short period of time. When considering that the fluids, such as tap water or natural gas, transported in a pipe often are pressurized and have varying temperatures, usual ly within a range of 0 °C to 50 °C, it is obvious that the pipes must meet demanding requirements.

Especially resistance to internal pressure (also denoted hydrostatic pressure), i.e. resistance against circumferential load is of importance.

Resistance to internal pressure of a polymer material depends on many

morphological properties, such as density, crystal I inity, co-monomer type, co- monomer content, mo lecular weight and mo lecular weight distribut ion and modal ity.

Effects of these material properties to resistance to hydrostatic pressure of plastic pipes are wel l known in the l iterature and in the industry.

However, the resistance to internal pressure can still be improved. It has now been discovered that resistance to internal pressure can be improved in case the pipe has an eccentric shape/dimensions.

Therefore, the present invention prov ides a polymer pipe hav ing a relat ive eccentricity of at least 0.03, whereby the relat ive eccentricity (e _r ) is defined as follows

(I)

+ S„

wherein

S ';max is the ma imum wal l thickness of the pipe; and

'min is the minimum wall thickness of the pipe.

The relat ive eccentricity (e _r ) is calculated as fol lows.

wherein

E is the eccentricity o f the pipe

is the average wail thickness of the pipe

The eccentricity (E) is calculated as follows

S, max min

(Ill)

2

Smax and Smin are as defined for formula (I) above. The average wall thickness of the pipe is calculated as follows. wherein

S _av is the average wall thickness of the pipe; and

Smax and Smin are as defined for formula (I) above.

By combining equations (II) to (IV) equation (I) results.

It has been surprisingly found that in case the pipe has an eccentricity of at least 0.03 the resistance against internal pressure is significantly improved compared with a pipe having a concentric wail thickness made from the same material under otherwise identical conditions. Hence, using the same material a pipe having higher stability can be formed. Moreover, the inner circumference (diameter) of the pipe according to the present invention remains the same compared with a corresponding concentric pipe, i.e. the flow capacity is the same. Furthermore, the outer circumference (diameter) is also the same compared with a corresponding concentric pipe. Thus, the same pipe processing equipment as for concentric pipes can be used, i.e. no investments for additional equipment is needed. It only needs to be ensured that the pipes are welded together such that the inner contours of two consecutive pipes which are welded together are congruent. However, this can be easily accomplished by providing appropriate markings on the pipe.

XRD measurements were carried out on the pipes according to the present invention whereupon we found that in the eccentric pipes according to the invention the circumferential orientation of the polymer molecules is far greater compared with a comparable pipe having even wall thickness.

In conventional pipe processing, axial orientation exist due to the processing nature, giving improved mechanical properties in longitudinal direction, like tensile and Charpy properties. Currently no circumferential orientation due to the standard processing means has been reported. Earlier studies and processing equipments designed to obtain circumferential orientation on the final pipe product in order to increase the resistance to hydrostatic pressure of plastic pipes. These studies cover either rotating die/mandrel, sets to have circumferent ial surface orientation

(US 3,404,203, CN 101 337 425 ) or a post processing step for circumferential orientation by enlarging the diameter of a pipe with a compl icated process (Biaxially oriented polypropylene pipes: implications for impact and hydrostatic pressure resistance, Plastics, Rubber and Composites, Volume 35 Issue 10 (01 December 2006), pp. 447-454 ). Hence, exist ing methods are cumbersome and require specific equipment and/or addit ional process steps leading to higher costs.

To further invest igate the how the increased circumferential orientation may occur heat transfer simulat ions were carried out (cf. experimental part for details). It has been found that the thinner part of the pipe is colder and, thus, the crystallisation is initiated there. The crystallisation then seems to propagate from the thinnest part to the thickest part around the pipe leading to higher circumferential orientation of the pipe. This improved circumferential orientation seems to compensate for the local lower thickness of the pipe which would usual ly be expected to be a weak spot. Thus, with the same polymer material pipes hav ing improved internal pressure resistance can be formed.

In the present invention the term "fluid" includes both the liquid and gases.

The polymer pipe is having a relat ive eccentricity of at least 0.03, preferably at least 0. 10, even more preferably at least 0. 14 and most preferably at least 0.2. The relat ive eccentricity is usually not higher than 0.30, preferably not h igher than 0.25.

Usually and preferably the pipe has the same eccentricity along its length.

The pipe may be a linear pipe. "Linear pipe" denotes that the pipe has a linear flow direction along its length. The pipe may alternat ively be bent, e.g. may have a hel ical structure, such as a spring. As in case of a bent pipe a definit ion of the eccentricity based on the pipe as a whole is geometrically not feasible in the following it is referred to the cross-sect ions of the pipe perpendicular to the flow direct ion.

Usual ly the outer circum ference and/or the inner circumference of each cross-section of the pipe, the cross-section being perpendicular to the flow direction of the pipe are circular. In the present invention "circular" with regard to the outer circumference denotes that the deviation from perfect circularity of the outer circumference (Dev(out)) calculated as follows

O! OD

Dev(out) mm

OD m, _m ax + OD mm.

2

with

OD _max being the maximum outer diameter of the pipe

OD _mm being the minimum outer diameter of the pipe

is less than 10.0 %, preferably less than 8.0%.

OD _max and OD _mm are determined as specified in IS04427-2.

Preferably the deviat ion from perfect circularity (Dev(out)) and the average outer diameter OD of the pipe calculated as follows

<9/ > , + OIX

OD 'mill

2

with OD _max and OD _mm are as defined above

fulfil the following relat ionship

with Dev(out ) given in %.

More preferably

0D x Dev( out ) < 50 and most preferably

In the present invention "circular" with regard to the inner circumference denotes that the deviation from perfect circularity of the inner circumference (Dev(in)) calculated as follows

Dev(i«) = _/g - _+fl) - ma min

2

with

ID _max being the maximum inner diameter of the pipe

ID _m i _n being the minimum inner diameter of the pipe

is less than 10.0 %, preferably less than 8.0%.

ID _max and ID _mm are determined analogous to the procedures as specified in IS04427- 2.

Preferably the deviation from perfect circularity (Dev(in)) and the average

diameter ID of the pi e calculated as follows

ID +ID

ID max min with ID _max and ID _mm are as defined above

fulfil the following relationship

415 X Deviin) < 70

ith Dev(in) given in %.

More preferably

«J7D X Deviin) < 50 and most preferably

Usually the ma imum wall thickness of the pipe and the minimum wall thickness of the pipe are determined on the same cross-section of the pipe, the cross-section being perpendicular to the flow direction of the pipe. Usually each of these cross-sections meet the requirements of the present invention. Preferably, said cross-section is identical along the entire length of the pipe.

The polymer pipe preferably has an outer diameter of at least 20 mm, more

preferably of at least 25 mm and most preferably of at least 32 mm. Usually the outer diameter of the pipe according to invention is not more than 260 mm, preferably not more than 170 mm and most preferably not more than 120 mm.

The average wall thickness of the pipe (S _av ) is preferably between 2.0 mm and 12, more preferably between 2.0 mm and 8.0 mm and most preferably from 2.0 mm to 5.0 mm.

As already outl ined above, with the above eccentricit ies the performance of the obtained pipe in the hoop stress test according to ISO 1 167 is significantly improved compared with a concentric pipe made from the ident ical material under otherwise identical conditions.

In one embodiment the pipe has an eccentricity (E) of at least 0.13, an outer diameter of 32 mm and an average wall thickness (s _av ) of 3.2 mm.

Preferably the polymer pipe is having a failure time of at least 200 hours in the test according to ISO 1 1 7 determined at 5.7 MPa and 80 C, more preferably at least 250 hours in the test according to ISO 1 1 67 determined at 5.7 Pa and 80°C, even more preferably at least 450 hours in the test according to ISO 1 167 determined at 5.7 MPa and 80°C. In a preferred embodiment the failure time in the test according to ISO 1 167 determined at 5.7 MPa and 80°C is at least 4000 hours. In a particular preferred embodiment the failure time in the test according to ISO 1 167 determined at 5.7 Pa and 80°C is at least 6000 hours.

Preferably the polymer pipe is having a failure t ime of at least 1 00 hours in the test according to ISO 1 167 determined at 5.9 Pa and 80 C, more preferably at least 1000 hours in the test according to ISO 1 167 determined at 5.9 MPa and 80 C. In a preferred embodiment the failure time in the test according to ISO 1 167 determined at 5.9 MPa and 80°C is at least 2000 hours.

Preferably the polymer pipe is having a failure time of at least 10 hours in the test according to ISO 1 167 determined at 6.1 MPa and 80°C, more preferably at least 150 hours in the test according to ISO 1 167 determined at 6.1 MPa and 80°C. In a preferred embodiment the failure time in the test according to ISO 1 167 determined at 6.1 MPa and 80°C is at least 700 hours.

Preferably, the time until failure of the pipe according to the present invention in the test according to ISO 1 167 at a pressure ranging from 5.4 to 6.1 MPa is at least 1.5 times higher compared with the time until failure of a pipe at the same pressure having a constant wail thickness identical to the average wail thickness S _av of the pipe according to the present invention, having the same inner and outer contours, made from the same polymer composition under the same conditions, more preferably, the time until failure of the pipe according to the present invention in the hoop stress test according to ISO 1 167 at a pressure ranging from 5.4 to 6.1 MPa is at least 2.0 times higher compared with the time until failure of a pipe at the same pressure having a constant wail thickness identical to the average wail thickness S _av of the pipe according to the present invention, having the same inner and outer contours, made from the same polymer composition under the same conditions, even more preferably, the time until failure of the pipe according to the present invention in the hoop stress test according to ISO 1 167 at a pressure ranging from 5.4 to 6.1 MPa is at least 3.0 times higher compared with the time until failure of a pipe at the same pressure having a constant wall thickness identical to the average wail thickness S _av of the pipe according to the present invention, having the same inner and outer contours, made from the same polymer composition under the same conditions.

Usually the failure time in a hoop stress test according to ISO 1 167 at a pressure ranging from 5.4 to 6.1 MPa is not more than 450 times higher compared to a concentric pipe having the same inner and outer diameter, made from the same polymer composition under the same conditions.

The polymer pipe maybe a polyolefin pi e such as a polyethylene pipe or a polypropylene pipe, e.g. made from a material having a σΙ.Ρ1, value of at least 10 a (predicted long term hydrostatic strength) according to ISO 9080.

Preferably, the polymer pipe consists of a polymer composit ion, the polymer composition having a viscosity at a shear stress of 747 Pa (r)747p _a ) of at least

650 kPa s. The method for determining the v iscosity at a shear stress of 747 Pa (j|747Pa) is described in the experimental part.

The polymer pi e preferably has a polymer content of at least 70 wt.% based on the pipe, more preferably at least 80 wt.%, even more preferably at least 90 wt.% and most preferably at least 95 wt.% based on the pipe.

The poly mer pipe is preferably a polyolefin pipe, more preferably the poiyoiefin pipe consists of a polyolefin composit ion, the polyolefin composition comprising

an ethylene homo- or copolymer (A) and/or

a propylene homo- or copolymer (B),

preferably

an ethylene homo- or copolymer (A) or

a propylene homo- or copolymer (B);

optional ly, carbon black; and

optionally, convent ional addit ives.

The total amount of ethylene homo- or copolymer (A) and propylene homo- or copolymer (B) is preferably at least 70 wt.% based on the total polyolefin composit ion, more preferably at least 80 wt.%, even more preferably at least 90 wt.% and most preferably at least 95 wt.% based on the total poiyoiefin composition. The ethylene homo- or copolymer (A) preferably has a density of from 0.930 g/cm ³ to 0.965 g/cm ³ , more preferably of 0.940 g/cm ³ to 0.965 g/cm ³ and most preferably 0.950 g/cm ³ to 0.960 g/cm ³ .

Ethylene homo- or copolymer (A) preferably has a viscosity at a shear stress of 747 Pa (Y|747Pa) of at least 650 kPa -s. The method for determining the viscosity at a shear stress of 747 Pa (r)747Pa) is described in the experimental part.

Ethylene homo- or copolymer (A) preferably has a melt flow rate MFR ₅ , determined according to ISO 1 133 at 190°C and under a load of 5.00 kg, of 0.05 to 2.0 g/10 min, more preferably 0. 1 to 1 .0 g/10 min and most preferably 0. 1 5 to 0.8 g 10 min.

The ethylene homo- or copolymer (A) is preferably an ethylene copolymer hav ing a comonomer content of 0. 1 to 2.0 mol%, more preferably 0. 1 to 1 .0 mol% based on the total weight of component (A).

As comonomers C ₄ to C20 alpha-o!efins are preferred, more preferred are C ₄ to C$ alpha-olefins, such as 1 -butene. 1 -hexene, 4-methyl- 1 -pentene and 1 -octene.

Ethylene homo- or copolymer (A) preferably comprises, more preferably consists of. i) a low molecular weight ethylene homopolymer or -copolymer and

ii) a high molecular weight ethylene homopolymer or -copolymer.

Preferably the weight ratio between i) and ii) is (35-55 ):(65-45 ), more preferably (43-5 1 ):(57-49) and most preferably (44-50):(56-50 ).

Usually, ethylene homo- or copolymer (A) is comprising at least two polyethylene fractions, which have been produced under different polymerisation conditions result ing in different (weight average) molecular weights and molecular weight distributions for the fractions. Such a polymer is usually referred to as "mult imodal". Accordingly, in this sense the ethylene homo- or copolymer (A) of the invent ion is a multimodal polyethylene. The prefix "muit i" relates to the number of different polymer fractions the ethylene homo- or copolymer (A) is consist ing of. Thus, in case ethylene homo- or copolymer (A) is consisting of two fractions only is called "bimodal".

The form of the molecular weight distribut ion curve, i.e. the appearance of the graph of the polymer weight fract ion as function of its molecular weight, of such a multimodal polyethylene will show two or more maxima or at least be dist inct ly broadened in comparison with the curves for the individual fractions. For example, if a polymer, such as ethylene homo- or copolymer (A), is produced in a sequential multistage process, utilising reactors coupled in series and using different conditions in each reactor, the polymer fractions produced in the different reactors will each have their own molecular weight distribut ion and weight average molecular w eight. When the molecular weight distribution curve of such a polymer is recorded, the indiv idual curves from these fractions are superimposed into the molecular weight distribution curve for the total result ing polymer product, usually yielding a curve with two or more dist inct maxima.

Ethylene homo- or copolymer (A) is preferably produced in a mult istage process wherein e.g. fract ions (i) and (ii) are produced in subsequent stages. In such a case, the properties of the fractions produced in the second step (or further steps) of the mult istage process can either be inferred from polymers, which are separately produced in a single stage by applying identical polymerisation condit ions (e.g. identical temperature, partial pressures of the reactants diluents, suspension medium, reaction time) with regard to the stage of the mult istage process in which the fract ion is produced, and by using a catalyst on which no prev iously produced polymer is present. Alternat ively, the properties of the fract ions produced in a higher stage of the mult istage process may also be calculated, e.g. in accordance with B. i lagstrom. Conference on Polymer Processing (The Polymer Processing Society), Extended Abstracts and Final Programme. Gothenburg. August 19 to 2 1 , 1997, 4: 13.

Thus, although not directly measurable on the multistage process products, the properties of the fractions produced in higher stages of such a mult istage process are usually be determined by applying either or both of the above methods. In the present invent ion the values are usually calculated in accordance w ith B. Hagstrom.

For example, WO 00/01765 and WO 00/22040 describe hi- or mult imodal polyethylenes usable in the present invent ion.

Preferably the ethylene homo- or copolymer (A) is mult imodal, more preferably bimodal. ln case ethylene homo- or copolymer (A) is comprising or consisting of fractions i) and ii), preferably fraction i) is a homo polymer and fraction ii) is a copolymer. In case fraction ii) is an ethylene copolymer, preferably fraction ii) is an ethylene copolymer comprising 0. 1 to 2.0 mol% comonomer, even more preferably 0. 1 to 1 .0 mol% comonomer. The comonomer is preferably selected from alpha-olefins having 4 to 20 carbon atoms, more preferably 4 to 8 carbon atoms, such as 1-butene, 1 - hexene, 4-methyi- 1 -pentene and 1 -oetene.

The propylene homo- or copolymer (B) preferably has a density of from 0.890 g/cm ³ to 0.915 g/cm ³ , more preferably of 0.895 g/cm ³ to 0.91 5 g/cm ³ and most preferably 0.900 g/cm' to 0.91 0 g/cm '.

Preferably the propylene homo- or copolymer (B) has a melt flow rate MFR, determined according to ISO 1 133 at 230°C and under a load of 2. 16 kg, of 0.05 to 2.0 g 1 0 min, more preferably 0. 1 to 1 .0 g 10 min and most preferably 0. 1 5 to 0.7 g/10 min.

The propylene homo- or copolymer (B) is preferably a propylene homo- or random copolymer.

A propylene random copolymer denotes a copolymer of propylene monomer units and comonomer units in which the comonomer units are randomly distributed in the polymeric chain. Thereby, a propylene random copolymer includes a fraction, which is insoluble in xylene xylene cold insoluble (XCU) fract ion , in an amount of at least 70 wt%, more preferably of at least 80 wt%, still more preferably of at least 85 wt% and most preferably of at least 90 wt%, based on the total amount of the propylene random copolymer.

The random copolymer does not comprise an eiastomeric phase dispersed therein. As known for skilled person, random copolymer is different from heterophasic polypropylene which is a propylene copolymer comprising a propylene homo or random copolymer matrix component (1) and an eiastomeric copolymer component (2) of propylene with one or more of ethylene and O-Cs alp a-olefin copolymers. wherein the elastomeric (amorphous) copolymer component (2) is dispersed in said propylene homo or random copolymer matrix polymer (1).

Usually, a propylene polymer comprising at least two propylene polymer fractions (components), which have been produced under different polymerisation conditions resulting in different (weight average) molecular weights and/or different

comonomer contents for the fract ions, preferably produced by polymerizing in multiple polymerization stages with different polymerization condit ions, is referred to as "multimodal". The prefix "mult i" relates to the number of different polymer fractions the propylene polymer is consist ing of. As an exam le of mult imodal polypropylene, a propylene polymer consisting of two fractions only is called

"bi modal", whereas a propylene polymer consisting of three fractions only is called "trimodal".

Thereby the term "different" means that the propylene polymer fractions differ from each other in at least one property, preferably in the weight average molecular weight or comonomer content or both, more preferably at least in the weight average molecular weight.

The form of the molecular weight distribut ion curve, i.e. the appearance of the graph of the polymer weight fract ion as funct ion of its molecular weight, of such a multimodal propylene polymer is at least distinctly broadened in comparison with the curves for the individual fract ions.

The propylene random copolymer used in the present invention is preferably a multimodal propylene random copolymer, more preferably a bi modal propylene random copoly mer. Preferably, the propylene random copoly mer consists of the two propylene copolymer fract ions with the proviso that at least one of the two fractions, preferably both fract ions are propylene random copolymer fract ions.

A propylene homo polymer thereby denotes a polymer consist ing essent ially of propylene monomer units. Due to the requirements of large- scale polymerizat ion it may be possible that the propylene ho mo polyme includes minor amounts of comonomer units, which usual ly is below 0. 1 mol%, preferably below 0.05 mol%, most preferably below 0.01 mol% of the propylene homopolymer.

The propylene random copolymer used in the polypropylene composition of the invent ion comprises at least one comonomer selected from alpha- olefins with 2 or 4 to 8 carbon atoms.

The propylene random copolymer may comprise only one type of comonomers or two or more types of comonomers.

The comonomers of said propylene random copolymer are preferably selected from C > and C ₄ to C<, a!pha-olefins. A particular preferred comonomer is ethylene.

Especial ly suitable for the polypropylene composit ion of the present invent ion is a propylene random copolymer which is a propylene random copolymer with ethylene comonomer.

It is preferred that the propylene random copolymer, which is preferably the propylene copolymer with ethylene comonomer, comprises at least a propylene random copolymer hav ing a low molecular weight (low molecular weight (LMW) fraction ) and a propylene random copolymer hav ing a high molecular weight (high molecular weight (HMW) fract ion ). Thereby, the LMW fract ion has a lower weight average molecular weight than the HMW fract ion.

It is wel l known that melt flow rate (MFR) of a polymer is an indicat ion of the weight average molecular weight ( Mw ) of the polymer, the higher the MFR the lower the Mw of the polymer and, respectively, the lower the MFR the higher the Mw of the polymer. Accordingly, the MFR of the low molecular weight fract ion is higher than the MFR of the high molecular weight fraction. The low molecular weight fract ion has preferably a MFR ₂ of from 0.2 to 3.0 g/ 10 min, more preferably a MFR ₂ from 0.25 to 2.0 g/10 min, more preferably from 0.3 to 2.0 g/10 min and most preferably of 0.35 to 2.0 g 10 min. Preferably both the low molecular weight fract ion and the high molecular weight fract ion arc propylene random copolymer fractions which may have essent ially the same or different comonomer content. It is preferred that the comonomer content of the high molecular weight fraction is equal to or higher than, preferably higher than the comonomer content of the low molecular weight fract ion.

The comonomer content of the low molecular weight fract ion is usually in the range of 1 .0 to 6.0 mol%, preferably 2.0 to 5.5 mol%, more preferably 3.0 to 5.0 mol%, most preferably 3.5 to 4.5 mol%, based on the total content of monomer units in the low molecular weight fract ion.

The comonomer content of the high molecular weight fract ion is usually in the range of 5.5 to 12 mol%, preferably 6.0 to 1 1 .0 mol%, more preferably 6.5 to 1 0.0 mol%%, still more preferably 7.0 to 9.0 mol%, most preferably 7.5 to 8.5 mol%, based on the total content of monomer units in the high molecular weight fraction .

In a preferred embodiment, the propylene random copolymer is a propylene random copolymer with ethylene comonomer comprising at least a propylene random copolymer hav ing a low molecular weight ( low molecular weight (LMW) fraction ) and a propylene random copolymer hav ing a high molecular weight (high molecular weight (HMW) fract ion ) and a higher content of comonomer, preferably ethylene comonomer, than the low molecular weight fract ion (LMW fraction ). In this preferred embodiment the content of the comonomer, preferably ethylene

comonomer in the LMW fraction, is within the preferred ranges as defined above. The comonomer content of the propylene random copolymer is usually in the range of 4.5 to 9.5 mol%, preferably 5.0 to 9.0 mol%, more preferably 5.5 to 8.0 mol%, still more preferably 5.5 to 7.5 mol%, most preferably 5.7 to 7.0 mol%, based on the total content of monomer units in the propylene random copolymer. The low molecular weight fraction and the high molecular weight fract ion may include the same type of comonomer or different types of comonomers. It is preferred that both fractions include the same type of comonomer.

The low molecular weight fract ion is preferably present in the propylene random copolymer in an amount of 30 to 50 wt%, more preferably in an amount of 35 to 47 wt% and most preferably in an amount of 37 to 47 wt%, based on the total amount of the propylene random copolymer ( 1 00 wt%), preferably, and the high molecular weight fract ion is preferably present in the propylene random copolymer in an amount of 70 to 50 wt%, more preferably in an amount of 65 to 53 wt% and most preferably in an amount of 63 to 5 wt%, based on the total amount of the propylene random copolymer (100wt%).

The propylene random copolymer preferably has a density of 890 to 910 kg/m ³ , preferably 895 to 905 kg/m ³ .

It is preferred that the propylene random copolymer consists of the propylene random copolymer having a low molecular weight ( low molecular weight (LMW) fraction ), the propylene random copolymer having a high molecular weight (high molecular weight (HMW) fract ion ).

The mult imodal propylene random copolymer may further comprise a prepolymer fraction. In case of the presence of a prepolymer fraction, said fract ion is calculated to the amount (wt%) of the low molecular weight fraction or high molecular weight fraction, preferably to the amount of low molecular weight fraction. The prepolymer fraction can be propylene homo polymer or copolymer.

For example, WO 2014/173530 describes polypropylenes usable in the present invent ion.

The polymer pipe, preferably, the preferred polyolefin composit ion the pipe is consist ing of, preferably comprises carbon black. I f present, the carbon black is preferably present in amount of 0. 1 0 to 10 wt.% carbon black based on the total weight of the polymer pipe, preferably, the preferred polyolefin composit ion the pipe is consist ing of, more preferably 0.50 to 5.0 wt.% carbon black based on the total weight of the polymer pipe, preferably, the preferred polyolefin composit ion the pipe is consist ing of and most preferably 0.75 to 3.5 wt.% carbon black based on the total weight of the polymer pipe polymer pipe, preferably, based on the preferred polyolefin composit ion the pipe is consist ing of. Thc polyolefin composition preferably has a density of from 0.890 g/cm ³ to 0.970 g em'.

In case the polyolefin composition comprises an ethylene homo- or copolymer (A), optional ly addit ional ly comprising carbon black and 'or conventional additives in the amounts according to the present invention, the polyolefin composit ion preferably has a density of from 0.935 g/cm ³ to 0.970 g/cm ³ , more preferably of 0.945 g/cm ³ to 0.970 g/cm ³ and most preferably 0.955 g/cm ³ to 0.965 g/cm ³ .

in case the polyolefin composit ion comprises an ethylene homo- or copolymer (A), optional ly addit ionally comprising carbon black and/or convent ional addit ives in the amounts according to the present inv ention, the polyolefin composit ion preferably has a melt flow rate MF ₅ , determined according to ISO 1 133 at 190°C and under a load of 5.00 kg, of 0.05 to 2.0 g 10 min, more preferably 0. 1 to 1 .0 g 10 min and most preferably 0. 1 5 to 0.8 g 10 min.

In case the polyolefin composit ion comprises an a propylene homo- or copolymer (B), optionally additional ly comprising carbon black and/or conv entional additiv es in the amounts according to the present inv ent ion, the polyolefin composit ion preferably has a density of from 0.890 g/cm ³ to 0.91 5 g/cm ³ , more preferably of 0.895 g/cm ³ to 0.91 5 g/cm ³ and most preferably 0.900 g/cm ³ to 0.91 0 g/cm ³ .

In case the polyolefin composit ion comprises an a propylene homo- or copolymer (B), optionally additional ly comprising carbon black and/or conventional addit ives in the amounts according to the present inv ent ion, the polyolefin composit ion preferably has a melt flow rate MFR, determined according to ISO 1 133 at 230°C and under a load of 2.16 kg, of 0.05 to 2.0 g/10 min, more preferably 0. 1 to 1 .0 g/ 10 min and most preferably 0. 1 5 to 0.7 g/10 min.

In case the polyolefin composition comprises an a propylene homo- or copolymer

(B), optionally addit ional ly comprising carbon black and/or conv ent ional addit ives in the amounts according to the present invent ion, the polyolefin composit ion preferably has a content of xylene cold solubles (XCS ) of from 1 .0 to 1 5.0 wt%, preferably of from 2.0 to 12.0 wt%, more preferably of from 4.0 to 1 0.0 wt%, determined at 25°C according to ISO 16152.

The material the polymer pipe is consisting of, preferably, the preferred polyolefin composit ion the pipe is consisting o opt ional ly addit ional ly comprising carbon black and/or convent ional addit ives in the amounts according to the present invention, preferably has a viscosity at a shear stress of 747 Pa (η 747 a) of at least 650 kPa-s.

The polymer pipe, preferably, the preferred polyolefin composit ion the pipe is consisting of. according to the present invent ion usually comprises convent ional additives for utilization with polyoiefins different from carbon black, such as pigments, stabilizers (ant ioxidant agents), antacids and/or anti-UVs, antistatic agents, clarifiers, brighteners and utilization agents (such as processing aid agents) preferably, the amount of these additives is 10 wt.% or below based on the total amount of the polymer pipe, preferably, the preferred polyolefin composit ion the pipe is consist ing of, further preferred 8 wt.% or below, still more preferred 4 wt.% or below of the polymer pipe, preferably, the preferred polyolefin composit ion the pipe is consist ing of. Such addit ives are general ly commercial ly available and arc described, for example, in "Plastics Addit ives handbook", 5 ^th edition, 201 1 of Hans Zweifel. The conventional additives are usually present in an amount of at least 0.1 wt.% based on the total amount of the polymer pipe, preferably, the based on preferred polyolefin composit ion the pipe is consisting of. Usually, the convent ional addit ives are present in an amount of not more than 1.0 wt.%, preferably not more than 0.70 wt.%.

It is preferred that the polymer pipe, preferably, the preferred polyolefin composit ion the pi e is consist ing of, does not comprise a polymeric nucleat ing agent that is added on purpose to funct ion as a nucleat ing agent. More preferably, the polymer pipe, preferably, the preferred polyolefin composition the pipe is consist ing of, does not comprise (i.e. is void of) a polymeric nucleating agent, selected from a polymerized vinyl com ound according to the fol lowing formula

CH ₂ =CH CH R ' R-'

wherein

R ¹ and R ^' together form a 5- or 6-membered saturated, unsaturated or aromatic ring, optional ly containing substituents, or independent ly represent an a Iky I group comprising 1 to 4 carbon atoms, whereby in case R ¹ and R form an aromat ic ring, the hydrogen atom of the CHR' R moiety is not present, for example vinyl cyclohexanc (VCH) polymer.

Conventional addit ives and carbon black arc often not added in pure form as the handling of powders, especially carbon black powders, requires addit ional safety precautions. Therefore, additives and carbon black are often added as so-called masterbatches, i.e. are dispersed in a polymer in high concentration. Said

masterbatches are then combined with the polymer the additive should be added to. Thus, the pipe and the polyolefin. composit ion the pipe is preferably consist ing of may comprise additional polymers besides component (A) and/or (B), including, preferably consist ing of, the polymers added as masterbatches, if any, besides component (A) and/or (B) in an amount of not more than 1 0 wt.% based on the pipe, preferably not more than 5 wt.% based on the pi e.

Preferably the polyolefin composition consists of

- the ethylene homo- or copolymer (A) and/or

the propylene homo- or copolymer ( B),

preferably

the ethy lene homo- or copolymer (A) or

the propylene homo- or copolymer (B);

- convent ional addit ives in the amounts according to the present invent ion; optional ly carbon black in the amounts according to the present invent ion ; optionally addit ional polymers besides components (A) and/or (B) in the amounts according to the present invent ion. In an even more preferred embodiment the polyolefin composition consists of the ethylene homo- or copolymer (A) and/or

the propylene homo- or copolymer (B),

preferably

the ethylene homo- or copolymer (A) or

the propylene homo- or copolymer (B)

convent ional addit ives in the amounts according to the present inv ent ion; carbon black in the amounts according to the present inv ention;

optionally and preferably addit ional polymers besides component (A) and/or (B) in the amounts according to the present invent ion.

The present invention is furthermore directed to a process for producing a pipe according to the present inv ent ion.

The process preferably comprised the following steps:

i. ) providing a molten polymer composit ion, preferably the preferred polyolefin composit ion;

ii. ) melt extruding the molten polymer composit ion, preferably the preferred polyolefin composit ion, through a mandrel and die set;

iii. ) cooling the molten polymer composit ion, preferably the preferred polyolefin composit ion, after exit ing the mandrel and die set

whereby the die and the mandrel are adjusted such that to lead a pipe having relat ive eccentricity of at least 0.03.

The relat iv e eccentricity of the pipe is determined as defined abov e and below. In order to produce the eccentric pipe of the inv ention the mandrel and 'or the die of the mandrel and die set used to produce a concentric pipe is adjusted and the eccentricity of the pipe is determined. The necessary adjustments depend on the desired diameter and wal l thickness of the pipe but can be figured out within a few experiments. Usually either the mandrel or the die of the mandrel and die set used to produce a concentric pipe is adjusted and the eccentricity of the pipe is determined. The preferred features of the pipe according to the present invention are also preferred features of the process according to the present invention and vice versa. The present invention is furthermore directed to the use of the polymer pipe according to the invention for the transport of pressurized fluids.

The preferred features of the pipe and process according to the present invention are also preferred features of the use according to the present invention and vice versa

Considering the above the invent ion is especial ly directed to the following embodiments:

[ 1 ] A polymer pipe having a relat ive eccentricity of at least 0.03, whereby the relative eccentricity (e _r ) is defined as follows

g S max S min ^j^

^max + ^min

wherein

Smax is the maximum wall thickness of the pipe; and

Smin is the minimum wall thickness of the pipe.

[2] The polymer pipe according to paragraph [ 1 ] having a relat ive eccentricity of at least 0.05.

[3] The polymer pipe according to paragraph [ 1 ] or [ 2] having a relat ive eccentricity of not more than 0.30.

[4] The polymer pipe according to any one of the paragraphs [ 1 ] to [3] which is a polyolefin pipe.

[ 5 ] The polyolefin. pi e according to paragraph [4], wherein the po I vole fin pipe consists of a polyolefin composition, the polyolefin composition comprising

- an ethylene homo- or copolymer (A) and/or a propylene homo- or copolymer (B).

[6] The polyolefin pi e according to paragraph [ 5], wherein the ethylene homo- or copolymer (A) has a density of from 0.930 g/cm ³ to 0.965 g/cm ³ .

[ 7] The polyolefin pipe according to any one of the the paragraphs [4] to [6], wherein the polyolefin composit ion comprises an ethylene homo- or copolymer (A) and has a melt flow rate MFR ₅ , determined according to ISO 1 133 at 1 90 C and under a load of 5.00 kg, of 0.05 to 2.0 g/10 min.

[8] The polyolefin pipe according to the paragraphs [ 5 ] to [ 7 ] wherein the ethylene homo- or copolymer (A) is mult imodal.

[9 ] The polyolefin pipe according to any one of the paragraphs [ 1 ] to [8] wherein the propylene homo- or copolymer (B) is a propylene homo- or random copolymer.

[ 1 0 ] The polyolefin pipe according to any one of the paragraphs [ 1 ] to [9 ] wherein the propylene homo- or copolymer (B) has a melt flow rate MFR, determined according to I SO 1 1 33 at 230°C and under a load of 2.16 kg, of 0.05 to 2.0 g/10 min.

[ 1 1 ] The polymer pipe according to any one of the paragraphs [ 1 ] to [ 1 0] having an outer diameter of at least 20 mm.

[ 1 2] The polyolefin polymer pipe according to any one of the paragraphs [ 1 ] to

[1 1] having a failure time of at least 450 hours in the hoop stress test according to

ISO 1 167 at 5.7 MPa.

[ 1 3] The polymer pipe according to any one of the paragraphs [ 1 ] to [ 1 2] having a failure time in the hoop stress test according to ISO 1 1 67 at a pressure ranging from 5.4 to 6. 1 MPa at least 1 .5 times higher compared to a concentric pipe having the same inner and outer diameter, made from the same polyolefin composit ion under the same conditions.

[ 14 ] A process for producing the polymer pipe according to any one of the

paragraphs [ 1 ] to [ 1 3 ] .

[ 1 5] Use of the polymer pipe according to any one of the paragraphs [ 1 ] to [ 14] for the transport of pressurized fluids.

The present invent ion will now be described by the following non-l imit ing examples. EXPERIMENTAL PART:

The determination is made by using a rheometer, preferably a Boh I in. CS Melt

Rheometer. Rheometers and their function have been described in "Encyclopedia of Polymer Science and Engineering", 2nd Ed., Vol. 14, pp. 492-509. The

measurements are performed under a constant stress between two 25 mm diameter plates (constant rotation direction). The gap between the plates is 1.8 mm. An 1.8 mm thick polymer sample is inserted between the plates.

The sample is temperature conditioned during 2 min before the measurement is started. The measurement is performed at 190 C. After temperature conditioning the measurement starts by applying the predetermined stress.

The stress is maintained during 1800 s to let the system approach steady state conditions. After this time the measurement starts and the viscosity is calculated. The measurement principle is to apply a certain torque to the plate a is via a precision motor. This torque is then translated into a shear stress in the sample. This shear stress is kept constant. The rotational speed produced by the shear stress is recorded and used for the calculation of the viscosity of the sample.

For determination of the viscosity at a shear stress of 747 Pa (η ₇ 4 ₇ ρ ₃ ) the pipe is re- melted.

Measurement of pipe wall thickness

A pipe wall gauge produced by Sciteq Denmark, having an electronic thickness gauge (Mahr, MarCator 1088) and a printer (M itutoyo DP- 1 VR )

The average wall thickness S _av is then calculated as follows. C min max whereby

Srnin is the minimum wall thickness of the pipe; and

Smax is the maximum wall thickness of the pipe

Density

Ail densities are measured according to ISO 1 183-187. Sample preparation is done by compression moulding in accordance with ISO 1872-2:2007.

Melt flow rate ( M FR )

The MFR is determined according to ISO 1 133.

Comonomer content

13C-NMR analysis was used to determine the comonomer content of the samples. Samples were prepared by dissolving approximately 0. 1 00 g of polymer and 2.5 ml of solvent in a 1 0 mm NMR tube. The solvent was a 90/ 1 0 mixture of 1 ,2,4- trichiorobenzene and benzene-d6. Samples were dissolved and homogenised by heat ing the tube and its contents at 1 50 C in a heating block.

The proton decoupled carbon- 13 single pulse NMR spectra with NOE were recorded on a Joel ECX 400 Hz NMR spectrometer. The acquisition parameters used for the experiment included a flip-angle of 45 degrees, 4 dummy scans, 3000 transients and a 1.6 s acquisition time, a spectral width of 20kHz, temperature of 125 C, WALTZ decoupl ing and a relaxation delay of 6.0 s. The processing parameters used included zero-fil ling to 32k data points and apodisation using an exponential window function within 1 .0 Hz artificial line broadening followed by automatic zeroth and first order phase correction and automatic baseline correction.

Comonomer contents were calculated using integral ratios taken from the processed spectrum using the assignments described in JC. Randal l's work (J MS - Rev.

Macromoi. Chem. Phys. , C29(2&3), 201 -317 (1989) using:

E = (\alphaB + \aiphaH + \betaB + \betaH + \gammaB + \gammaH + \delta++)/2 B = (methine B + 2B + 1 B)/3

H = (methine H + 4H + 3H + 2H)/4

where methine is the CH branch site, alpha, beta, gamma the carbon sits adjacent to the CH i.e. CH , alpha, beta, gamma, delta. \delta++ is the bulk CH2 site and the 1 ,2,3 and 4 sites represent ing the various carbon sites along the branch with the methyl group being designated 1 .

CE = 100% * ΕΛΈ+Β+Η)

CB = 100% * B/(E+B+H)

CH = 1 00% * H/(E+B+H)

Resistance to internal pressure

The resistance to internal pressure of pipes has been determined according to ISO

1 1 67- 1 on pipes having an outer diameter of 32 mm and an average wal l thickness of 3.2 mm. The measurement has been carried out at 5.7 MPa. Internal pressure of the pipe is calculated according to follow ing equat ion given in ISO ! 167- 1

uem ^min

where

σ is the hoop stress to be induced by the applied pressure, in MPa,

dmin is the minimum wail thickness of the free length of the test piece, in

millimetres, and

dem is the mean outside diameter of the test piece, in mil limetres. XRD measurement:

Diffractograms were obtained in transmission geometry with a Bruker D8 Discover equipped with an X-ray tube with a copper target operating at 40kV and 40mA and a GADDS 2-D detector, on thin slices cut from the pipes. The intensity vs. φ curves of (1 10) and (200) diffraction planes were obtained by integrating the 2D

diffractograms within the relevant 2Θ ranges.

The Hermans a-axis orientation factor f _a was obtained as

-a

2

where

<cos ² q> _a;Z > = <cos ² (p _200;Z :

and Hermans b-axis orientation factor ¾ was obtained as

where

< cos ² <p _{h /} >=<cos <p _{1 | o /} >-0.308 (p _{:m /} >0.692

K, White JL, Fellers JF, J. Appl. Poiym. Sci. 29, 21 17 (1984)]

The values of

^<cos2( Phki,z

is defined in general, for the reflect ion from the (hkl) plane as:

, / _η ^2π Ι(φ) sin cp cos ² (p dcp

>=

hkl,Z

ί ^2π Ι(φ) 8Ϊη φ d(p Xylenc cold solubles (XCS, wt.-%)

The XCS content was determined at 25 °C according ISO 16152; first edition; 2005- 07-01 . EXAMPLES:

In all examples a polyethylene composition comprising 2 wt.% carbon black having a density of 0.959 g/cm ³ an MFR ₅ , determined according to ISO 1 133 at 190°C and under a load of 5.00 kg, of 0.25 g/10 min, (Borsafe HE3490-LS)

Pipes hav ing an outer diameter of 2 mm and an average wall thickness of 3.2 mm with relative eccentricities provided in table 1 below have been produced using the above composit ion on a Reifenhauser R I I 381 pipe extruder with a die head of 32 mm. The temperature profile during extrusion was 1 75 °C to 185°C [175-180-185- 185-185-185]. The cooling of the pipes after the die exit has been taken place by spraying cooling water at 20 °C on the pipe outer surface.

The results of resistance to internal pressure test according to ISO 1 167 in hours are given in the following table 1 .

Table 1

* Test stopped without failure

** Test ongoing As can be seen from the above the eccentric pipes according to the present invention have improved performance in the hoop stress test according to ISO 1 167 compared with concentric pipes made from the same material and having the same average wall thickness.

X RD studies for OD32 mm pipes having relative eccentricity of 0 and 0. 14 revealed that (Table 1), orientation of the molecules on the radial direction is reduced and orientation on the direction perpendicular to machine direction (MD) is increased at both inner surface and in the core of the pipe. These findings show that the eccentricity creates molecular orientation on circumferential (hoop) direction. Table 2 Hermans orientation distribution factors (f _a perpendicular to MD, fi, radial direct ion, f _c MD)

A heat transfer simulation study, using Ansys Polyf!ovv performed to analyze the effect of eccentricity on the pipe wall temperature around circumference. A polymer melt at 200°C (BorSafe H E3490LS ) entering in the first cooling tank hav ing 20 °C water spray and 6. 1 5m length, then entering into the second cooling tank having 20°C water spray and 9 meter length and a 0.9 m gap between the first cooling tank with a pipe production line speed at 4 m m in and 32 mm OD and 3.2 mm average wail thickness and eccentricity values (e) at 0, 0.13, 0.33 and 0.44 are used for simulations. A constant density value was employed equal to 750kg nv and A constant thermal conductiv ity value was employed equal to 0.26W/m/ . Heat transfer coefficient for cooling water 360 W/(m ² K ) and Heat transfer coefficient for env ironment 10 W/(m ² K) are used.

The results of the simulat ion study are verified with experimental temperature measurements at the outer surface of the pipe at different locations along the pipe production line. The heat transfer analysis showed that eccentricity changes the temperature profile of the pipe wail, leading a temperature gradient not only from outer to inner surface, but also from thicker part to the thinner part of the pipe. The temperature gradient is directly related to the time to reach the crystallization temperature of the material and crystallization rate. As shown in the Figure 1 to Figure 4, temperature is high at the thicker part of the pipe wall and less at the thinner part. Furthermore, temperature difference between outer and inner surface of the pipe is less at the thinner part compared to thick part.

Figure 1 shows the temperature profile of an OD 32 SDR 1 1 pipe wall, with a relative eccentricity (e _r ) of zero

Figure 2 shows the temperature profile of OD 32 SDR 1 1 pipe wall, with e _r = 0.04 Figure 3 shows the temperature profile of OD 32 SDR ! 1 pipe wall, w ith e _r = 0. 1 Figure 4 shows the temperature profile of OD 32 SDR 1 1 pipe wall, with e _r = 0. 14