OBTAINING HEXANE SOLVENT FROM THE RAFFINATE OF...

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© Electronic scientific journal "Oil and Gas Business". 2014. №3 http://www.ogbus.ru

UDC 66.0

OBTAINING HEXANE SOLVENT FROM THE RAFFINATE OF THE

INSTALLATION L-PENSION POLYMERIZATION OF ETHYLENE

ПОЛУЧЕНИЕ ГЕКСАНОВОГО РАСТВОРИТЕЛЯ ИЗ РАФИНАТА

УСТАНОВКИ Л-35/6 ДЛЯ ПРОЦЕССА СУСПЕНЗИОННОЙ

ПОЛИМЕРИЗАЦИИ ЭТИЛЕНА

D.K. Saifullin, R.G. Spaschenko, A.M. Kiryukhin, A.Y. Spaschenko

FSBEI HPE «Ufa State Petroleum Technological University»,

Ufa, the Russian Federation

JSC «Scientific-technical centre «Salavatneftorgsintez»,

Salavat, the Russian Federation

Сайфуллин Д.К, Спащенко Р.Г, Кирюхин А.М., Спащенко А.Ю.

ФГБОУ ВПО «Уфимский государственный нефтяной технический

университет», г. Уфа, Российская Федерация

ООО «НТЦ Салаватнефтеоргсинтез», г. Салават, Российская Федерация

Abstract. Currently polyolefins find wide application in various industries in

mind the availability of a wide range and high performance. Among realized on

an industrial scale of ways to get polyolefins the suspension polymerization is

one of the most popular and traditional. In the process of suspension

polymerization of olefins as solvents are used uskoritjsya faction aliphatic

hydrocarbons with boiling temperature 65-95 °C. Development of high-

modified catalysts has allowed to simplify the technological scheme, increase

the output of the resulting polymer, to expand the grade range, but also to

toughen requirements to quality of the original solvents. So, the presence of

aromatic solvent, diene, acetylene, sulfur compounds leads to increased

consumption and deactivation of the catalyst, decrease the rate of

polymerization, instability of molecular mass and physical-mechanical

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properties of polymer and so on. Therefore, upon receipt of the solvent

polymerization purity of one of the most important tasks is to search for

available raw materials with minimal content of impurities.

As a result of research of raw materials and product flows refinery JSC

“Gazprom neftekhim Salavat” shown that gasoline-raffinate reforming

installation L-35/6 is a promising material for production of hexane fraction of

high purity, satisfying the requirements developed in JSC “Gazprom neftekhim

Salavat” synthesis technology suspension of high-density polyethylene. This

refined oils characterized by low content of aromatic and olefinic connections. It

is established that for allocation hexane solvent polymerization purity

insufficient use only distillation methods. It is shown that for deep purification

from impurities requires the use of additional methods: selective hydrogenation

of unsaturated hydrocarbons and adsorption at the molecular sieves.

Аннотация. В настоящее время полиолефины находят широкое

применение в различных областях промышленности в виду доступности,

широкого ассортимента и высоких эксплуатационных характеристик.

Среди реализованных в промышленных масштабах способов получения

полиолефинов суспензионная полимеризация является одной из самых

востребованных и традиционных. В процессе суспензионной

полимеризации олефинов в качестве растворителей используются

узкокипящие фракции алифатических углеводородов с температурой

кипения 65-95 °С. Разработка высокоэффективных модифицированных

катализаторов позволила упростить технологические схемы, повысить

выход образующегося полимера, расширить марочный ассортимент, но

одновременно и ужесточить требования к качеству исходных

растворителей. Так, наличие в растворителе ароматических, диеновых,

ацетиленовых, сернистых соединений приводит к увеличению расхода и

дезактивации катализатора, снижению скорости полимеризации, к

нестабильности молекулярно-массовых и физико-механических

характеристик полимера и т. д.

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Поэтому при получении растворителя полимеризационной чистоты

одной из важнейших задач является поиск доступного сырья, обладающего

минимальным содержанием нежелательных примесей.

В результате проведенных исследований сырьевых и продуктовых

потоков НПЗ ОАО «Газпром нефтехим Салават» показано, что бензин-

рафинат риформинга установки Л-35/6 является перспективным сырьем

для получения гексановой фракции высокой чистоты, удовлетворяющей

требованиям освоенной в ОАО «Газпром нефтехим Салават» технологии

синтеза суспензионного полиэтилена высокой плотности. Этот рафинат

характеризуется низким содержанием ароматических и олефиновых

соединений. Установлено, что для выделения гексанового растворителя

полимеризационной чистоты недостаточно использования только

ректификационных методов. Показано, что для глубокой очистки от

примесей необходимо использование дополнительных методов:

селективное гидрирование непредельных углеводородов и адсорбция на

молекулярных ситах.

Key words: solvent, raffinate, hexane fraction, distillation, hydrogenation,

adsorption.

Ключевые слова: растворитель, рафинат, гексановая фракция,

ректификация, гидрирование, адсорбция.

Introduction

Suspension method of obtaining high-density polyethylene (HDPE) is one of

the major in modern industry. Polymerization of ethylene occurs in aliphatic

environment, using inflicted titanium-magnesium catalysts, which can simplify

instrumentation of technological process, reduce energy consumption and keep

the process under mild conditions: reactor temperature 80-90 °C, the pressure of

0.3-0.5 MPa.

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As the solvent, used narrow fractions of isomeric hexanes and heptanes

[1c.92-94]. To the solvent purity have very strict requirements on the content of

aromatic, diene, acetylene and heteroatomic compounds. Exceeding norms

allowable concentrations of impurities leads to a decrease of reaction rate of

polymerization, deactivation costly catalyst and change in quality of the final

HDPE [2].

Gasoline fractions and dearomatised gasoline from catalytic reforming

(raffinates) are the feedstock to obtain solvent used in the suspension

polymerization of ethylene. Impractical using thermal and catalytic cracking

gasoline for separation aliphatic hydrocarbon concentrates, due to the high

content of unsaturated hydrocarbons and the difficulty of their separation from

close-boiling saturated hydrocarbons [1 pр.55-58]. Obtaining the target fraction

of aliphatic hydrocarbons by using a simple distillation is difficult, due to the

formation of azeotropes, hexane isomers with naphthenic and aromatic

hydrocarbons [3 pр.1;5].

Therefore, to get polymerization purity solvent by simple distillation,

requires raw materials, which is a concentrate of aliphatic hydrocarbons,

purified from aromatic and unsaturated hydrocarbons C3-C6 and sulfur

compounds. If you have a large number of these impurities should use special

methods of separation and purification of selected fractions [6].

In JSC “Gazprom neftekhim Salavat” successfully implemented Hostalen

technology process for suspension polymerization of ethylene. As a solvent is

used hexane fraction. (Table 1).

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Table 1. Requirements for the quality of the solvent by Hostalen technology

Parameter Value

Temperature limits of the distillation,°С:

-the beginning of the boil, not less than 65

-the end of the boil, not more than 70

Saturated hydrocarbons, % wt. not less than 99.97

Aromatic hydrocarbons, % wt. not more than 0.01

n-Hexane, % wt. not less than 44

Cyclohexane, % wt. not more than 2

Bromine index, mg Br2/100 g sample, not more than 50

Benzene, ppm, not more 100

Water, ppm, not more 50

Sulfur, ppm, not more 2

The main purpose is to choose the optimal variant for recovery and

purification hexane fraction, satisfying the requirements of the suspension

Hostalen technology. As a source of raw materials for production of solvent

chosen, dearomatized raffinate from extractive distillation unit L-35/6 in JSC

“Gazprom neftekhim Salavat”. Selection raffinate as a source of raw materials,

due to the fact, that this faction is not currently qualified practical application

and it is available in sufficient quantities in JSC “Gazprom neftekhim Salavat”.

Experimental

Object of laboratory research is gasoline-raffinate from extractive distillation

unit L-35/6.

Individual hydrocarbon composition of raw materials and accumulating

target fractions determined in accordance with GOST R 52714-2007 on a gas

chromatograph "Crystal 5000" with a flame ionization detector on a capillary

column DB-1 100 m x 0,25 mm x 0,5 m. Programmable temperature rise from 0

°C to 250 °C at a rate of 1 to 4 °C/min.

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Fractional composition of raw materials determined in accordance with

GOST 2177 on an automated analyzer OptiDist HERZOG company. Bromine

index (ASTM D1492) and water content in the samples (ASTM D4928) - on the

coulometric titrator C30X Mettler Toledo company. Sulfur content - by using

X-ray fluorescence analyzer SPECTROSCAN MAX-GV with GOST 52660-

2006.

Accumulation hexane fraction 63-70 °C and 65-70 °C were carried out on

semi-automatic column AUTOMAXX 9400 B/R Instrument company (USA)

with ASTM D 2892-05. The distillation column with Propak packing has an

efficiency of 15 theoretical trays.

Selective hydrogenation of olefins fractions 63-70 °C was carried out using

platinum alumina supported catalyst domestic production at a specialized

laboratory installation R-301 manufactured by Reaction Enginering (South

Korea). Installation represents, automated computer controlled system, including

high-precision piston pump, heated mixer, flow tubular catalytic reactor, furnace

with three heating zones, refrigerator, hydrogen flow and pressure regulators in

the system. Hydrogenation was carried out at a temperature of 250 °C, a

pressure of 1.5 MPa, feed space velocity 2 h-1, volume ratio of hydrogen to raw

material is 1:80.

Studies of adsorption purification method from benzene was carried out on

an installation, comprising three serially connected thermostated adsorber with

dimensions (d = 2 cm, h = 25 cm) loaded zeolite NaX produced by "SkatZ"

(Salavat) with 2.5-3.0 mm diameter extrudate (Figure 1). Purification was

carried out at atmospheric pressure, a temperature of 40 °C, feed rate - 5 ml/min.

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Figure 1. Schematic diagram of the adsorption dearomatisation hexane fraction:

E-1 – feedstock pump; N-1 - pump; K-1, K-2, K-3 - adsorbers

Results and discussion

In our experiments we used petrol raffinate following composition (Table 2).

Е-1

Н-1

К-1 К-2

Sampling 1 Sampling 2

Sampling 3

К-3

Feed

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Table 2 .Characteristics of petrol raffinate used to obtain a hexane fraction

As can be seen from Table 2, the content of benzene in the initial raffinate

was 0.24 % wt. According to [3 pр. 3-5.] hexane solvent recovery from the

raffinate by simple distillation method without additional dearomatization

possible only with a low content of benzene 0.05-0.1 % wt. Indeed,

experimental studies on the separation fraction 65-70 °C from gasoline-raffinate

showed excess of allowable standards for content of benzene and olefins. The

hydrocarbon composition of the fractions obtained is shown in Table 3.

Parameter Value

Density at 15°C, g/cm3 0.670

Fractional composition, °C

- Initial boiling point 38.7

- 10% of the product 51.5

62.5

90.5 - 50% of the product

- 90% of the product

- End of boiling 138.8

Hydrocarbon composition, % wt.:

n-С3 0.01

n-С4 1.18

∑ i-C4 0.66

n-С5 8.46

∑ i-C5 9.47

n-С6 15.71

∑ i-C6 38.80

n-С7 2.71

∑ i-C7 9.59

n-С8 0.29

∑ i-C8 1.39

∑ n-С9-Сn, i-C9-Сn 0.35

∑ aromatics 4.01

including benzene 0.24

∑ cycloparathins 7.29

∑ C5-C6 olefins 0.03

Unidentified components 0.05

Bromine index, mg Br2/100 g sample 165.5

Total sulfur content, ppm 20.0

Water Content, ppm 29.6

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Table 3. Hydrocarbon composition hexane fractions 65-70 °C

Parameter

Value Hydrocarbon composition,% wt.:

i-Pentane 0.01

n-Pentane 0.01

2,2-dimethylbutane 0.02

2,3-dimethylbutane 0.64

2-methylpentane 7.18

3-methylpentane 15.92

n-Hexane 58.27

2-methylpenten-2 0.02

3-methylcyclopenten-1 0.02

3-methylpenten-2 0.05

Methylcyclopentane 15.16

2,4-dimethylpentane 0.73

2,2,3-trimethylbutane 0.14

Benzene 0.79

3,3-dimethylpentane 0.13

Cyclohexane 0.47

2-methylhexane 0.30

3-methylhexane 0.13

n-Heptane 0.01

Bromine index, mg Br2/100g sample 268.3

Water Content, ppm 54.6

As can be seen from Table 3, high benzene content (0.79% wt.) and

unsaturated hydrocarbons (0.09 % wt.) makes it impossible to involvement of

this solvent in HDPE producing process.

The next stage of research on the production of high purity hexane solvent is

the selective hydrogenation of unsaturated hydrocarbons [12-17]. For the

experiments from gasoline-raffinate was accumulated fraction 63-70 °C

(Table 4).

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Table 4. The hydrocarbon composition of the target fraction 63-70 °C before

and after hydrogenation

Parameter Hexane fraction 63-70°С before hydrogenation

Hexane fraction

63-70°С after

hydrogenation

Hydrocarbon composition,% wt.: Value

i-Butane 0.05 0.02

n-Butane 0.11 0.05

i-Pentane 5.66 4.06

n-Pentane 6.38 4.99

2,2-dimethylbutane 5.55 5.21

Cyclopentane 2.49 2.20

2,3-dimethylbutane 5.01 5.00

2-methylpentane 23.47 23.66

3-methylpentane 18.23 18.79

n-Hexane 19.41 20.78

Methylcyclopentane 4.92 5.37

2,4-dimethylpentane 0.71 0.78

2,2,3-trimethylbutane 0.11 0.13

Benzene 0.36 0.25

3,3-dimethylpentane 0.42 0.48

Cyclohexane 0.38 0.56

2-methylhexane 2.84 3.27

3-methylhexane 1.98 2.28

3-ethylpentane 0.16 0.19

n-Heptane 0.81 0.93

Toluene 0.44 0.40

Others 0.51 0.60

Bromine index, mg Br2/100g sample 177.7 21.0

Sulfur content, ppm 22.76 2.0

As the analysis of samples in the experiment, the olefins in hexane fraction

were almost completely removed, bromine index fell from 177.7 to 21 mg

Br2/100 g solvent, the total sulfur content was reduced to 2 ppm. However, the

aromatic content is not actually changed, which makes the question of further

purified hexane solvent.

As the most economically reasonable method of adsorption purification

method is chosen adsorption on molecular sieves. The homogeneous crystal

structures of the zeolite, the presence of well-defined input window size allow

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its use for separations based on differences in the size and shape of the

molecules [18]. To purify a hexane solvent most promising type of zeolites is

NaX, exhibiting high selectivity towards to benzene with a critical molecular

diameter of 0.7 nm [19, 20]. Paraffins, isoparaffins, naphthenic hydrocarbons

penetrate into adsorption cavity through the input window in zeolite NaX, but

not retained therein. According to [21], in a single stage passage of hexane

solvent through a molecular sieve at a temperature of 20-60 °C may reduce the

aromatics content to less than 0.01% wt.

In our studies on the adsorption purification as feedstock taken hydrotreated

hexane fraction 63-70 °C. The hydrocarbon compositions of samples after each

adsorber are shown in Table 5.

Table 5. Hydrocarbon composition of the target fraction 63-70°C after

adsorption purification on zeolites of NaX

Parameter After first adsorber After second

adsorber After third adsorber

Hydrocarbon composition, % wt. Value

i-Butane 0.14 0.06 0.03

n-Butane 0.22 0.11 0.06

i-Pentane 6.41 5.29 4.49

n-Pentane 6.37 5.61 4.99

2,2-dimethylbutane 6.40 6.45 6.18

Cyclopentane 2.19 2.03 1.91

2,3-dimethylbutane 5.23 5.34 5.35

2-methylpentane 23.68 24.15 24.42

3-methylpentane 18.41 18.93 19.25

n-Hexane 18.21 18.57 19.12

Methylcyclopentane 4.68 4.82 4.99

2,4-dimethylpentane 0.75 0.82 0.86

2,2,3-trimethylbutane 0.13 0.14 0.15

Benzene 0.002 - -

3,3-dimethylpentan 0.47 0.52 0.54

Cyclohexane 0.36 0.37 0.39

2-methylhexane 2.88 3.10 3.33

3-methylhexane 2.02 2.17 2.33

3-ethylpentane 0.18 0.20 0.20

n-Heptane 0.79 0.84 0.89

Others 0.003 0.001 -

Bromine index mgBr2/100g sample 0.48 0.48 0.52

i-Butane 19.7 17.9 11.2

n-Butane 2.1 1.8 1.7

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Table 5 show that a purification hexane fraction on NaX zeolites occurs

complete adsorption of aromatic compounds. Benzene and toluene are adsorbed

in first adsorber, their content reduced from 0.25 % wt. and 0.40 % wt.

respectively to trace amounts. After the second adsorber are observed absence of

benzene and toluene content of 0.001% wt. The absence of toluene recorded

after the third adsorber.

Conclusion

So as a result of studies found:

1) Gasoline-raffinate of the L-35/6 is a perspective raw material for

producing a hexane solvent satisfying the requirements of Hostalen technology;

2) Technology for producing hexane solvent the required quality must

include the following steps isolation and purification:

a) fractionating the gasoline raffinate from installation L-35/6 to obtain a

narrow fractions 65-70 °C;

b) selective hydrogenation separated fraction 65-70°C to obtain on platinum

alumina supported catalyst hydrogenate with olefinic hydrocarbon content not

more than 50 mg Br2/100 g of solvent;

c) the adsorption treatment hydrogenate in NaX type zeolite to obtain a

hexane solvent with chemical composition given in Table 1.

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272


About the authors

Сведения об авторах

D.K. Saifullin, Master of MPT 21-12-02 Group, of the Chair «Technology of

Oil and Gas», FSBEI HPE USPTU, Ufa, the Russian Federation

Сайфуллин Д.К., магистрант гр. МТП21-12-02, кафедра «Технологии

нефти и газа», ФГБОУ ВПО УГНТУ, г. Уфа, Российская Федерация

e-mail: [email protected]

R.G. Spaschenko, Candidate of Chemical Science, Lead Specialist of

Laboratory of Physico-Chemical Studies of Polymers, JSC «Scientific-Technical

Centre «Salavatneftorgsintez», Salavat, the Russian Federation

Спащенко Р.Г., канд. хим. наук, ведущий специалист, ООО «НТЦ

Салаватнефтеоргсинтез», г. Салават, Российская Федерация

A.M. Kiryukhin, Candidate of Chemical Science, Head of laboratory of

Physico-Chemical Studies of Polymers, JSC «Scientific-technical Centre

«Salavatneftorgsintez», Salavat, the Russian Federation

Кирюхин А.М., канд. хим. наук, начальник лаборатории физико-

химических исследований полимеров, ООО «НТЦ

Салаватнефтеоргсинтез», г. Салават, Российская Федерация

A.Y. Spaschenko, Candidate of Engineering Science, Head of Refining

Processes laboratory, JSC «Scientific-Technical Centre «Salavatneftorgsintez»,

Salavat, the Russian Federation

Спащенко А.Ю., канд. техн. наук, начальник лаборатории процессов

нефтепереработки, ООО «НТЦ Салаватнефтеоргсинтез», г. Салават,

Российская Федерация

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