WO2020169888A1

WO2020169888A1 - Method and process arrangement for producing hydrocarbons and use

Info

Publication number: WO2020169888A1
Application number: PCT/FI2020/050111
Authority: WO
Inventors: Matti Nieminen; Matti Reinikainen
Original assignee: VTT Technical Research Centre of Finland Ltd
Current assignee: VTT Technical Research Centre of Finland Ltd
Priority date: 2019-02-21
Filing date: 2020-02-21
Publication date: 2020-08-27
Anticipated expiration: 2021-08-21
Also published as: JP2022521284A; US20240150664A1; BR112021016440A2; US20220145194A1; CN113677748A; US12365846B2; CN113677748B; KR20210128470A; KR102925277B1; EP3927764A1; CA3130873A1; US11905477B2

Abstract

The invention relates to a method and process arrangement for producing hydrocarbons from polymer-based waste in which the polymer-based waste (1) is gasified with steam (3) at low temperature in a gasifier (2) for forming a product mixture (4), and the temperature is 640 – 750 °C, and the product mixture (4) is supplied from the gasifier (2) to a recovery unit (6) of the hydrocarbons for separating at least one hydrocarbon fraction (7,8,9). Further, the invention relates to the use of the method.

Description

METHOD AND PROCESS ARRANGEMENT FOR PRODUCING HYDROCAR BONS AND USE

FIELD

The application relates to a method defined in claim 1 and a process arrangement defined in claim 15 for producing hydrocarbons, e.g. olefins. Further, the application relates to a use of the method defined in claim 21.

BACKGROUND

Known from the prior art is to produce hydro carbons and olefins from fossil raw material by a cracking process. Further, it is known from the prior art that different olefin fractions can be separated by a recovery process.

Further, it is known from the prior art that waste plastic is difficult to recycled and to utilize as raw material in new products. Mechanical recycling is the cheapest way to recycle but its applicability is limited to clean plastic, and mechanically recycled plastic is typically used in lower level applications.

OBJECTIVE

The objective is to disclose a new type meth od and process arrangement for producing hydrocarbons, such as olefins, from waste raw material. Further, the objective is to disclose a new type method and process arrangement for utilizing polymer-based waste as raw material. Further, the objective is to replace virgin fossil raw material in olefin production.

SUMMARY

The method and process arrangement and use are characterized by what are presented in the claims. In the method and process arrangement, hydro carbons, e.g. olefins, are produced from polymer-based waste by treating the polymer-based waste by means of gasification in a gasifier to form a product mixture and the hydrocarbons are separated from the product mixture in a recovery unit.

BRIEF DESCRIPTION OF THE DRAWINGS

The accompanying drawings, which are included to provide a further understanding of the invention and constitutes a part of this specification, illus trate some embodiments of the invention and together with the description help to explain the principles of the invention. In the drawings:

Fig. 1 is a flow chart illustration of a pro cess according to one embodiment, and

Fig. 2 is a flow chart illustration of a pro cess according to another embodiment.

DETAILED DESCRIPTION

In the method for producing hydrocarbons from polymer-based waste, the polymer-based waste (1) is gasified with steam (3) at low temperature in a gasi fier (2) for forming a product mixture (4), and the temperature is 640 - 750 °C in the gasifier, and the product mixture (4) is supplied from the gasifier (2) to a recovery unit (6) of the hydrocarbons for sepa rating at least one desired hydrocarbon fraction (7,8, 9) .

The process arrangement for producing hydro carbons from polymer-based waste comprises a gasifier (2) in which the polymer-based waste (1) is gasified with steam (3) at low temperature which is 640 - 750 °C for forming a product mixture (4), a steam inlet for supplying the steam (3) to the gasifier (2), and a recovery unit (6) into which the product mixture (4) is supplied from the gasifier (2) and in which at least one desired hydrocarbon fraction (7,8,9) is sep arated .

One embodiment of the method and the process arrangement is shown in Fig 1. Another embodiment of the method and the process arrangement is shown in Fig 2.

In this context, the polymer-based waste (1) means any waste which comprises polymer or polymers, or which consists of one or more polymers. Often the poly mer-based waste is a heterogenous material. In one em bodiment, the polymer-based waste comprises at least polyolefins, e.g. polyethylene or polypropylene. The polymer-based waste may contain also other polymers. Further, the polymer-based waste may contain also oth er components, such as paper, cardboard and/or alumin ium material. In one embodiment, the polymer-based waste is a mixed plastic material. In one embodiment, the polymer-based waste comprises multi-layer plastic packages and products. In one embodiment, the polymer- based waste comprises polyolefins over 80 w-%, prefer ably over 90 w-%. In one embodiment, the polymer-based waste comprises polyolefins below 80 w-%, in one em bodiment below 70 w-%, in one embodiment below 60 w-% and in one embodiment below 50 w-%. In one embodiment, the polymer-based waste comprises PVC plastic, in one embodiment below 2 w-%. In one embodiment, the poly mer-based waste, i.e. the feed of the gasifier (2), is in a solid form, e.g. in the form of shredded materi al. In one embodiment, the polymer-based waste is treated before the supply into the gasifier, for exam ple by means of grinding, milling, chopping, shred ding, briquetting, pelletizing or other means of com pacting. In one embodiment, particle sizes of the pol ymer-based waste can vary, for example between 0.1 mm - 100 mm in flat form particles and for example 0.1 mm - 30 mm in spherical form particles. In one embodi ment, the polymer-based waste is inertisized with ni trogen, for example to decrease oxygen from the feed, before the supply into the gasifier.

In this context, the product mixture (4) means any product mixture, such as product gas, from the gasifier (2) . Usually the product mixture is a mixture of hydrocarbons, and further may comprise car bon monoxide and hydrogen. The product mixture com prises one or more components. In one embodiment, the product mixture may contain ethylene, propylene, buta diene, aromatic hydrocarbons and/or other hydrocar bons. In one embodiment, the product mixture comprises at least light hydrocarbons, such as C1-C6 hydrocar bons. In one embodiment, the product mixture comprises at least olefins. In one embodiment, the product mix ture comprises at least ethylene. In one embodiment, the product mixture comprises at least ethylene, pro pylene and light aromatic hydrocarbons, such as ben zene or toluene. In one embodiment, the product mix ture further comprises hydrogen and/or carbon monox ide. Further, the product mixture may contain also other components or compounds, e.g. solid components, such as solid particles or solid impurities. In one embodiment, the product mixture is an olefin-rich product mixture. In one embodiment, the product mix ture is an ethylene-rich product mixture.

In this context, the gasification in a gasi fier means any gasification process by steam. The gas ification is a process that converts starting material into gasification products, e.g. hydrocarbons and hy drogen. This is achieved by treating the starting ma terial at suitable temperatures, with a controlled amount of steam and/or additional oxygen.

In one embodiment, the gasifier (2) is ar ranged in parallel with one or more known cracking unit (12), in which the cracking unit comprises at least one cracking device, such as a steam cracker. In one embodiment, the gasifier (2) is arranged in paral lel with at least one cracking unit (12) . In one em bodiment, the process arrangement comprises at least one cracking unit (12) which is arranged in parallel with the gasifier (2). In said cracking unit (12), a hydrocarbon mixture (13) of the cracking unit is pro duced by cracking from other raw material (11), such as crude oil derived distillates or their upgraded products, e.g. naphtha, ethane or propane. Then both the product mixture (4) from the gasifier (2) and the hydrocarbon mixture (13) of the cracking unit (12) can be supplied the recovery unit (6), or to a desired step or device of the recovery unit (6), and the prod uct mixture (4) is a portion of a feed to the recovery unit (6) . In one embodiment, the product mixture (4) and the hydrocarbon mixture (13) of the cracking unit can be supplied to the same step or device of the re covery unit (6) . In one embodiment, the product mix ture (4) and the hydrocarbon mixture (13) of the cracking unit can be supplied to the different steps or devices of the recovery unit (6) . In this context, the hydrocarbon mixture (13) of the cracking unit means any hydrocarbon-containing mixture which com prises at least olefins, such as ethylene, propylene and/or other olefins. Further, the hydrocarbon mixture (13) may be comprise other hydrocarbons and/or other components .

In one embodiment, the gasifier (2) is a flu idized bed gasifier. Any suitable bed material can be used as the fluiding material in the fluidized bed. In one embodiment, the bed material is sand and/or calci um-containing bed material, such as lime, limestone, dolomite, CaCCg or CaO. In one embodiment, the bed ma terial contains 0 - 100 w-% sand and 100 - 0 w-% cal- cium-containing bed material. In one embodiment, the bed material consists of sand. In one embodiment, the bed material consists of calcium-containing bed mate rial. In one embodiment, the bed material contains below 60 vol-%, in one embodiment below 50 vol-%, in one embodiment below 30 vol-%, calcium-containing bed material. In one embodiment, AI2O3 is added to the bed material. In one embodiment, the bed material may com prise 0.1 - 100 vol-% AI2O3.

In one embodiment, the treatment temperature is over 700 °C, e.g. between 700 - 750 °C in the gasi fier (2) . In one embodiment, the treatment temperature is 710 - 740 °C, and in one embodiment 720 - 730 °C. In one embodiment, the treatment temperature is 690 - 730 °C, and in one embodiment 700 - 720 °C. In one em bodiment, the treatment temperature is 640 - 700 °C. In one embodiment, the treatment temperature is 640 - 670 °C.

In one embodiment, the treatment is carried out under atmospheric pressure in the gasifier (2) . In one embodiment, the treatment is carried out at a pressure of below 4 bar, in one embodiment below 3 bar and in one embodiment below 2 bar.

In one embodiment, a residence time in the gasifier (2) is clearly longer than a residence time in the cracking device, such as in the steam cracker, of the cracking unit (12) . In one embodiment, the res idence time is 3 - 30 seconds in the gasifier (2) . In one embodiment, the residence time is 4 - 30 seconds in the gasifier (2) . In one embodiment, the residence time is 4 - 20 seconds in the gasifier (2) . In one em bodiment, the residence time is 5 - 15 seconds in the gasifier (2) . In one embodiment, the residence time is 10 - 20 seconds in the gasifier (2) .

In one embodiment, the product mixture (4) is cooled after the gasifier (2) . In one embodiment, the product mixture is cooled to temperature of 400 - 500 °C. In one embodiment, the product mixture (4) is cooling before the supplying to the recovery unit (6) . In one embodiment, the process arrangement comprises at least one cooling device for cooling the product mixture ( 4 ) .

In one embodiment, the product mixture (4) is filtered after the gasifier (2) . In one embodiment, the product mixture (4) is filtered after the cooling of the product mixture. In one embodiment, the product mixture (4) is filtered by a hot filter. Alternative ly, the product mixture can be filtered by any suita ble filter, cyclone or other filtration device. In one embodiment, the process arrangement comprises at least one filter (5), e.g. a hot filter or other suitable filter or filtration device, for filtering the product mixture (4) . In the filtration solid components, such as solid particles or solid impurities, can be removed from the product mixture (4) . In one embodiment, chlo rine (Cl) and/or chlorine compounds are removed from the product mixture by injecting absorbent before gas filtration or using calcium based bed additive.

In one embodiment, the product mixture (4) comprises over 30 w-% olefins, such as ethylene and propylene, in one embodiment over 25 w-% and in one embodiment over 20 w-%. In one embodiment, the product mixture (4) comprises over 25 w-% ethylene, and in one embodiment over 20 w-%. In one embodiment, the product mixture (4) comprises over 13 w-% light aromatics, such as benzene, and in one embodiment over 10 w-%.

In one embodiment, the product mixture (4) can be supplied to the desired step in the recovery unit (6) of the hydrocarbons, e.g. to the first step or device, or to the later step or device. In one em bodiment, the product mixture (4) is a portion of the feed to the recovery unit (6) . In one embodiment, the product mixture (4) is used at least as the portion of the feed to the recovery unit (6) . In one embodiment, the product mixture can be used as such in the feed to the recovery unit. In one embodiment, the product mix ture (4) can be treated before the supply to the re covery unit (6) . In one embodiment, undesired compo nents of the product mixture, for example impurities or metals, e.g. aluminium, or heavy aromatic hydrocar bons may be removed from the product mixture (4) after the gasifier (2) . In one embodiment, the aromatic hy drocarbons, e.g. heavy aromatic hydrocarbons and/or light aromatic hydrocarbons, may be removed from the product mixture (4) after the gasifier (2) .

A recovery process which comprises the recov ery unit (6) may be multistep process, in which de sired hydrocarbons, such as hydrocarbon fractions, and/or desired other components or fractions are sepa rated from the feed of the recovery process. The re covery process is a separation process for separating hydrocarbons in which the feed is separated into its component parts or fractions. The process arrangement comprises at least recovery unit (6) in which hydro carbons, such as hydrocarbon fractions (7,8,9), are recovered. The recovery unit (6) comprises more than one device for separating desired hydrocarbons and hy drocarbons fractions. Further, other components or fractions may be separated in the recovery unit. The recovery unit (6) may comprise different devices for separating hydrocarbons or other components, such as separating devices, distillation apparatuses, cooling devices, hydrogenation devices, dewatering devices, or other suitable devices. In one embodiment, the recov ery unit (6) comprises at least separating device and/or distillation apparatus. In one embodiment, the recovery unit (6) comprises at least distillation ap paratus. In one embodiment, the desired hydrocarbons are separated by distillation. In one embodiment, the recovery unit (6) comprises at least separating de vice. In one embodiment, the desired hydrocarbons are recovered or removed by separating means of one or more separation devices. In one embodiment, carbon monoxide and/or hydrogen are recovered in the recovery unit. In one embodiment, the aromatic hydrocarbons are recovered in the recovery unit. In one embodiment, un desired components of the product mixture can be re moved in the recovery unit. Any suitable separation device known per se can be used as the separation de vice in the process arrangement. Any suitable distil lation apparatus known per se can be used as the dis tillation apparatus in the process arrangement. The distillation apparatus may be based on distillation, e.g. fractional distillation, or extraction distilla tion.

In one embodiment, the recovered hydrogen can be recirculated to a suitable process step of the pro cess or to a desired refining process, in which the hydrogen is needed for processing. In one embodiment, the recovered carbon monoxide, aromatic hydrocarbons, tars and/or methane can be recirculated to a suitable process step of the process or to a desired reforming process, or back to the gasifier (2), for example to form energy for the gasifier or maintain temperature in the gasifier. In one embodiment, the aromatic hy drocarbons, e.g. light aromatic hydrocarbons, can be used as a final product or as a source material for chemicals .

In one embodiment, the product distribution can be adjusted based on gasification conditions in the gasifier (2) and/or the selected polymer-based waste material (1) . In one embodiment, ethylene-rich product mixture is formed from the polymer-based waste (1) in the gasifier (2) . In one embodiment, undesired components of the product mixture (4), methane, hydrogen, carbon monoxide and/or the aromatic hydrocarbons, e.g. heavy aromatic hydrocarbons, are used to produce energy for the gasi- fication or recirculated back to the gasifier (2) . In one embodiment, said components and materials can be treated in a device integrated with the gasifier for producing energy. In one embodiment, the undesired components of the product mixture (4), methane, hydro- gen and/or carbon monoxide can be used as energy mate rial to provide heat to the gasifier (2) . In one em bodiment, the aromatic hydrocarbons, e.g. heavy aro matic hydrocarbons, are used to produce energy for the gasification, and they can be used as energy material to provide heat to the gasifier (2) .

In one embodiment, the process arrangement comprises at least one recirculation device for recy cling undesired components, carbon monoxide and/or aro matic hydrocarbons back to the gasifier (2) . In one em- bodiment, the recirculation device is arranged to re circulate the aromatic hydrocarbons, carbon monoxide and/or undesired components from the recovery unit (6) to the gasifier (2) .

In one embodiment, the process arrangement comprises more than one gasifier (2) for treating the polymer-based waste (1) . Then the product mixtures, such as product gases, from said gasifiers (2) can be supplied to the recovery unit (6), or to the desired step or device of the recovery unit (6) .

In one embodiment, the process arrangement comprises at least one first feed inlet for supplying the polymer-based waste (1) into the gasifier (2) . In one embodiment, the process arrangement comprises at least one first outlet for discharging the product mixture (4) out from the gasifier (2) . In one embodiment, the process arrangement comprises at least one feed inlet of the recovery unit (6), e.g. second feed inlet, for supplying the product mixture (4) of the gasifier (2) and/or the hydrocarbon mixture (13) of the cracking unit (12) into the recov ery unit (6) . In one embodiment, the process arrange ment comprises at least one outlet, e.g. second out let, for discharging at least one olefin fraction (7,8,9) out from the recovery unit (6).

The feed inlet may be any suitable inlet known per se, e.g. pipe, port or the like. The outlet may be any suitable outlet known per se, e.g. pipe, outlet port or the like.

In one embodiment, the process arrangement comprises at least one feeding device for feeding pol ymer-based waste (1) to the gasifier (2) . In this con text, the feeding device can be any feeding device, equipment or other suitable device. In one embodiment, the feeding device is selected from the group compris ing a screw, conveyor, tube, pipe, pneumatic feeding device, pneumatic conveyor, extruder, other suitable feeding device and their combinations. In one embodi ment, the polymer-based waste is fed to the gasifier by means of a pneumatic feeding device or pneumatic conveyer using methane, e.g. recycled methane from this process, as a pneumatic gas.

The steam (3) can be supplied via the steam inlet to the gasifier (2) . In one embodiment, the steam is fed from bottom of the gasifier to the gasi fier. In one embodiment, the steam inlet is arranged in connection with the bottom of the gasifier. In one embodiment, the process arrangement comprises a dis tribution means, e.g. a grate, which is arranged in conncetion with the bottom of the gasifier for dis tributing the steam inside the gasifier. Any suitable steam inlets and distribution means can be used in the gasifier .

The method and process arrangement can be op erated as a continuous process.

In one embodiment, the method and process ar rangement are used and utilized in a production of hy drocarbons such as light hydrocarbons, olefins, e.g. ethylene, propylene and butadiene, light aromatic hy drocarbons, e.g. bentzene and toluene, carbon monox ide, hydrogen, or their combinations. The products, such as hydrocarbon fractions, from the recovery unit can be used as such or can be supplied, for example, to a polymerization process, oxidation process, halo- genation process, alkylation process or other chemical process, or to a production of plastic. For example, ethylene and propylene are building blocks for plastic products, petrochemical products and chemicals.

Thanks to the invention polymer-based waste can be treated and utilized easily and effectively. The desired hydrocarbons, like olefins, can be recov ered. Further, light aromatic hydrocarbons, such as benzene, toluene, xylene or the like, derived from the polymer-based waste can be recovered, and heavy aro matic hydrocarbons can be recirculated and utilized in the process. In this process the waste can be upgrad ed. The method and process arrangement offer a possi bility to treat the polymer-based waste easily, and energy- and cost-effectively.

The present invention provides an industrial ly applicable, simple and affordable way to produce hydrocarbons and especially olefins from the polymer- based waste. The present invention provides flexible and economically feasible way to recycle waste poly olefins back to olefins. The method and process ar rangement are easy and simple to realize in connection with production processes. Further, the recycling of the polymer-based waste can be improved by means of the invention. Fur ther, a part of new crude oil based raw material can be replaced with the polymer-based waste. Further, no investment is needed for a recovery unit when the ex isting recovery process can be applied.

EXAMPLES

Figs. 1 and 2 present the method and also process arrangement for producing hydrocarbons contin uously from polymer-based waste.

The process of Fig. 1 comprises a fluidized bed gasifier (2) in which the polymer-based waste (1) is gasified with steam (3) at low temperature which is 640 - 750 °C, for example 720 - 730 °C, for forming a product mixture (4), a steam inlet for for supplying the steam (3) to the gasifier (2), and a recovery unit (6) into which the product mixture (4) is supplied from the gasifier (2) and in which at least one de sired hydrocarbon fraction (7,8,9) is separated. The treatment is carried out under atmospheric pressure in the gasifier (2), and the residence time is 4 - 30 s, in one embodiment 5 - 15 s, in the gasifier.

The steam (3) is fed by means of a suitable steam feed device via the steam inlet to the gasifier (2) .

The product mixture (4) comprises at least ethylene, propylene and light aromatic hydrocarbons such as benzene or toluene, and further may comprise hydrogen and carbon monoxide. Further, the product mixture may comprise other hydrocarbons. Preferably, the product mixture is the ethylene rich product mix ture .

In one embodiment, the product mixture (4) may be cooled, for example to temperature of 400 - 500 °C, after the gasifier (2) . In one emdodiment, the process arrangement may comprise at least one filter ing device (5), e.g. a hot filter, for filtering the product mixture (4) and for removing solid components from the product mixture after the gasifier, for exam ple after the cooling of the product mixture.

The product mixture (4) can be supplied to a desired step or device in the recovery unit (6) of the hydrocarbons. The product mixture (4) is a portion of the feed to the recovery unit (6) . In the recovery unit (6) at least desired hydrocarbons or hydrocarbon fractions are recovered, e.g. ethylene (7), propylene (8) and aromatic hydrocarbons (9) . The recovery unit (6) comprises different devices for separating desired hydrocarbons, such as separating devices, distillation apparatuses, cooling devices, hydrogenation devices, dewatering devices or other suitable devices. Prefera bly, the recovery unit (6) comprises at least separat ing device and/or distillation apparatus. The hydro carbon fractions (7,8,9) are separated by separation and/or distillation in the recovery unit (6) .

Further, the carbon monoxide, hydrogen, me thane, aromatic hydrocarbons (9) and/or other unde sired components may be recovered in the recovery unit (6) . The recovered hydrogen may be recirculated to a suitable process step of the process or to a desired refining process, in which the hydrogen is needed for processing. The recovered carbon monoxide, aromatic hydrocarbons, methane and/or other undesired compo nents may be recirculated to a suitable process step of the process, or back to the gasifier (2) . Said com ponents may be recirculated back to the gasifier to produce energy, temperature and/or steam for the gasi fication. The process arrangement may comprise at least one recirculation device for recycling carbon monoxide, methane and/or undesired components from the recovery unit (6) back to the gasifier (2) . The process arrange- ment may comprise at least one recirculation device for recycling the aromatic hydrocarbons (9), e.g. heavy ar omatic hydrocarbons (10), from the recovery unit (6) back to the gasifier (2) . Alternatively, the aromatic hydrocarbons, e.g. light aromatic hydrocarbons, can be used as a final product or as a source material for chemicals .

According to Fig. 2, the gasifier (2) is ar ranged in parallel with a known cracker unit (12), which comprises at least one cracking device such as a steam cracker. In said cracking unit (12), a hydrocar bon mixture (13) is produced by cracking from other raw material (11), such as fossil raw material. Then both the product mixture (4) from the gasifier (2) and the hydrocarbon mixture (13) from the cracking unit (12) can be supplied the recovery unit (6), or to the desired step or device of the recovery unit (6), and the product mixture (4) is the portion of the feed to the recovery unit (6) .

Example 1

The process was studied in a bench scale bubling fluidized bed gasifier.

Polyethylene based waste was used as a feed and steam was used as a gasification agent in the gas ifier. Low gasification temperatures were used, and the temperatures were between 690 - 730 °C in the gas ifier. The residence time was about 4 - 8 s in the gasifier. A product gas was formed during the gasifi cation in the gasifier. Five test periods have been carried out and analysed.

In olefin industry, an olefin mixture com prising, for example, ethylene and propylene are nor mally produced by cracking and treating naphtha, ethane or propane in a cracking unit, and olefins are recovered from the olefin mixture by multistep recov ery process.

It was observed from the tests that the main components in the dry product gas were: 28.1 - 33.3 vol-% ¾, 20.0 - 27.7 vol-% CH and 21.1 - 26.5 vol-%

CH , and in additional tests 22.2 - 39.3 vol-% CH . The product gas was surprisingly rich in ethylene. The results were compared with results from the olefin mixture of the conventional naphtha cracker, in which the olefin mixture contains 1.03 vol-% ¾ + CO, 15.35 vol-% CH and 31.02 vol-% CH . The product distribu tion of the product gas was quite similar than the conventional product distribution of the olefin mix ture from the naphtha cracker. Further, it was ob served from the tests that the product gas had high tar loading. However, no filtration problems were ob served. Thus, the mixture of the product gas, compris ing at least ethylene, and further aromatic hydrocar bons, e.g. tars, was suitable feedstock for the down stream process of the conventional olefin recovery process or recovery unit. The steam gasifier according to the present invention can be installed parallelly with the conventional naphtha cracker enabling partial replacement of virgin naphtha by means of recycled polyolefins .

Example 2

The process was studied in a bench scale bubling fluidized bed gasifier.

In the gasifier the polymer-based feed was gasified with steam at low temperature which is 700 - 720 °C for forming a product mixture.

Polyethylene material was used as a feed in the first test, and mixed plastic material, which is not suitable for mechanical recycling, was used as a feed in the second test. The bed material was sand or a mixture of sand and dolomite in the tests.

In the first test, the product mixture com prised ethylene, propylene and light aromatic hydro- carbons such as benzene, and further comprised hydro gen, methane and other hydrocarbons. Further, the product mixture comprised carbon dioxide and carbon monoxide. In PL-9 and PL-16 sand was used as the bed material, and in PL-6 the mixture of the dolomite and sand (dolomite : sand was 50:50) was used as the bed ma terial. The temperature was 705 °C and fluidizing ve locity was 0.31 m/s in PL-6 and PL-9 gasifications, and the temperature was 720 °C and fluidizing velocity was 0.5 m/s in Pl-16 gasification. The yield of the product components per polyethylene material feed, as dry product gas, is presented in Table 1.

Table 1

In the first test, it was observed that high olefin yield can be achieved. Further, it was observed that the product gas comprised tar, i.e. condensable hydrocarbon compounds including for example aromatic compounds. However, no filtration problems were ob served. Further, from the PL-6 it was observed that the dolomite addition (dolomite : sand was 50:50) in the bed material increased the olefin yield.

In the second test, the product mixture com prised ethylene, propylene and light aromatic hydro carbons such as benzene, and further comprised hydro gen, methane and other hydrocarbons. Further, the product mixture comprised carbon dioxide and carbon monoxide. In NP-12 sand was used as the bed material. The temperature was 720 °C and fluidized velocity was 0.31 m/s in NP-12 gasification. The yield of the prod uct components per polyethylene material feed, as dry product gas, is presented in Table 2.

Table 2

In the second test, it was observed that high olefin yield can be achieved. Further, it was observed that the product gas comprised tar, i.e. condensable hydrocarbon compounds including for example aromatic compounds. However, no filtration problems were ob served .

The devices and equipments of the process used in these examples are known per se in the art, and therefore they are not described in any more de tail in this context.

The method and process arrangement are suita- ble in different embodiments for producing hydrocar bons from different polymer-based waste.

The invention is not limited merely to the examples referred to above; instead many variations are possible within the scope of the inventive idea defined by the claims.

Claims

1. A method for producing hydrocarbons from polymer-based waste, char a c t e r i z e d in that the method comprises

- gasifying the polymer-based waste (1) with steam

(3) at low temperature in a gasifier (2) for forming a product mixture (4), and the tempera ture is 640 - 750 °C, and

- supplying the product mixture (4) from the gasi- fier (2) to a recovery unit (6) of the hydrocar bons for separating at least one hydrocarbon fraction (7,8,9) .

2. The method according to claim 1, cha r a c t e r i z ed in that the gasifier (2) is arranged in parallel with at least one cracking unit (12) .

3. The method according to claim 1 or 2, cha ra c t e r i z e d in that the gasifier (2) is a fluidized bed gasifier.

4. The method according to any one of claims 1 to 3, cha ra c t e r i z ed in that the treatment temperature is 700 - 750 °C in the gasifier (2) .

5. The method according to any one of claims

1 to 4, cha ra c t e r i z e d in that the treatment temperature is 700 - 720 °C in the gasifier (2) .

6. The method according to any one of claims

1 to 5, cha r a ct e r i z e d in that the bed materi al is sand and/or calcium-containing bed material in a fluidized bed of the gasifier.

7. The method according to any one of claims 1 to 6, cha r a ct e r i z e d in that the polymer- based waste comprises at least polyolefins and other polymers .

8. The method according to any one of claims 1 to 7, cha r a c t e r i z e d in that residence time is 4 - 30 seconds in the gasifier (2) .

9. The method according to any one of claims

1 to 8, cha r a c t e r i z e d in that the product mixture (4) is cooled to temperature of 400 - 500 °C after the gasifier (2) .

10. The method according to any one of claims

1 to 9, cha r a c t e r i z e d in that the product mixture (4) is filtered after the gasifier (2) .

11. The method according to any one of claims

1 to 10, cha r a c t e r i z e d in that the product mixture (4) comprises at least ethylene, propylene and light aromatic hydrocarbons.

12. The method according to any one of claims 1 to 11, cha ra c t e r i z e d in that the aromatic hydrocarbons are recovered.

13. The method according to any one of claims 1 to 12, cha r a c t e r i z e d in that undesired com ponents of the product mixture (4) and/or the aromatic hydrocarbons are used to produce energy for the gasi fication .

14. The method according to any one of claims 1 to 13, cha ra c t e r i z e d in that the product mixture (4) is a portion of the feed to the recovery unit ( 6) .

15. A process arrangement for producing hy drocarbons from polymer-based waste, cha r ac t e r i z e d in that the process arrangement comprises

- a gasifier (2) in which the polymer-based waste (1) is gasified with steam (3) at low temperature which is 640 - 750 °C for forming a product mix ture ( 4 ) ,

- a steam inlet for supplying the steam (3) to the gasifier (2), and

- a recovery unit (6) into which the product mix ture (4) is supplied from the gasifier (2) and in which at least one desired hydrocarbon fraction (7,8,9) is separated.

16. The process arrangement according to claim 15, c h a r a c t e r i z e d in that the process arrangement comprises at least one cracking unit (12) which is arranged in parallel with the gasifier (2) .

17. The process arrangement according to claim 15 or 16, c h a r a c t e r i z e d in that the gasifier (2) is a fluidized bed gasifier.

18. The process arrangement according to any one of claims 15 to 17, c h a r a c t e r i z e d in that the process arrangement comprises at least one hot filter (5) for filtering the product mixture (4) .

19. The process arrangement according to any one of claims 15 to 18, c h a r a c t e r i z e d in that the recovery unit (6) comprises at least separating device and/or distillation apparatus.

20. The process arrangement according to any one of claims 15 to 19, c h a r a c t e r i z e d in that process arrangement comprises at least one recircula tion device for recycling undesired components of the product mixture (4) back to the gasifier (2) and/or at least one recirculation device for recycling the aro matic hydrocarbons back to the gasifier (2) .

21. A use of the method according to any one of claims 1 to 14, c h a r a c t e r i z e d in that the method is used in a production of hydrocarbons, light aromatic hydrocarbons, carbon monoxide, hydrogen, or their combinations.