# US 12,006,480 B2 · Method for processing liquefied waste polymers

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- Number: US 12,006,480 B2
- Document ID: US12006480B2
- Status: Granted
- Kind: B2
- Application number: 18/259,794
- Filed: 2021-10-29
- Published: 2023-12-07
- Granted: 2024-06-11
- Earliest claimed: 2020-12-30
- Assignees: Neste Oyj
- Applicants: Neste Oyj
- Inventors: Pekka Aalto; Heikki Aaltonen; Antti Ojala; Andrea Pérez Nebreda; Emma Sairanen; Ville Paasikallio; Antti Kurkijärvi
- Web page: https://patentgrep.com/patent/US12006480B2

## CPC

- C10G 45/08: in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
- C10G 45/32: Selective hydrogenation of the diolefin or acetylene compounds
- C10G 1/002: {in combination with oil conversion- or refining processes}
- C10G 1/10: from rubber or rubber waste
- C10G 65/02: plural serial stages only
- C10G 69/02: plural serial stages only
- C10G 2300/1003: Waste materials
- C10G: CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION (cracking to hydrogen or synthesis gas C01B; cracking or pyrolysis of hydrocarbon gases to individual hydrocarbons or mixtures thereof of definite or specified constitution C07C; cracking to cokes C10B); RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES

## Abstract

The present disclosure relates to methods for processing liquefied waste polymers (LWP) containing diolefins. The LWP feed is supplied to steam stripper A to provide a distillate containing diolefins and naphtha, and a distillate bottom. The distillate is subjected to hydrotreatment B to produce a diolefin depleted distillate which is separated by distillation C to give rise to one or more fractions comprising at least a naphtha fraction, an optional middle fraction and a bottom fraction. Hydroprocessing D of the naphtha fraction gives rise to hydrogenated naphtha which is suitable as a feed for a steam cracker E. Since the distillation bottom, bottom fraction and the middle distillate are predominantly free from diolefins, they can be mixed with crude oil and processed further in oil refinery.

## Claims

### Claim 1

A method for processing liquefied waste plastic (LWP), the method comprising the following steps:
a) providing an LWP stream containing diolefins and naphtha;
b) subjecting the LWP stream to a steam stripper to obtain a distillate containing diolefins and naphtha, and a distillate bottom;
c) subjecting the distillate to hydrotreatment reaction conditions in a presence of hydrogen and one or more hydrotreatment catalysts to produce diolefin depleted distillate, wherein the hydrotreatment reaction conditions include a temperature of 120-210° C., a pressure of 1-50 barg, and a liquid hourly space velocity (LHSV) of 1-5 h−1, and the one or more hydrotreatment catalysts are selected from CoMo and NiMo;
d) separating the diolefin depleted distillate to:
one or more fractions including:
at least a naphtha fraction with a boiling point below 180° C. at atmospheric pressure,
an optional middle fraction with a boiling point between 180° C. and 360° C. at atmospheric pressure; and
a bottom fraction; and
e) subjecting the naphtha fraction of step d) to hydroprocessing reaction conditions in a presence of hydrogen and one or more hydroprocessing catalysts to produce hydrogenated naphtha.

### Claim 2 (depends on 1)

The method according to claim 1, wherein the hydroprocessing reaction conditions of step e) comprise:
a temperature of 280-350° C., and a pressure of 20-100 barg.

### Claim 3 (depends on 2)

The method according to claim 2, wherein the hydrotreatment reaction conditions comprise:
a LHSV of 1-5 h−1, and a hydrogen/hydrocarbon ratio of 100-900 Nm3/m3.

### Claim 4 (depends on 1)

The method according to claim 1, wherein the one or more hydroprocessing catalysts are selected from CoMo and NiMo.

### Claim 5 (depends on 1)

The method according to claim 1, comprising:
feeding the hydrogenated naphtha to a steam cracker.

### Claim 6 (depends on 1)

The method according to claim 1, comprising:
admixing the bottom fraction of step d) and crude oil to form an admixture.

### Claim 7 (depends on 6)

The method according to claim 6, comprising:
feeding the admixture to a crude oil distillation unit.

### Claim 8 (depends on 1)

The method according to claim 1, wherein the one or more fractions of step d) comprise
a middle fraction with a boiling point between 180° C. and 360° C. at atmospheric pressure.

### Claim 9 (depends on 8)

The method according to claim 8, comprising:
feeding the middle fraction to a crude oil distillation unit.

### Claim 10 (depends on 1)

The method according to claim 1, wherein the LWP is selected from waste plastic pyrolysis oil, hydrothermally liquefied waste plastic oil or mixtures thereof.

### Claim 11 (depends on 1)

The method according to claim 1, wherein the LWP comprises:
waste plastic pyrolysis oil.

### Claim 12 (depends on 1)

The method according to claim 1, comprising:
feeding a mixture of crude oil and the bottom fraction of step d) to an oil refinery feed.

### Claim 13 (depends on 1)

The method according to claim 1, comprising:
feeding a mixture of crude oil and the middle fraction of step d) to an oil refinery.

### Claim 14 (depends on 1)

The method according to claim 1, comprising:
feeding a mixture of crude oil and distillation bottom of step b) to an oil refinery.