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Conversion of waste plastic to propylene and cumene

A technology of propylene and cumene, applied in the field of conversion of waste plastics to propylene and cumene, can solve the problems of affecting the economy of bisphenol A and expensive cumene, etc.

Active Publication Date: 2019-08-16
SABIC GLOBAL TECH BV
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

Cumene produced from intermediates derived from petroleum feedstocks is expensive, affecting the economics of the bisphenol A production process

Method used

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  • Conversion of waste plastic to propylene and cumene
  • Conversion of waste plastic to propylene and cumene
  • Conversion of waste plastic to propylene and cumene

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0098] High-severity pyrolysis of mixed waste plastics to investigate the production of propylene and benzene for cumene synthesis. The mixed waste plastic has 82% olefin feedstock (such as high-density polyethylene (HDPE), low-density polyethylene (LDPE), linear low-density polyethylene (LLDPE) and polypropylene (PP)), 11% polystyrene ( PS), and the remaining 7% is polyethylene terephthalate (PET). The pyrolysis is carried out with continuous catalytic cracking in a circulating fluidized bed. The cracking was carried out with 57.5% spent fluid catalytic cracking (FCC) catalyst and 42.5% ZSM-5 based zeolite additive and operated at a feed and catalyst cupmix temperature of 390-560°C. The feed rate of the plastic feed was 316 g / hour and the catalyst / feed weight ratio was about 30. In the case of the single-stage pyrolysis process, the propylene content of the pyrolysis effluent was 23.7%, as can be seen from the data in Table 1. The overall yield of light gas olefins was abo...

Embodiment 2

[0114]Low-severity pyrolysis of mixed waste plastics to investigate the production of propylene and benzene for cumene synthesis. The mixed waste plastic has 82% olefin feedstock (such as high-density polyethylene (HDPE), low-density polyethylene (LDPE), linear low-density polyethylene (LLDPE) and polypropylene (PP)), 11% polystyrene ( PS), and the remaining 7% is polyethylene terephthalate (PET). Mixed plastic waste was pyrolyzed as described in Example 1, except that the temperature was about 450°C. The pyrolysis effluent is further hydrotreated to saturate all liquid olefins before being sent further to steam cracking. The hydrotreated pyrolysis liquid can generally contain 35-45% paraffins, 35-45% isoparaffins, 15-20% naphthenes and 5-10% aromatics, wherein the hydrotreated pyrolysis liquid Boiling below 400°C. Hydrotreated pyrolysis liquids can be subjected to (i) steam cracking only; (ii) steam cracking followed by C 4 -C 5 Catalytic cracking of cracking; or (iii) c...

Embodiment 3

[0119] Mixed plastic waste is cracked in a modular unit at low severity; or in a circulating fluidized bed at high severity; or in a circulating fluidized bed at low severity to generate heat Degreasing. The results of these cracking experiments are shown below. The cup mixing temperature was varied between 400-600°C, especially 450-550°C. Depending on the severity of the operation, gas and liquid products are separated. The composition of the cracked liquid product is shown in the table below. The saturated hydrocarbons present in the gas are sent to a gas cracker, either an ethane cracker or a propane cracker. The choice of gas cracker depends on the desired end product. The cracked liquids from the pyrolysis unit are sent to hydrotreating to saturate all the liquid olefins as this is a liquid / naphtha cracker requirement. Hydrotreating is carried out at 300-450° C. and a pressure of 20-100 barg using a commercially available hydrotreating catalyst to produce a hydrotrea...

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Abstract

A process for producing propylene and cumene comprising converting plastics to hydrocarbon liquid and pyrolysis gas in pyrolyzer; feeding hydrocarbon liquid to hydroprocessor to yield hydrocarbon product and first gas stream; introducing hydrocarbon product to second separator to produce first C6 aromatics and refined product; feeding refined product to steam cracker to produce steam cracker product; introducing steam cracker product to third separator to produce second C6 aromatics, third propylene stream, second C2&C4 unsaturated stream, C1-4 saturated gas, and balance hydrocarbons product;introducing pyrolysis gas and / or first gas stream to first separator to produce first propylene stream, first C2&C4 unsaturated stream, and saturated gas stream; feeding first and / or second C2&C4 unsaturated stream to metathesis reactor to produce second propylene stream; feeding first and / or second C6 aromatics, and first, second, and / or third propylene stream to alkylation unit to produce cumene; and conveying balance hydrocarbons product to pyrolyzer and / or hydroprocessor.

Description

technical field [0001] The present disclosure relates to the production of high value products such as olefins and aromatics from blended plastics by processes including pyrolysis, hydrotreating, steam cracking, alkylation and olefin metathesis, with cumene and propylene being the preferred products. Background technique [0002] Cumene is an important chemical intermediate, almost all of the cumene produced is converted to cumene hydroperoxide, an intermediate in the synthesis of other industrially important chemicals such as phenol and acetone, which can be Further used in the production of bisphenol A. Current methods of producing cumene convert petroleum feedstocks into benzene and propylene, which then react to form cumene. Cumene produced from intermediates derived from petroleum feedstocks is expensive, affecting the economics of the bisphenol A production process. Therefore, there is a continuing need to develop methods for producing cumene from feedstocks other th...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C07C11/06C07C15/085C10G1/10C10G45/00C10G69/06C10G69/12
CPCC07C2/66C07C6/04C10G47/04C10G47/12C10G47/14C10G69/06C10G69/123C10G1/002C10G1/02C10G1/10C10G2300/1003C10G2400/20C10G2400/30C07C11/06C07C15/085
Inventor 克里希纳·库马尔·拉马穆尔蒂拉维钱德尔·纳拉亚纳斯瓦米文卡塔·拉马纳拉亚南·加纳帕蒂·博特拉亚历山大·斯坦尼斯劳斯桑托什·甘吉
Owner SABIC GLOBAL TECH BV
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