PVC AND PE WASTE TREATMENT TO HYDROCARBON FUEL

PRESENTED BY

AHSAN GHANIHASSANUDDIN NIZAMIHASNEN AHMEDUMER HASAN AND RASHID KHAN

INTRODUCTION

The increase of waste PVC is serious environmental problem issue for today.

PVC plastic can serve as a potential resource with the correct treatment and its converting as hydrocarbon raw materials or as a useful fuel.

PVC plastic has high chlorine (Cl) content and percentage is 56% by total weight.

INTRODUCTION

Chlorine component need to be removed by using alkali wash before using produce fuel.

Thermal degradation process with 5% Zinc Oxide (ZnO) can reduce chlorine content result in polymer chain generating product with heavy molecular weight and some uncontrolled Cl content.

The thermal degradation of waste PVC produces only 35.6% of liquid product, some light gas 34.47% and rest of residue29.93%.

INTRODUCTION

Thermal degradation temperature was use 75-400 ºC.

This produced fuel can be used for feedstock refinery for potential energy generation.

EXPERIMENTAL PROCESS DESCRIPTION

Waste plastic PVC to liquid hydrocarbon fuel production process into laboratory scale was use thermal degradation process with 5% Zinc Oxide (ZnO) catalyst with 1% activated carbon and at temperature 75 - 400 ºC under atmospheric pressure in presence of oxygen.

Sample was using only polyvinyl chloride and experiment was performing fully close system.

Experimental purpose sample was use 75 gm and glass reactor was use.

PROCESS

Reactor temperature range can go up to 450 ºC.

Grinded waste plastic (PVC) fence sample put into reactor chamber with 5% Zinc Oxide catalyst and 1% activated carbon then heat start from 75 ºC temperature to up to 400 ºC.

When PVC waste plastic start to melt due to temperature increase from melted PVC waste plastic turn into liquid phase and liquid phase to turn into vapor, vapor passing through condenser unit its becomes liquid form and it’s called plastic fuel.

PROCESS

This PVC waste plastic to fuel conversion rate is 35.6%.

This produced fuel density is 0.81 g. /ml.

5% Zinc Oxide catalyst was use for remove chlorine content from this experiment and no extra chemical used in this conversion process.

PROCESS

During plastic converting to liquid fuel all vapor is not turn into fuel some vapor portion is come out as a light gas because that gas boiling point is minus temperature.

Light gas cleaning purpose was use as an AgNO3 and NaOH/ NaHCO3 solution and after wash light gases passing through also water wash and at the end we put light gas into gas storage tank.

PROCESS

Alkali wash and water wash was cleaning chorine content.

Light gas percentage is 34.47%.

From PVC waste plastic to fuel production total conversion rate is 70.07%.

PROCESS

The produced PVC plastic to fuel passes through filter paper to remove fuel sediment to making fuel clean and water and sediment come out separately its call fuel sediment, this sediment and water we can retreat.

PROCESS

When we collected fuels some chlorine contents are came out with fuel, this fuel we passed through again Zinc Oxide solution to remove all chlorine content by precipitation method.

PROCESS

PVC waste plastic to fuel production period we are getting some black solid residue and this residue percentage is 29.93%.

PROCESS

Because PVC plastic has 56% chlorine contains and additives.

Experimental run time was 5.45 hours.

MASS BALANCE

In mass balance calculation showed 75 gm PVC to liquid fuel 26.7gm, light gas 25.85 gm and black solid residue 22.45 gm.

PVC WASTE PLASTIC TO FUEL PRODUCTION PROCESS WITH 5% ZnO AND 1% ACTIVATED CARBON

THERMO-CATALYTIC DEGRADATION OF LOW DENSITY POLYETHYLENE TO LIQUID FUELPOLYETYLENE (PE)

INTRODUCTION

Waste low-density polyethylene samples were subjected to thermo-catalytic degradation using kaolin as catalyst in a batch reactor at temperature range of 400 to 500°C and atmospheric pressure.

INTRODUCTION

The quality and yield of the condensable product has been studied as a function of temperature and amount of catalyst.

Both in thermal and catalytic degradation, the condensable fraction was less viscous liquid oil at low temperatures (up to 450°C), whereas with increase of temperature (from 475°C) the fraction became viscous and waxy.

INTRODUCTION

The recovery of condensable fraction increased from 30.8 wt. % at 400°C to 71.45% at 450°C and further increased to a maximum of 86.65wt. % at 500°C in absence of catalyst.

The catalyst increased the yield of the condensable product and decreased the reaction time.

The catalyst increased the yield of the condensable product and decreased the reaction time.

INTRODUCTION

The composition of the oil obtained at optimum reaction condition was characterized by gas chromatography-mass spectroscopy (and found consisting of paraffin’s and olefins with mainly C10-C16 components.

MATERIALS

The fine cuttings of waste polyethylene (PE) shopping bags (made of LDPE) of 2 cm area were used for the pyrolysis experiments. The catalyst employed in this study, commercial grade kaolin clay (Composition: SiO2 43.12%, Al2O3 46.07%, Fe2O3 nil, MgO 0.027%, CaO 0.030%, ZnO 0.0064%, K2O 0.01%, TiO 20.74) at 1,000°C, Surface area: 23m2/g, ammonia temperature programmed desorption (TPD) acidity: 0.049 mmol/g (with mesoporous surface).

EXPERIMENTAL SETUP

The experimental setup used in this work consists of a batch reactor made of stainless steel (SS) tube (length – 145 mm, internal diameter – 37 mm and outer diameter – 41 mm) sealed at one end and an outlet tube at other end.

EXPERIMENT

The SS tube is heated externally by an electric furnace, with the temperature being measured by a K type thermocouple fixed inside the reactor and temperature is controlled by external proportional-integral-derivative (PID) controller.

PID controller was used to control temperature of the furnace.

EXPERIMENT

20g of LDPE samples were loaded in each pyrolysis reaction. In the catalytic pyrolysis, a mixture of catalyst and the plastic pieces in different catalyst to plastics proportion (1:1, 1:2, 1:3, 1:4, 1:6, 1:10, 1:20) was subjected to decomposition in the reactor set up and heated at a rate of 20°C/min. up to the desired temperature.

EXPERIMENT

The condensable liquid  products were collected through the condenser and weighed.

After completion of reaction, the carbonaceous solid residue left out inside the reactor was weighed.

Then the weight of gaseous product was calculated from the material balance.

Reactions were carried out at different temperatures ranging from 400 to 500°C.

FIGURE

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