DE102007047931A1 - Thermal degassing of organic waste uses a main reactor, together with catalyst additives, to give active coke and a gas with an oil content free of tar and dioxin - Google Patents

Abstract

For the thermal degassing of organic waste materials, the organic waste (OA) is chopped in a grinder (1) and is converted in a main reactor (4) into coke (K) and a gas (OG) with an oil content, by pyrolysis at 500-650[deg] C. The chopped waste is dried (2), using exhaust gas (AG) from the main reactor mantle (5). A catalyst additive (ZK1) is fed (3) into the main reactor. The gas is fed (6) to a condenser (7) together with a catalyst additive (ZK2), to give liquid and gas phases. The gas phase is washed in a gas cleaner (8) with a catalyst additive (ZK3) and dried (13). The dry gas is used for heating, with surplus gas fed to a gas motor (12) to generate electrical energy (EE). The coke is activated by steam in an active coke reactor.

Description

Technical environment

The The invention relates to a process for the thermal degassing work-up of organic waste according to the characteristics Features of the main claim. It is particularly suitable organic waste to activated coke and high calorie fuels while avoiding harmful To work up byproducts such as dioxin.

since 2005 is the disposal of organic waste (AO), such as plastics of all kinds, waste wood, paper, rejects, shredder fractions z. B. from car recycling, sorted household waste, bitumen, waste oils, scrap tires, Siebresten and textiles only allowed if the Glückückstand is less than 3% by weight. Organic waste with a higher one Residue on ignition currently have in an elaborate Process in secondary raw materials and residual waste be separated. This can then only by pyrolysis or combustion be worked up.

at high water and / or large Plastic content is not easily burned and pyrolysis. During combustion, the large chlorine content of z. PVC, PCB and dioxin formation is an environmental problem. In addition, the high cost of this thermal utilization as a disadvantage. At the pyrolysis have other problems occurred, for. B. deposition / obstruction of / with Tars and dusts in the gas line.

Farther has already been proposed organic waste especially shredded material like shredded material from household waste, Used tires, biomass, plastics, intensively mixed with an olefin mixture, especially waste oil in a relationship of organic waste to olefin mixture of 5: 1 to 2: 1, preferably 7: 2 to 5: 2 to one homogeneous suspension to mix, this mixture of a heat treatment at temperatures of 200 ° C to 500 ° C, preferably 250 ° C to 300 ° C too undergo and by cooling to solidify.

Disclosure of the invention

Technical problem

task Therefore, the invention is a simpler process for working up of organic waste, as well as uses for the propose tar and dioxin-free products produced by the process, in which the recyclables contained therein another effective Recovery and supplied can be.

Technical solution

These The object is achieved by a method according to claim 1. In the dependent claims Additional features are provided for improved performance of the method.

to thermolytic processing of organic waste for the production of activated coke and high calorie fuels, are the crushed and dried organic waste OA in a main reactor decomposed to coke K, oil and gas. To do this the organic waste ground in the crusher.

The Ground material is made in a dryer using the exhaust gas dried waste heat contained in the reactor jacket of the main reactor.

z. B. wobei x = 3 – 6, y = 17 – 33, z = 5 – 11 und t = 7 – 12 ist und wirkt katalytisch, indem das Reaktionsgleichgewicht zu Gunsten der gewünschten Endprodukte verschoben wird sowie die Zerlegung der Ausgangsstoffe für Dioxinbildung erfolgt, wobei allerdings im Gegensatz zu echten Katalysatoren ein Teil der Substanz in das Ausgangsprodukt der Reaktion eingeht.Subsequently, it is fed to the main reactor with the addition of a first aggregate-catalyst mixture ZK1 by means of a feed unit. This additive-catalyst mixture ZK1 has the empirical formula

z. B. where x = 3 - 6, y = 17 - 33, z = 5 - 11 and t = 7 - 12 and acts catalytically by the reaction equilibrium is shifted in favor of the desired end products and the decomposition of the starting materials for dioxin formation takes place, However, in contrast to real catalysts part of the substance enters into the starting material of the reaction.

in the Main reactor are the organic waste at temperatures of 500 up to 650 ° C by thermolysis in coke, oil and gas disassembled.

wobei x = 24 – 34, y = 61 – 85, z = 3 – 3, t = 12 – 14 und m = 1 – 2 ist.The oily gas with the addition of a second aggregate-catalyst mixture ZK2 to avoid any tar and dust deposition, by a conveyor 6 a capacitor 7 fed. This additive-catalyst mixture ZK2 has the empirical formula

where x = 24-34, y = 61-85, z = 3 - 3, t = 12-14 and m = 1-2.

There becomes the oily one Gas in a liquid and a gaseous Phase separated.

bei der x = 6 – 18, y = 16 – 48, z = 3 – 9 und t = 7 – 21 ist, in einer Nassgasreinigung ausgewaschen und in einem Gastrockner getrocknet.The oil-free gas is then added with the addition of a third to schlagstoff-catalyst mixture ZK3 with a molecular formula

where x = 6 - 18, y = 16 - 48, z = 3 - 9 and t = 7 - 21, washed out in a wet gas cleaning and dried in a gas dryer.

The resulting dry gas is as necessary the main reactor as Fuel supplied.

Excess dry gas is used in a gas engine to generate electrical energy.

The condensate separated in the condenser is in a fractionation unit in oil and Aggregate-catalyst mixture ZK2 separated.

The resulting additive-catalyst mixture ZK2 from the oil-containing gas is the conveyor 6 fed while the oil is in a coke reactor 10 with the from the main reactor 4 coke mixed and decomposed into gas and coke.

Coke produced in this process is converted into activated carbon in an activated carbon reactor with steam at approx. 800-950 ° C 19 activated.

The Gas produced in both reactions is used in the gas purification plant further processed together with the coming out of the condenser gas.

attack end Washing water from the gas purification is in a distillation plant taking advantage of the waste heat of the gas engine separated into distilled water and salt.

The distilled water will partially replace the gas purification system and spent water used.

One other part of the defined water is using the waste heat in one Evaporator evaporates and the resulting vapor is in the activated carbon reactor used to activate the coke, which then as activated coke the Plant can be removed.

A in the conveyor rotating snail-shaped Brush, which also serves to clean the conveyor, supports the gas movement.

Short description of drawings

in the The invention is based on a drawing in the form of a Embodiment will be explained. It shows

1 a schematic representation of the method.

The best way, the invention exploit

For the thermolytic processing of organic waste for the production of activated coke and high-calorie fuels, shredded shredded material from household waste, scrap tires, biomass, plastics in a main reactor 4 decomposed to coke K, oil and gas. For this, the organic waste will be in the crusher 1 ground.

The millbase is placed in a dryer 2 using the exhaust gas AG from the reactor shell 5 of the main reactor 4 dried waste heat.

wobei x = 4, y = 21, z = 9 und t = 9 ist und wirkt katalytisch, indem das Reaktionsgleichgewicht zu Gunsten der gewünschten Endprodukte verschoben wird sowie die Zerlegung der Ausgangsstoffe für Dioxinbildung, wobei allerdings im Gegensatz zu echten Katalysatoren en teil der Substanz in das Ausgangsprodukt der Reaktion eingeht.Then it is added with the addition of a first aggregate-catalyst mixture ZK1 using a feed unit 3 the main reactor 4 fed. This additive-catalyst mixture ZK1 has the empirical formula

where x = 4, y = 21, z = 9 and t = 9 and acts catalytically by the reaction equilibrium is shifted in favor of the desired end products and the decomposition of the starting materials for dioxin formation, however, in contrast to real catalysts en part of the substance enters into the starting material of the reaction.

In the main reactor 4 and the organic wastes are decomposed at temperatures of 500 to 650 ° C by thermolysis in coke K oil OE and gas G.

wobei x = 28, y = 71, z = 3, t = 14 und m = 1 ist.The oily gas with the addition of a second aggregate-catalyst mixture ZK2 to avoid any tar and dust deposition, by a conveyor 6 a capacitor 7 fed. This additive-catalyst mixture ZK2 has the empirical formula

where x = 28, y = 71, z = 3, t = 14 and m = 1.

There becomes the oily one Gas it in a liquid Phase F and a gaseous Phase separated.

bei der wobei x = 6, y = 26, z = 9 und t = 21 ist, in einer Nassgasreinigung 8 ausgewaschen und in einem Gastrockner 13 getrocknet.The oil-free gas is then added with the addition of a third additive-catalyst mixture ZK3 with a molecular formula

where x = 6, y = 26, z = 9 and t = 21, in a wet gas purification 8th washed out and in one gas dryer 13 dried.

The resulting dry gas TG becomes part of the main reactor 4 supplied as heating material.

Excess dry gas is in a gas engine 12 used to generate electrical energy EE.

That in the condenser 7 separated condensate OZ is in a fractionation unit 11 separated in oil Oe and additive-catalyst mixture ZK2.

The resulting additive-catalyst mixture ZK2 is the oily gas of the conveyor 6 fed while the oil Oe in a coke reactor 10 with the from the main reactor 4 coke mixed and decomposed into gas and coke.

The resulting coke is in an activated carbon reactor 13 with steam at about 800-950 ° C to activated coke 19 activated.

The resulting gas in both reactions is in the gas purification plant 8th together with the one from the condenser 7 further processed gas.

Accumulating washing water Wd from the gas cleaning 8th is in a distillation plant 14 taking advantage of the waste heat AW of the gas engine 12 separated into distilled water Wg and salt S

The distilled water Wg will partially replace the gas purification system 8th spent water used.

Another portion of the distilled water Wg is using the waste heat AW in an evaporator 15 evaporates, and the resulting vapor Da is in the activated carbon reactor 13 used to activate the coke, which can then be removed as activated coke AK the plant.

One in the conveyor 6 rotating helical brush, while cleaning the conveyor 6 serves, supports the gas movement.

1

shredder

2

dryer

3

feeding unit

4

main reactor

5

reactor shell

6

Conveyor

7

capacitor

8th

gas cleaning

10

Koksreaktor

11

fractionation

12

gas engine

13

gas dryer

14

distillation plant

15

Evaporator

19

activated coke

AG

exhaust

AK

activated coke

AW

waste heat

There

steam

EE

electric energy

F

phase

K

coke

OA

scraps

Oe

oil

ÖG

gas

OZ

condensate

S

salt

TG

dry gas

Wd

wash water

wg

water

ZK1

Additive-catalyst mixture

ZK 2

Additive-catalyst mixture

ZK3

Additive-catalyst mixture

Claims (5)

Process for the thermal degassing of organic wastes for the production of gas, oil and activated coke, in which the comminuted and dried organic waste in a main reactor ( 4 ) are decomposed into coke (K) and oil-containing gas, characterized by the following process steps: 1. the organic waste (OA) is in the comminutor ( 1 2. the ground material is placed in a dryer ( 2 ) in the exhaust gas (AG) from the reactor shell ( 5 ) of the main reactor ( 4 ), 3.1. is then added with the addition of a first aggregate-catalyst mixture (ZK1) by means of a feed unit ( 3 ) the main reactor ( 4 ), 3.2. in the main reactor ( 4 ) and decompose the organic waste at temperatures of 500 to 650 ° C by pyrolysis in coke (K) and oily gas (ÖG), 4.1. the oily gas is added by adding a second aggregate-catalyst mixture (ZK2) through a conveyor ( 6 ) a capacitor ( 7 ), 4.2. there separated into a liquid phase (F) and a gaseous phase, 4.3.1. Subsequently, the gaseous phase with addition of a third additive-catalyst mixture (ZK3) in a gas cleaning ( 8th ) and 4.3.2 in a gas dryer ( 13 ), 4.4. the dry gas (TG) will, as necessary, the main reactor ( 4 ) supplied as heating material, 4.5. the excess dry gas is stored in a gas engine ( 12 ) used to generate electrical energy (EE), 5.1. that in the capacitor ( 7 ) separated condensate (OZ) is in a fractionation ( 11 ) in oil (Oe) and aggregate-catalyst mixture (ZK2), 5.1.1. The additive-catalyst mixture (ZK2) from the oily gas is the conveyor ( 6 ) and 5.1.2. the oil (Oe) is in a coke reactor ( 10 ) with the from the main reactor ( 4 ) and mixed into gas and coke 5.1.3. The resulting coke is in an activated carbon reactor ( 13 ) with water vapor at about 800-950 ° C to activated coke ( 19 ), 5.1.4. gas produced in both reactions is added to the gas purification plant ( 8th ) and there together with the from the capacitor ( 7 ) get the gas processed, 6.1. the washing water (Wd) and from the gas purification ( 8th ) is used in a distillation plant ( 14 ) using the waste heat (AW) of the gas engine (AW) 12 ) in distilled water (Wg) and salt (S), 6.1.1. the distilled water (Wg) is partly used to replace the gas purification plant ( 8th ) and used water, 6.1.2. another part of the defined water (Wg) is produced by means of the waste heat (AW) in an evaporator ( 15 ) vaporized, 6.1.2 the resulting vapor (Da) is in the activated carbon reactor ( 13 ) used to activate the coke, which can then be removed as activated coke (AK) of the plant. A method according to claim 1, characterized in that the gas movement in the conveyor ( 6 ) by a rotating helical brush, which at the same time cleaning the conveyor ( 6 ), is supported. Method according to one of the preceding claims, characterized in that the aggregate-catalyst mixture (ZK1) the empirical formula

where x = 3 - 6, y = 17 - 33, z = 5 - 11 and t = 7 - 12. Method according to one of the preceding claims, characterized in that the additive-catalyst mixture (ZK2) the empirical formula

where x = 24-34, y = 61-85, z = 3 - 3, t = 12-14, and m = 1-2. Method according to one of the preceding claims, characterized in that the aggregate-catalyst mixture (ZK1) the empirical formula

has, being.