DE202017102445U1 - Apparatus for the thermal processing of pollutant-containing organic waste for the production of gas, oil and activated coke - Google Patents

Abstract

Device for thermal processing of polluted organic waste (IN) for the production of gas, oil and activated coke, characterized in that it consists of a digestion complex, a gas treatment, a coke preparation and the energy converter, wherein 1.1., The digestion complex from a dryer ( 2), the main reactor (8) and a coke reactor (11), 1.1.1. in which the dryer (2) has a feed device (1) through which the waste (IN) can be fed to the dryer (2) and 1.1.1.1. the dryer (2) is surrounded by a heating jacket (3) through which the waste (IN) can be heated to a drying temperature of 80 ° C to 120 ° C, preferably 110 ° C, 1.1.2. in which the main reactor (8) is connected to the dryer (1) via a material lock (4) through which the dried waste (IN) can be transferred to the main reactor (8), 1.1.3. in which the main reactor (8) is surrounded by a heating jacket (3) through which the waste (IN) is heated to a temperature of 350 ° C to 420 ° C, preferably 400 ° C, 1.1.3.1. wherein the main reactor (8) includes a liquid feed (6) through which a molten liquid consisting of waste oil (aÖ), tar (T) and a first aggregate mixture (ZA) can be added to the waste (1.1), 1.1.4. in which a further material lock (9) connects the main reactor (8) and the coke reactor (11) so that the waste (IN) can be transferred to the coke reactor (11) after the reaction with the molten liquid, 1.1.5. in which the coke reactor (11) has a further heating jacket (12), by means of which the reaction mixture supplied from the material lock (9) can be heated by means of purified process offgases to a temperature of 500 ° C. to 600 ° C., preferably 550 ° C. 1.1 .5.1. wherein in the coke reactor (11) there is a conveying device, preferably in the form of a screw conveyor (10), through which the reaction mixture is conveyed from the material lock (9) to the coke preparation (13-16) and during which it is thermally separated into coke and gas, 1.2. Coke preparation (13-16) from the coke separator (13), coke cleaning (14) and process water treatment (16), 1.2.1. In this case, the Kokstrenner (13) has a cooling jacket, which is charged with cooling water (KW), with a line emanating from the cooling jacket leads the heated water in the coke cleaning (14) and 1.2.2. In addition, the Kokstrenner (13) has a further material lock (15) through which the washed coke (K) can be removed, 1.2.3. a from the coke cleaning (14) outgoing water line leads to the process water treatment (16), in which the process water from the coke cleaning (14) and the gas scrubbing (19 to 23) using the waste heat from the combined heat and power plant (18) in distilled water (dW) and Fertilizing salts (D) to be separated, ...

Description

The invention relates to a method and a device for the thermal workup of pollutant-containing organic waste for the production of gas, oil and activated carbon.

For some years, the deposition of organic waste, such as plastics of all kinds, waste wood, paper, shredder fractions z. B. from car recycling, sorted household waste, bitumen, waste oils, used tires, Siebresten and textiles only allowed if the Glückückstand is below 3 wt .-%. Organic waste with a higher incineration residue must currently be separated in a complex process in secondary raw materials and residual waste. This can then be worked up only by pyrolysis or combustion. With high water and / or a large proportion of plastic combustion and pyrolysis is not without problems. When burning the large chlorine content of z. As PVC, PCB and the dioxin formation is an environmental problem. In addition, the high cost of this thermal utilization to name a disadvantage. In pyrolysis also occur further problems, such. B. settling / clogging of / with tars and dusts in the gas line. It has already been proposed, organic waste, in particular shredded from household waste, scrap tires, biomass, plastics intensive with an olefin mixture, especially waste oil in a ratio of organic waste to olefin mixture of 5: 1 to 2: 1, preferably 7: 2 to 5: 2 to mix a homogeneous suspension to subject this mixture to a heat treatment at temperatures of 200 ° C to 500 ° C, preferably 250 ° C to 300 ° C and solidify by cooling. According to DE 697 03 945 T2 For example, there is already proposed a process for the conversion of organic sludges comprising the steps of: (a) feeding dried sludge to a first reactor, (b) heating the dried sludge in the absence of oxygen in the first reactor to evaporate oil-producing organic contained therein Material which gives gaseous products and a sludge residue (coal), (c) condensing oil from the gaseous products of the first reactor in a condensation system to produce oil having a reduced water content, (d) injecting the oil from step (e) into a second reactor, (e) transferring the sludge residue (coal) from the first reactor to the second reactor, (f) contacting the heated sludge residue from step (b) in the second reactor with the oil from steps (c) and (d) in the absence of oxygen to allow the production of pure products and a high quality oil product; and (g) Removing the gaseous products from the second reactor.

The processing of unused raw materials or secondary raw materials for the production of charcoal, coke or activated carbon describes the DD 238 162 A1 , Here, the starting materials are prepared by coking or activation in a shaft furnace with rotary grate after the purge gas, charred with a pyrolysis temperature up to 600 ° C to charcoal, coked to coke or activated at a temperature up to 950 ° C.

Another method for thermal workup of polymer and cellulosic substances describes the EP 1078698 A1 , For this purpose, shredded plastic waste in an indirectly heated main reactor mixed with a nitrogen-containing additive-catalyst mixture and heated in a main reactor with mixing by means of a mixing screw to a temperature of 350 ° C to 600 ° C. The resulting coke is treated in an aftertreatment reactor at temperatures of 350 ° C to 600 ° C with the carbonization gas, further degassed, activated by the hydrogen contained in the carbonization and transported through a perforated screw conveyor to a material discharge. Resulting coke is ground in a mill to the desired fineness, after which the metal components are separated by means of magnetic separator and the free of metals coke is pressed in a briquetting to activated carbon pellets. The gas produced during the carbonization is washed, inter alia, with a solution containing calcium oxide and burned to heat the main reactor and the aftertreatment reactor. The object of the invention is therefore to propose a simpler apparatus for the treatment of organic waste, can be produced in the tar and dioxinfreie products, so that contained in the organic waste recyclables can be supplied to another effective recovery.

Thus, it remains an object of the invention to provide a device with the organic waste with ingredients that can lead to pollutant emissions with simple combustion, can be disposed of without environmental impact.

This object is achieved by drying the organic waste (IN) in a first step at a drying temperature of 80 ° C. to 120 ° C., preferably 110 ° C., and feeding it to the homogenization. The thus anhydrous organic waste (IN) are fused in the second step with a mixture of waste oil, tar and a first aggregate mixture (ZA) at a temperature of 350 ° C to 420 ° C, preferably 400 ° C and homogenized to a pasty mass. Finally, the pasty mass is thermally decomposed in the third step at a temperature of 500 ° C to 600 ° C, preferably 550 ° C in raw coke and a gas phase. When Aggregate mixture (ZA) is a mineral mixture with the components silicon, aluminum, nitrogen, oxygen and phosphorus. Its stoichiometric composition must be adapted to the respective pollutant content of the waste (IN).

The gas phase formed during the thermal decomposition is decomposed by stepwise cooling and admixture of a second aggregate mixture (ZB) into water, gas, oil and tar.

Tar and parts of the oil are recycled to digest the organic waste (IN), while the remaining parts of the oil and the recovered gas are sent for energy recovery.

The resulting water is prepared by admixing a third aggregate mixture (ZC) and used in the process by washing out the salts contained in the raw coke and then recovering it from the water by evaporation and further processing it into fertilizer.

To implement this method, a plant is proposed, which consists of a dryer ( 2 ), the main reactor ( 8th ) and a coke reactor ( 11 ) consists.

The dryer ( 2 ) has a feeding device ( 1 ), through which the waste (IN) the dryer ( 2 ) can be supplied. To dry the waste (IN), the dryer ( 2 ) of a heating mantle ( 3 ), through which the waste (IN) can be heated to a drying temperature of 80 ° C to 120 ° C, preferably 110 ° C. To improve the heat transfer, the walls of the dryer ( 2 ) with bulges ( 2a ).

The dryer ( 1 ) is connected to the main reactor ( 8th ) via a material lock ( 4 ), through which the dried waste (IN) enters the main reactor ( 8th ) can be handed over.

Also the main reactor ( 8th ) is from a heating mantle ( 3 ) by which the wastes (IN) are heated to a temperature of 350 ° C to 420 ° C, preferably 400 ° C. The main reactor ( 8th ) via a fluid supply ( 6 ) is supplied with a molten liquid and mixed with the waste (IN) consisting of waste oil (aÖ), tar (T) and the first aggregate mixture (ZA). Inside the main reactor ( 8th ) Stirrers can be arranged to improve the mixing.

Another material lock ( 9 ) connects the main reactor ( 8th ) and the coke reactor ( 11 ) so that the waste (IN) after the reaction with the molten liquid in the coke reactor ( 11 ) be handed over.

The coke reactor ( 11 ) has another heating jacket ( 12 ), through which the material from the sluice ( 9 ) is heated by means of purified process offgases to a temperature of 500 ° C to 600 ° C, preferably 550 ° C heated.

In the coke reactor ( 11 ) is a conveyor, preferably in the form of a screw conveyor ( 10 ), through which the reaction mixture from the material lock ( 9 ) for coke processing ( 13 - 16 ). Meanwhile, the reaction mixture is thermally decomposed into coke and gas.

Coke preparation ( 13 - 16 ) is made up of the Kokstrenner ( 13 ), coke cleaning ( 14 ) and process water treatment ( 16 ) together.

The Kokstrenner ( 13 ) has a cooling jacket, which is charged with cooling water (KW). The water which is heated in this process is passed through a line leading from the cooling jacket into the coke cleaning ( 14 ) guided. Through another material lock ( 15 ), the washed coke (K) from the Kokstrenner ( 13 ) are discharged.

That in the coke cleaning ( 14 ) and salted process water is used for process water treatment ( 16 ). Here, with the help of waste heat from the combined heat and power plant ( 18 ) in distilled water (dW) and fertilizer salts (D) separated, which in Kokstrenner ( 13 ) separated hot gas mixture is a gas line (G) for gas treatment ( 19 to 22 ).

This gas treatment ( 19 to 24 ) consists of the coolers ( 19 to 21 ), a distillation ( 22 ), an oil separator ( 23 ), an oil dryer ( 24 ) as well as the clean gas storage ( 25 ).

In the coolers ( 19 to 21 ), the exhaust gas (G) from the Kokstrenner ( 13 ) are cooled gradually. The cooling temperature of cooler 1 ( 19 ) 200 ° C, from cooler 2 ( 20 ) 120 ° C and finally cooler 3 ( 21 ) 30 ° C. As a result, crude oil of various composition is gradually separated from the gas.

From the coolers ( 19 to 21 ) lead crude oil pipes into the still ( 22 ), in which by means of the exhaust gas of the heating mantle ( 12 ) from the coke reactor ( 11 ) the crude oil is separated into tar (T) and fuel oil.

By another line is from the crude oil from the oil separator ( 23 ) separated, contaminated water for wastewater treatment ( 17 ).

The plant is finally as energy converter a cogeneration plant ( 18 ), which converts the purified exhaust gases and heating oils into electrical energy and process heat.

In the cooler 1 ( 19 ), a spray device is preferably provided, through which the gas can be additionally washed by means of a second aggregate mixture (ZB). As a second aggregate mixture (ZB), an organic liquid with a pH of 11-13 is proposed, by which the reaction of chloroaromatics and phenols to dioxin can be prevented.

Furthermore, according to the invention, it is suggested in wastewater treatment ( 17 ) to add a third aggregate mixture (ZC) to the wastewater, by means of which the wastewater can be freed from inorganic admixtures.

Based on the drawing 1 the invention will be explained below in an embodiment.

It shows

1 a block diagram of a plant for the thermal processing of pollutant-containing organic waste

To implement the method, a plant is proposed which consists of a dryer 2 , the main reactor 8th and a coke reactor 11 consists.

The dryer 2 has a feeder 1 on, through which the waste IN the dryer 2 can be supplied. To dry the waste IN, is the dryer 2 from a heating mantle 3 surrounded by which the waste IN can be heated to a drying temperature of 110 ° C. To improve the heat transfer, the walls of the dryer 2 with bulges 2a be provided.

The dryer 1 is with the main reactor 8th via a material lock 4 connected through which the dried waste IN into the main reactor 8th can be handed over.

Also the main reactor 8th is from a heating mantle 3 surrounded by which the waste IN to a temperature of 350 ° C to 420 ° C, preferably 400 ° C are heated. This is the main reactor 8th via a fluid intake 6 a melt liquid consisting of waste oil aÖ, tar T and the first aggregate mixture ZA, fed and mixed with the waste IN. Inside the main reactor 8th For the sake of clarity, stirrers, not shown, are arranged to improve mixing.

Another material lock 9 connects the main reactor 8th and the coke reactor 11 so that the waste IN after the reaction with the molten liquid in the coke reactor 11 be handed over.

The coke reactor 11 has another heating jacket 12 on, through which the material from the sluice 9 supplied reaction mixture using purified process exhaust gases to a temperature of 500 ° C to 600 ° C, preferably 550 ° C is heated.

In the coke reactor 11 is a screw conveyor 10 present, through which the reaction mixture from the material lock 9 for coke preparation 13 - 16 and thermally decomposed into coke and gas.

The coke preparation 13 - 16 sits down from the Kokstrenner 13 , the coke cleaning 14 and process water treatment 16 together.

The Kokstrenner 13 has a cooling jacket, which is charged with cooling water KW. The water heated in the process is removed by a line from the cooling jacket into the coke cleaning 14 guided. Through another material lock 15 can the washed coke K from the Kokstrenner 13 be dissipated.

That in the coke cleaning 14 used and enriched with salts process water is used for process water treatment 16 directed. Here it is using the waste heat from the combined heat and power plant 18 separated into distilled water dW and fertilizer salts D, Das in Kokstrenner 13 separated hot gas mixture is via a gas line G for gas treatment 19 to 22 directed.

This gas treatment 19 to 24 consists of the coolers 19 to 21 , a distillation 22 , an oil separator 23 , an oil dryer 24 as well as the clean gas storage 25 ,

In the coolers 19 to 21 can the exhaust gas G from the Kokstrenner 13 be cooled gradually. The cooling temperature of radiator 1 is 200 ° C, of radiator 2 120 ° C and finally radiator 3 30 ° C. As a result, crude oil of various composition is gradually separated from the gas,

From the coolers 19 to 21 lead crude oil pipes in the still 22 in which with the help of the exhaust gas of the heating mantle 12 from the coke reactor 11 the crude oil is separated into tar T and heating oil.

By another line is from the crude oil from the oil separator 23 separated, contaminated water for wastewater treatment 17 directed.

The plant is finally as energy converter a cogeneration plant 18 assigned, which converts the cleaned exhaust gases and heating oils into electrical energy and process heat.

In the radiator 1 19 a spray device is preferably provided, through which the gas can be additionally washed by means of a second aggregate mixture ZB. As the second aggregate mixture ZB, an organic liquid with a pH of 11-13 is proposed, by which the reaction of chloroaromatics and phenols to dioxin can be prevented.

Furthermore, according to the invention, it is stimulated in the purification of wastewater 17 to add to the wastewater a third aggregate mixture ZC by which the wastewater can be freed from inorganic admixtures.

The second aggregate mixture ZB is an organic liquid with a pH of 11-13, by which the reaction of chloroaromatics and phenols to dioxin can be prevented.

LIST OF REFERENCE NUMBERS

aÖ

waste oil

D

fertilizer salts

dW

water

G

exhaust

IN

scraps

K

coke

KW

cooling water

T

tar

ZA

Aggregate mixture

For example,

Aggregate mixture

ZC

Aggregate mixture

1

feeder

2

dryer

2a

bulge

3

heating jacket

4

material lock

6

hydration

8th

main reactor

9

material lock

11

Koksreaktor

12

heating jacket

13

Koksaufbereitung

14

Koksreinigung

15

material lock

16

Process water treatment

17

wastewater treatment

18

CHP

19

Cooler 1

20

Cooler 2

21

Cooler 3

22

distillation

23

oil separator

24

oil dryer

25

Clean gas storage

QUOTES INCLUDE IN THE DESCRIPTION

This list of the documents listed by the applicant has been generated automatically and is included solely for the better information of the reader. The list is not part of the German patent or utility model application. The DPMA assumes no liability for any errors or omissions.

Cited patent literature

• DE 69703945 T2 [0002]
• DD 238162 Al [0003]
• EP 1078698 A1 [0004]

Claims (7)

Device for thermal processing of polluted organic waste (IN) for the production of gas, oil and activated coke, characterized in that it consists of a digestion complex, a gas treatment, a coke preparation and the energy converter, wherein 1.1., The digestion complex from a dryer ( 2 ), the main reactor ( 8th ) and a coke reactor ( 11 ), 1.1.1. where the dryer ( 2 ) a feeding device ( 1 ), through which the waste (IN) the dryer ( 2 ) and 1.1.1.1. the dryer ( 2 ) of a heating mantle ( 3 ), by which the waste (IN) can be heated to a drying temperature of 80 ° C to 120 ° C, preferably 110 ° C, 1.1.2. in which the main reactor ( 8th ) with the dryer ( 1 ) via a material lock ( 4 ), through which the dried waste (IN) enters the main reactor ( 8th ), 1.1.3. in which the main reactor ( 8th ) of a heating mantle ( 3 ) by which the waste (IN) is heated to a temperature of 350 ° C to 420 ° C, preferably 400 ° C, 1.1.3.1. with the main reactor ( 8th ) a fluid supply ( 6 ), by means of which waste (IN) may be mixed with a molten liquid consisting of waste oil (aÖ), tar (T) and a first aggregate mixture (ZA), 1.1.4. when a further material lock ( 9 ) the main reactor ( 8th ) and the coke reactor ( 11 ) so that the waste (IN) after the reaction with the molten liquid in the coke reactor ( 11 ), 1.1.5. at the coke reactor ( 11 ) a further heating jacket ( 12 ), through which the material from the sluice ( 9 ) can be heated to a temperature of 500 ° C to 600 ° C, preferably 550 ° C using purified process exhaust gases, 1.1.5.1. in the coke reactor ( 11 ) a conveyor, preferably in the form of a screw conveyor ( 10 ), through which the reaction mixture from the material lock ( 9 ) for coke processing ( 13 - 16 ) and during which it is thermally separated in coke and gas, 1.2. the coke preparation ( 13 - 16 ) from the Kokstrenner ( 13 ), coke cleaning ( 14 ) and process water treatment ( 16 ), 1.2.1. while the Kokstrenner ( 13 ) a cooling jacket, which is supplied with cooling water (KW), wherein a line emerging from the cooling jacket, the heated water in the coke cleaning ( 14 ) and 1.2.2. In addition, the Kokstrenner ( 13 ) another material lock ( 15 ), through which the washed coke (K) can be discharged, 1.2.3. one of the coke cleaning ( 14 ) outgoing water line leads to process water treatment ( 16 ), in which the process water from the coke cleaning ( 14 ) and gas scrubbing ( 19 to 23 ) using the waste heat from the combined heat and power plant ( 18 ) into distilled water (dW) and fertilizer salts (D), 1.2.4. Finally, a gas line (G) from Kokstrenner ( 13 ) for gas treatment ( 19 to 22 ), 1.3. the gas treatment ( 19 to 24 ) from the coolers ( 19 to 21 ), a distillation ( 22 ), an oil separator ( 23 ), an oil dryer ( 24 ) as well as the clean gas storage ( 25 ), 1.3.1. in the coolers ( 19 to 21 ) with a cooling temperature of radiator 1 ( 19 ) 200 ° C, cooler 2 ( 20 ) 120 ° C and finally cooler 3 ( 21 ) to 30 ° C, the exhaust gas (G) from the Kokstrenner ( 13 ) are gradually cooled, whereby crude oil is separated from the gas, 1.3.2. from the coolers ( 19 to 21 ) lead crude oil pipes into the still ( 22 ), in which by means of the exhaust gas of the heating mantle ( 12 ) from the coke reactor ( 11 ) the crude oil can be separated into tar (T) and fuel oil, 1.3.3. a second line leads from the oil separator ( 23 ) for wastewater treatment ( 17 1.4. finally the plant as energy converter a combined heat and power plant ( 18 ), which converts the purified exhaust gases and heating oils into electrical energy and process heat. Apparatus according to claim 1, characterized in that in the cooler 1 ( 19 ) a spray device is provided, through which the gas can be additionally washed by means of a second aggregate mixture (ZB). Apparatus according to claim 1 or 2, characterized in that in the wastewater treatment ( 17 ) a third additive mixture (ZC) can be added to the wastewater, through which the wastewater can be freed from inorganic admixtures. Apparatus according to claim 1 to 3, characterized in that the first aggregate mixture (ZA) is a mineral mixture with the constituents silicon, aluminum, nitrogen, oxygen and phosphorus, whose stoichiometric composition is adapted to the pollutant content of the waste (IN). Device according to one or more of claims 1 to 4, characterized in that the second aggregate mixture (ZB) is an organic liquid having a pH of 11-13, by which the reaction of chloroaromatics and phenols to dioxin can be prevented. Device according to one or more of claims 1 to 5, characterized in that the walls of the dryer ( 2 ) with bulges ( 2a ) are provided to improve the heat transfer. Device according to one or more of claims 1 to 6, characterized in that inside the main reactor ( 8th ) Stirrers are present to improve the mixing.

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