CN1022928C

CN1022928C - Technological process and device for transforming imflammable pollutants or wastes into clean energy sources and useful products

Info

Publication number: CN1022928C
Application number: CN 88103704
Authority: CN
Inventors: 维莱里奥·托基尼兹奥
Original assignee: Individual
Current assignee: Individual
Priority date: 1987-05-28
Filing date: 1988-06-20
Publication date: 1993-12-01
Anticipated expiration: 2003-06-20
Also published as: CN1038830A

Abstract

The present invention relates to a technological process for converting combustible pollutants and wastes into pure energy sources and utilizable products. The present invention is characterized in that materials which are to be processed in a hot spray pipe in the atmosphere of no air, and the materials are completely decomposed and extracted to obtain combustible gases, non-combustible gases and inert gases. The thermal decomposition products are cooled by water, inert products are separated from the water, and simultaneously, steam is generated. The steam and the cooled gases are introduced into a heated carbonaceous material in order to filter the gases and partially convert the gases to obtain hydrogen, carbon monoxide and other useful gas products, and the gas products are cooled.

Description

Technological process and device for transforming imflammable pollutants or wastes into clean energy sources and useful products

The present invention relates to a kind of technological process and device that flammable pollutent or refuse is transformed into the clean energy and useful product.

As you know can be by under the condition of controlled temperature and excess air, making waste material oxidation such as municipal wastes or industrial waste one class, thus the high temperature that makes it to produce thermolysis and utilize flue gas obtains heat energy and electric energy.

But the existing technology of this processing waste recovery energy can only reach mid-efficiency, and can discharge combustible material and a spot of pollutent.

The objective of the invention is to eliminate this shortcoming, make in flammable pollutent or refuse are changed and to reclaim whole energy, and obtain the clean energy and useful product, thereby benefit resident, society and help environment.

Purpose of the present invention also is in order to handle city, industry and the agriculture various types of waste materials that produce, particularly solid waste, black liquor residue (black liquor sludge) and flammable pollutent or the like.

Purpose of the present invention also is to adopt a kind ofly can regain the processing waste material of its manufacturing cost and the device of flammable pollutent rapidly.

Purpose of the present invention also is in order to obtain useful product in industry, construction industry and agricultural etc. from waste disposal.

According to the present invention, by a kind of flammable pollutent or waste material are transformed into the technological process of the clean energy and useful product, can reach these purposes and other following result.Being characterized as of described technological process:

The material that desire is handled is handled under airfree atmosphere, to make it to decompose fully and therefrom extract combustible gas, not combustion gas and rare gas element in hot jet pipe;

Water cooling heat degradation production is also therefrom isolated inert products, produces steam simultaneously,

This steam and the described gas that is cooled are incorporated in a kind of warmed-up carbonaceous material, also partly it are changed to obtain hydrogen, carbon monoxide and other useful gaseous product so that filter this gas; And

This gaseous product is cooled off.

In order to implement this method, the present invention includes a kind of device, this device comprises:

A kind of hot jet pipe decollator, this decollator is operated under airfree situation, handled material is decomposed fully so that extract inflammable gas, non-flammable gas and rare gas element;

A kind of water separator is in order to isolate and to produce steam with gas from rare gas element;

A kind of strainer-thermal reactor, in carbonaceous material arranged and be connected with separator with above-mentioned decollator, be used for filtering the gaseous product that decollator and separator come, make them change into hydrogen, carbon monoxide and other useful gaseous product fully; And a kind of water cooler that is used for this gaseous product.

The following drawings further specifies the present invention, and wherein Fig. 1 shows the block flow diagram of the inventive method; Fig. 2 signal has shown the device of implementing present method; Fig. 3 has provided the total figure that adopts the workshop of apparatus of the present invention; Fig. 4 is the enlarged view of Fig. 3 details.

As can be seen from Figure 1, flow process of the present invention is as follows: handled material is introduced decollator 1, in this effect owing to oxygen hydrogen flame 2, and produce thermolysis completely, so that next step is separated into inflammable gas, non-flammable gas and rare gas element.

Mainly constituted from decollator 1 effusive mixture by carbonic acid gas, hydrogen, carbon monoxide, water vapor and waste liquid.Mixture is fed in a large amount of water 3, cool off, and waste liquid is changed into inert solid (particle), water is heated simultaneously, and produces steam.

Isolated inert solid can be used for various uses (as being used for construction industry), and gas and vapour mixture then enter in the strainer-thermal reactor 4 that contains carbonaceous material.

There, carbon and steam reaction form carbon monoxide and hydrogen and purify and change other gas.Because steam and carbon reaction are endothermic reactions, its required heat is from decollator 1.

This gas is hydrogen through behind strainer-thermal reactor 4, carbon monoxide and other useful gaseous product.

Then, these gases cool off in heat exchanger, through purifying and introducing umformer 39 later on steam humidifying, are transformed into carbonic acid gas and hydrogen and are cooled to about 200 ℃ under the situation that this carbon monoxide and steam are having appropriate catalyst to exist.

Then, gas cooling is cured to-70 ℃ of carbonic acid gas, hydrogen is then by strainer 49, latter's available fuel battery, next life the electrogenesis energy.

As in umformer 39, using other catalyzer, then carbon monoxide and hydrogen can be changed into methane or make hydrogen and nitrogen in conjunction with and obtain ammonia.

This process can realize by the device that adopts Fig. 2 and Fig. 3 signal.

As shown in these figures, device of the present invention has a decollator, oxyhydrogen flame 2 is arranged and by waste material pipe and pulverizing in the decollator, sorting, and devices such as drying connect.

This pipe connecting 6 and two mercury valves 7,8 connect.

These valves have cylindrical shell 9, at its top hydraulic efficiency piston 10 are arranged, be used for driving " lid " 11 with

close outlet pipe

12,12 '.

Sealing " lid " 11 partly is soaked in the mercury 13, and this mercury is stored in the space 14 (and be connected with expansion chamber 15).

Inlet tube 6 has the oblique door 16 that is driven by hydraulic efficiency piston 17, and a protrusion position 18 is arranged on the top, when the latter opens at Xie Men, plays a part the corresponding space 14 of protection.

The top of the connecting leg 12 between two mercury valves 7,8 have an off-gas pump 19 '.

(another) off-gas pump 19 " is connected with decollator 1 by pipe 19.

Second mercury valve 8 times, pipe 12 ' be divided into several arms to be connected with oxyhydrogen flame decollator 1.

This decollator 1 is to make with refractory materials, and is arch basically.Its arched cover board 20 supports a plurality of hydraulic efficiency pistons 21, in decollator 1, and these piston driven annular stock pushers 22.Cover plate 20 is also supporting hot jet pipe 23.

Stock pusher 22 is along jet pipe 23 coaxial operations, and its limit position matches with annular neck portion 24 in the decollator 1.

The bottom 25 of decollator 1 is protruding upward a little to keep certain amount of fluid, and it has mesopore 26 and is used to carry degradation production, also has the spiral coil 27 that links to each other with the heat exchanger (not shown).

Decollator 1 is placed in cylindrical circular basically carbonaceous strainer-thermal reactor 4.

For attal, strainer-thermal reactor 4 has outer tube 28, and there are two mercury valves identical with above-mentioned valve 7,8 upper end of outer tube 28.

Strainer-reactor is coaxial to be placed in the water cooler similar to its shape 29, and two coaxial moisture films 30,31 that produced by two circular holes on the cover plate 32 of water cooler 29 are wherein arranged.

Cover plate 32 has that two concentric annular walls 33,34 are used for being filled with water and condensation is positioned at the bottom of described concentric structure from water-filled groove 3() steam of the annular space that passes through described water cooler 29 35 that comes.

Spiral tube 36 is arranged in the receiving tank, and this coil pipe is connected with the heat exchanger (not shown), and travelling belt 37 will deposit to the material of case 3 bottoms and remove.

The exit end of this travelling belt 37 is positioned between two mercury valves (identical with mercury valve above-mentioned).

Pipe 38 on water cooler 29 bottoms makes water cooler be connected with several concentric regions 40 of umformer 39.The catalyzer that described each concentric regions is had nothing in common with each other, catalyzer is determined according to desired exit gas.This concentric regions 40 has water spouting nozzle (not shown) and feeding device 41, and they just link to each other with filling tube 28 like this.

The bottom of the concentric regions 40 of umformer 39 also has dumping device 42.

Umformer 39 43 is connected on the refrigerator 44 by pipe, and the latter is by coil pipe 45 coolings that are connected with common heat pump (not shown).Also be furnished with the refuse of stock pusher 46 with drain along skewed slot 47 ice and reaction in the bottom of water cooler 44.

The travelling belt 48 of skewed slot 47 bottoms is transported to the ice of skewed slot 47 outside the equipment.

Refrigerator 44 connects self-stip hydrogenous filters 49, and the latter is identical with the above-mentioned mercury valve of mentioning by having mercury valve 51(again) pipe 50 lead to the device outside.

Whole device is included in and is filled with rare gas element (as CO ₂) housing 52 in so that avoid air to infiltrate in the device to guarantee its safety.

According to the present invention, the operation scheme of this device is as follows:

Be transported in the mercury valve 7 by managing 6 through suitable processing, pulverizing, sorting and exsiccant material.

In the interval, hydraulic efficiency piston 10 will cover 11 and rise at the fixed time, and the through hole of opening pipe 12 makes the mercury 13 that overflows into chamber 15 flow back into space 14.

When lid 11 rose fully, the oblique door 16 that is driven by hydraulic efficiency piston 17 began to descend.The convex part 18 at door 16 tops is closed space 14 preventing and from the material of valve 7 this space is full of.

When the material of requirement had passed through, door 16 was closed pipe 6 again, covered 11 simultaneously and closed pipe 12 again.

After finishing above two operations, manage pump 19 on 12 tops ' begin to start, will extract out with the air that the material of handling is come in through valve 7.

After pipe has rebulid vacuum in 12, mercury valve with as valve 7 with the sampling device unlatching, make material by managing 12 ' entering decollator 1.

When valve 8 is opened, the gas in the decollator can enter pipe 12 ' in, " extract out and send back in the decollator but these gases will be by off-gas pump 19 ' by managing 19.

The accumulative material is pushed annular neck 24 to by stock pusher 22 it is transported away in decollator.

In this operation, material contacts with hot jet pipe 23 its cooling, and plays a part stopper for following dispersing chamber 53.

Like this, partly be blocked, avoid high thermo-contact with 2000 ℃ of oxyhydrogen flames with the top of protection decollator 1 from this dispersing chamber escaping gas.

Because the gradient oxyhydrogen flame 2 of inlet pipe has special shape, decompose thereby make compression material by neck 24 carry out four times, be at the flame head for the first time, second and third, be at afterbody four times, shown in Fig. 2 intermittent line.

The material part that decomposes compiles in the bottom 13 of decollator 1, thereby makes it avoid contacting with the direct of flame.

After further decomposing, fluent meterial and the gas by neck 24 fall into and are full of the water groove 3 of (being kept at a certain temperature by coil pipe 36).Transfer out and discharging outside equipment by travelling belt 37 by the solid particulate that is settled out in the water 3.

The water vapor of a part of cooling degradation production produces steam, and with CO, CO ₂Mix Deng gas.These gases enter in strainer-thermal reactor 4 by managing 54, and the latter is by pipe 28 filling carbonaceous materials.In strainer-thermal reactor 4, the carbon in the carbonaceous material since from decollator 1 absorb heat and and gas reaction, thereby produce carbon monoxide and hydrogen and further Purge gas.

The gas that obtains thus enters water cooler 29 by managing 55, is cooled by moisture film 30 and 31 at this, becomes stable and is further purified, and adjusts H simultaneously ₂The ratio of O/CO.Enter through cooling and the gas of humidification and to have in which floor catalyzer umformer 39, the first layer catalyst component is Fe ₂O ₃-Cr ₂O ₃, the component of the second layer and the 3rd layer of catalyzer is Cu-ZnO-AC ₂O ₃In the first layer, thermopositive reaction makes gas temperature be raised to 450 ℃; Before entering the second layer, spray water so that gas cooling to 180 ℃.

In the second layer, the temperature of gas is raised to 250 ℃; Water spray carries out intercooling, makes to enter trilaminar temperature and be reduced to 200 ℃.

The gas that contains a large amount of hydrogen leaves last one deck in 220 ℃, enters deep freezer 44, makes its temperature drop to-70 ℃ approximately.

The bottom solid carbon dioxide (dry ice) that in deep freezer 44 ingress is deep freezer is discharged by stock pusher 46.After by self-purification strainer 49 and mercury valve 51, Last gas is pure hydrogen, and it is outer for use that it is sent device.

The following examples further describe the present invention.

By manage 6,12 and 12 ', the city and the industrial waste that will have the 780kg/h of following essentially consist are introduced decollator:

Carbon 44.46%

Hydrogen 9.89%

Nitrogen 1.62%

Oxygen 35.84%

Sulphur 1.33%

Chlorine 0.83%

Other is 6.03% years old

Carry out the required O of pyrolysated oxyhydrogen flame ₂Be that 526 kilograms of/hour water are 287 kilograms/hour.

Required purity oxygen is provided by device external dedicated oxygenerator, and hydrogen is provided by device itself.

After the contained water sections evaporation of cooling tank 3, from 1400 ℃ of gases of the outlet of decollator 1, contain steam by water vapor in the cooling tank 3, its volumetric flow rate is 2598Nm ³/ h, its component is as follows:

CO 22.3%

Hydrogen 44.4%

CO ₂2.3%

H ₂O 29%

Other trace

65kg/h inert solid refuse is deposited in the tank 3.

Thermolysis produces carbon black fully and not.

Its heat recovery rate of the temperature of decollator 1 and refractory materials thereof very high (2000 ℃) is 50,000Kcal/h.

2598Nm ³The gas of/h enters strainer-thermal reactor 4 by managing 54, and the coke reaction of this gas and 238kg/h obtains 3023Nm ³The gas of/h with following composition:

CO 32.8%

Hydrogen 56.2%

H ₂O 11%

Other trace

Thereby these gases were cooled to 380 ℃ from 800 ℃ and make it stable before entering umformer 39.

The steam of having used the water of 607kg/h and 1098kg/h in process of cooling is to readjust H ₂The ratio of O/CO.

3467Nm ³/ h, temperature are that 380 ℃ the gas that contains a large amount of water vapors enters and contains Fe ₂O ₃-Cr ₂O ₃The first layer of umformer 39, carry out thermopositive reaction, make its temperature be elevated to 450 ℃.

Contain Cu-ZnO-Al entering ₂O ₃Second Catalytic Layer before, gas is by water cooling to 180 ℃, its heat recovery rate is 2000Kcal/h.

In second Catalytic Layer, the temperature of gas is elevated to 250 ℃; Allowing heat recovery rate is 94, and the internal cooling technology of 000Kcal/h makes that trilaminar temperature in is 200 ℃.

Flow out 5145Nm from umformer 39 with following composition ³/ h(220 ℃) gaseous mixture.

Hydrogen 49.8%

CO 20%

H ₂O 28%

Hydrogen-rich gas is from umformer 39(220 ℃) flow out, enter deep freezer 44, be cooled to-70 ℃.

The CO of 2077kg/h ₂Collect in the bottom of deep freezer 44 with the form of dry ice, transport by travelling belt 48.Also reclaim the hydrogen of 229kg/h from same deep freezer 44, wherein 66kg/h is used for the oxyhydrogen flame 2 of decollator 1, and 163kg/h is outer the confession.For example, if this hydrogen is used for fuel cell, just can obtain the output rating of about 2600Kwh/.

Be clear that from above, provide multiple advantage according to method of the present invention and the device of implementing this method, specifically:

The clear energy sources high productivity;

All reclaim secondary product;

Security is the highest;

Pollution-free;

Investment can be reclaimed rapidly;

Can make equipment be transformed into free of contamination efficient propelling system, as eliminating the device that pollutes.

Claims

1, a kind of technological process that flammable pollutent or refuse is transformed into clear energy sources and can utilizes product is characterized in that:

Under the airfree atmosphere material to be processed is being handled in hot jet pipe to reach required result's base temperature, to make it all to decompose and extract combustible gas, not combustion gas and rare gas element;

Water cooling heat degradation production is also separated inert products in the water, produces steam simultaneously;

This steam and described cold gas are guided in a kind of warmed-up carbonaceous material, also partly their are changed to obtain hydrogen, carbon monoxide and other useful gaseous product so that filter this gas; And

Cool off described gaseous product.

2,, it is characterized in that using from the handled material of heat preheating of different refrigerating work procedures and make it reach suitable temperature according to the technological process of claim 1.

3, by the technological process of claim 1, this material is compressed to it is characterized in that making material to be processed to handle before in hot jet pipe (23).

4,, it is characterized in that compressing material to be processed and realize by forcing described material to enter decomposition chamber (53) by ingate (24) by the technological process of claim 3.

5, by the technological process of claim 1, the thermolysis that it is characterized in that material to be processed is that a kind of oxyhydrogen flame (2) is realized.

6,, it is characterized in that material to be processed is several times by oxyhydrogen flame (2) by the technological process of claim 5.

By the technological process of claim 1, it is characterized in that in the process of thermolysis material to be processed that 7, the tectum of decomposition chamber (53) bottom (25) is by the substance protection of former decomposition.