CN106395826A - System and method for processing waste electronic products - Google Patents
System and method for processing waste electronic products Download PDFInfo
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- CN106395826A CN106395826A CN201610750704.XA CN201610750704A CN106395826A CN 106395826 A CN106395826 A CN 106395826A CN 201610750704 A CN201610750704 A CN 201610750704A CN 106395826 A CN106395826 A CN 106395826A
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- 239000002699 waste material Substances 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 29
- 238000012545 processing Methods 0.000 title claims abstract description 8
- 238000000197 pyrolysis Methods 0.000 claims abstract description 161
- 239000005997 Calcium carbide Substances 0.000 claims abstract description 111
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 claims abstract description 111
- 238000000926 separation method Methods 0.000 claims abstract description 66
- 239000007787 solid Substances 0.000 claims abstract description 43
- 238000000746 purification Methods 0.000 claims abstract description 37
- 238000004519 manufacturing process Methods 0.000 claims abstract description 36
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 31
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 31
- 239000002994 raw material Substances 0.000 claims abstract description 25
- 238000002156 mixing Methods 0.000 claims abstract description 24
- 229910052755 nonmetal Inorganic materials 0.000 claims abstract description 23
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims abstract description 9
- 229910052791 calcium Inorganic materials 0.000 claims abstract description 9
- 239000011575 calcium Substances 0.000 claims abstract description 9
- 238000007599 discharging Methods 0.000 claims abstract description 9
- 239000007789 gas Substances 0.000 claims description 180
- 239000000126 substance Substances 0.000 claims description 26
- 238000006243 chemical reaction Methods 0.000 claims description 22
- 238000001816 cooling Methods 0.000 claims description 14
- 238000002485 combustion reaction Methods 0.000 claims description 13
- 239000003575 carbonaceous material Substances 0.000 claims description 11
- 239000007788 liquid Substances 0.000 claims description 10
- 239000000446 fuel Substances 0.000 claims description 9
- 239000000428 dust Substances 0.000 claims description 8
- 230000002378 acidificating effect Effects 0.000 claims description 7
- 229910052736 halogen Inorganic materials 0.000 claims description 7
- 150000002367 halogens Chemical class 0.000 claims description 7
- 239000002245 particle Substances 0.000 claims description 7
- 239000003513 alkali Substances 0.000 claims description 6
- 230000035484 reaction time Effects 0.000 claims description 6
- 238000005406 washing Methods 0.000 claims description 6
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 4
- 235000019738 Limestone Nutrition 0.000 claims description 4
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 4
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 4
- 239000000920 calcium hydroxide Substances 0.000 claims description 4
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 4
- 235000011116 calcium hydroxide Nutrition 0.000 claims description 4
- 239000004571 lime Substances 0.000 claims description 4
- 239000006028 limestone Substances 0.000 claims description 4
- 239000002893 slag Substances 0.000 claims description 4
- 239000000571 coke Substances 0.000 claims description 2
- 238000007885 magnetic separation Methods 0.000 claims description 2
- 239000007800 oxidant agent Substances 0.000 claims 2
- 230000001590 oxidative effect Effects 0.000 claims 2
- 230000008569 process Effects 0.000 abstract description 9
- 239000000203 mixture Substances 0.000 abstract description 7
- 238000004064 recycling Methods 0.000 abstract description 7
- 239000000463 material Substances 0.000 abstract description 5
- 238000007781 pre-processing Methods 0.000 abstract description 4
- 238000011084 recovery Methods 0.000 abstract description 3
- 239000000047 product Substances 0.000 description 120
- 239000003921 oil Substances 0.000 description 45
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 28
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 14
- 229910002091 carbon monoxide Inorganic materials 0.000 description 14
- 229910052739 hydrogen Inorganic materials 0.000 description 14
- 239000001257 hydrogen Substances 0.000 description 14
- 229910052751 metal Inorganic materials 0.000 description 14
- 239000002184 metal Substances 0.000 description 14
- 239000002585 base Substances 0.000 description 12
- 150000002431 hydrogen Chemical class 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 9
- 239000005416 organic matter Substances 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 7
- 239000000295 fuel oil Substances 0.000 description 6
- 150000002739 metals Chemical class 0.000 description 6
- 238000004939 coking Methods 0.000 description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 230000005294 ferromagnetic effect Effects 0.000 description 4
- 239000003365 glass fiber Substances 0.000 description 4
- 239000007921 spray Substances 0.000 description 4
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 239000010813 municipal solid waste Substances 0.000 description 3
- 230000004075 alteration Effects 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000009854 hydrometallurgy Methods 0.000 description 2
- 238000005272 metallurgy Methods 0.000 description 2
- 239000011368 organic material Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229920000915 polyvinyl chloride Polymers 0.000 description 2
- 239000004800 polyvinyl chloride Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000012265 solid product Substances 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- XTXRWKRVRITETP-UHFFFAOYSA-N Vinyl acetate Chemical compound CC(=O)OC=C XTXRWKRVRITETP-UHFFFAOYSA-N 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 239000010793 electronic waste Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000003822 epoxy resin Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000007769 metal material Substances 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 229920000647 polyepoxide Polymers 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000007158 vacuum pyrolysis Methods 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
- F23G5/033—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment comminuting or crushing
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
- F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a system and method for processing waste electronic products. The system comprises a preprocessing unit, a separation unit, a pyrolysis unit, a mixing unit, an oil-gas separation and purification unit and a calcium carbide production unit. The method using the system to process the waste electronic products comprises the following steps: 1, preprocessing: disassembling and crushing the waste electronic products; 2, separating: carrying out fine crushing and sorting separation on the above obtained preprocessing product to obtain a nonmetal product; 3, pyrolyzing: pyrolyzing the nonmetal product to generate a high-temperature oil gas and a solid carbon-containing material, collecting the high-temperature oil gas, and discharging the solid carbon-containing material; 4, mixing: mixing the solid carbon-containing material with a calcium-based raw material; 5, separating and purifying the oil gas: separating the high-temperature oil gas to obtain uncondensed gas, and processing the uncondensed gas to obtain pyrolysis gas; and 5, producing calcium carbide: reacting a mixture obtained in step 4 to obtain calcium carbide. The system and the method, which couple the recovery of the waste electronic products with production of calcium carbide, realize recycling of the waste electronic products, and reduce the production cost of calcium carbide.
Description
Technical Field
The invention belongs to the field of solid waste recycling treatment, and particularly relates to a system and a method for treating waste electronic products.
Background
With the rapid development of science and technology, waste electronic products and leftover materials formed in the processing process of the electronic products are increasing day by day. Annual yields of electronic waste in developed countries such as japan, the usa and the european union account for 1%, 2-5% and 4% of municipal waste, respectively, and increase at a rate of 16% -28% per 5 years, which is 3-5 times the rate of municipal waste growth. The situation is particularly serious in China, the population of China is large, and the China is also a main place for dumping electronic garbage in developed countries, data shows that 80% of electronic garbage in the United states is exported to Asia, and 90% of the electronic garbage enters China.
The technology for recycling and treating the waste circuit boards at home and abroad mainly comprises a mechanical physical separation method, a hydrometallurgy technology, a biological metallurgy technology and a pyrolysis technology, and most of the technologies pay attention to recycling metal in the waste printed circuit boards except for pyrolysis. The mechanical physical separation method is easy to scale, relatively causes little pollution to the environment, but various metals cannot be thoroughly separated, and the residual organic matters are buried or burned, so that resources are wasted and the environmental pollution is serious; the metal recovery rate of hydrometallurgy is high, but the consumption of chemical reagents is large, the process is complex, and the high molecular organic compounds in the circuit board are not recycled; the biological metallurgy technology is still in the research stage at present, and suitable bacteria are few and are difficult to culture; in comparison, through the combination of pyrolysis technology pyrolysis and physical separation methods, the metal in the waste electronic products can be effectively recovered, and the high molecular organic materials in the waste electronic products can be utilized to decompose the metal into fuel oil, fuel gas and carbide.
The chemical name of calcium carbide, colorless crystal, is mainly used for producing acetylene gas, and has been called as the mother material of organic synthesis industry. Acetylene is an important chemical raw material and is mainly used for producing polyvinyl chloride and vinyl acetate products, 70 percent of the raw material acetylene for producing PVC products in China is from calcium carbide, the calcium carbide has very important effect on the economic development of China, the yield is continuously increased in more than ten years, and the yield reaches over 2200 million tons in 2013.
The production process of calcium carbide mainly comprises an electric heating method and an oxygen heating method.
In addition, because the heat release amount of the unit carbon-containing fuel in incomplete combustion is small, a large amount of carbon-containing fuel needs to be combusted to supply heat, more ash is generated and is enriched into a calcium carbide product, and the quality of the calcium carbide product is greatly influenced. How to reduce the production cost of calcium carbide and increase the income of calcium carbide enterprises becomes one of the development problems of the calcium carbide industry in China.
At present, a simple pyrolysis method is generally adopted for treating waste electronic products, a method for recovering metals after pyrolysis is provided, but the method neglects the utilization of pyrolysis gas, pyrolysis carbon and other products in the pyrolysis process, does not achieve the maximization of resource utilization, and simultaneously, the vacuum pyrolysis has high requirements on equipment, so that the industrialization is difficult to realize.
As can be seen from the above, the following problems exist in the prior art: the recycling level of the non-metallic substances is not enough in the waste electronic product treatment; pyrolysis treatment of waste electronic products is mostly used as a pretreatment means, and subsequent utilization technology of pyrolysis products is lacked; the production of calcium carbide needs a large amount of coke and heat energy/electric energy, and has high raw material cost and high energy consumption; the ash after the combustion by the oxygen thermal method is enriched in the calcium carbide product, and the quality of the calcium carbide product is influenced.
Disclosure of Invention
In order to solve the problems, the invention aims to couple the resource recycling treatment of the waste electronic products with the calcium carbide production process, provide heat for the calcium carbide production by utilizing pyrolysis gas generated by pyrolyzing the waste electronic products, and simultaneously realize the purposes of resource recycling of the waste electronic products, reduction of the calcium carbide production cost and reduction of the ash content of the calcium carbide.
In order to achieve the above object, the present invention provides a system for processing waste electronic products, comprising: a pretreatment unit, a separation unit, a pyrolysis unit, a mixing unit, an oil-gas separation and purification unit and a calcium carbide production unit,
the pretreatment unit comprises a disassembly unit and a crushing unit, the disassembly unit comprises a waste electronic product inlet and a disassembly product outlet, the crushing unit comprises a disassembly product inlet and a pretreatment product outlet, and the disassembly product inlet is connected with the disassembly product outlet;
the separation unit comprises a pretreatment product inlet and a nonmetal product outlet, and the pretreatment product inlet is connected with the pretreatment product outlet;
the pyrolysis unit comprises a non-metal product inlet, a solid carbon-containing substance outlet and a high-temperature oil gas outlet, and the non-metal product inlet is connected with the non-metal product outlet;
the mixing unit comprises a solid carbonaceous inlet, a calcium-based raw material inlet and a mixed product outlet, and the solid carbonaceous inlet is connected with the solid carbonaceous outlet;
the oil-gas separation and purification unit comprises a high-temperature oil-gas inlet and a pyrolysis gas outlet, and the high-temperature oil-gas inlet is connected with the high-temperature oil-gas outlet;
the calcium carbide production unit comprises a pyrolysis gas inlet, a mixed product inlet and a calcium carbide product outlet, wherein the pyrolysis gas inlet is connected with the pyrolysis gas outlet, and the mixed product inlet is connected with the mixed product outlet.
Specifically, the separation unit is one or a combination of an air separation unit, a magnetic separation unit or an electrostatic separation unit; and a sealed discharging device is arranged at the solid carbon-containing substance outlet.
Further, the calcium carbide production unit comprises a calcium carbide tail gas outlet; the system further comprises a gas purification and dust removal unit, wherein the gas purification and dust removal unit comprises a calcium carbide tail gas inlet, and the calcium carbide tail gas inlet is connected with the calcium carbide tail gas outlet.
Furthermore, the calcium carbide production unit also comprises a combustion-supporting gas inlet, and combustion-supporting gas is introduced into the auxiliary pyrolysis gas through the combustion-supporting gas inlet for combustion; the oil-gas separation and purification unit further comprises a pyrolysis oil outlet.
The invention also provides a method for treating the waste electronic products, which comprises the following steps:
a, pretreatment: disassembling and crushing the waste electronic products in the pretreatment unit to obtain a pretreatment product;
b, separation: finely crushing, sorting and separating the pretreated product to obtain a nonmetal product;
c, pyrolysis: feeding the nonmetal products into the pyrolysis unit for pyrolysis reaction to generate high-temperature oil gas and solid carbon-containing substances, wherein the high-temperature oil gas is collected through an oil gas pipeline arranged in the pyrolysis furnace, and the solid carbon-containing substances are discharged through an outlet;
d, mixing: mixing the solid carbonaceous material with a calcium-based raw material to obtain a mixed product;
e, oil-gas separation and purification: separating the high-temperature oil gas into non-condensable gas and condensable liquid through direct cooling or indirect cooling in the oil-gas separation and purification unit, wherein the non-condensable gas is treated to obtain pyrolysis gas;
f, calcium carbide production: and (3) feeding the mixed product into a calcium carbide furnace for reaction to obtain the calcium carbide after the reaction is finished.
Specifically, in the step F, the pyrolysis gas in the step E is used as a fuel, and a plurality of electrodes and a plurality of burners are combined to be a heat source of the calcium carbide furnace, so as to perform a reaction in the calcium carbide furnace; and adding combustion-supporting gas into the pyrolysis gas to assist combustion.
As a preferred embodiment, the particle size of the non-metallic product in step B is controlled to be 0.5 to 100 mm; and D, the calcium-based raw material in the step D is one or more selected from lime, limestone, hydrated lime or carbide slag.
Further, the temperature of the pyrolysis reaction in the step D is 450-; and F, controlling the reaction temperature of the calcium carbide furnace to be 1700-2200 ℃ and the reaction time to be 5-50 min.
Further, the pyrolysis gas in the step E is obtained by removing acidic harmful gases such as halogen and the like from the non-condensable gas through alkali washing and electric coking; and D, directly hot charging the solid carbon-containing substance in the step F into a calcium carbide furnace, wherein the hot charging temperature of the solid carbon-containing substance is 350-750 ℃.
By utilizing the system and the method, the resource recovery treatment of the waste electronic products and the calcium carbide production process are coupled together, and the waste electronic product pyrolysis gas is utilized to provide heat for the calcium carbide production, so that the following effects are achieved:
(1) the clean and efficient resource treatment of waste electronic products is realized;
(2) the high-value utilization of the pyrolysis products of the waste electronic products is realized;
(3) the raw materials with low price can be used, so that the cost of the raw materials for calcium carbide production is reduced;
(4) the byproduct pyrolysis gas is burnt to be used as a supplementary heat source for calcium carbide generation, so that the power consumption is reduced;
(5) the pyrolysis solid product is thermally sent into a calcium carbide furnace, so that the heating energy consumption is reduced;
(6) the combustion pyrolysis gas has no ash content and has no influence on the quality of the calcium carbide product.
Additional aspects and advantages of the invention will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice of the invention.
Drawings
Fig. 1 is a schematic structural diagram of a system for processing waste electronic products according to the present invention.
Fig. 2 is a process flow diagram of the present invention for treating waste electronic products.
Detailed Description
The following detailed description of the present invention, taken in conjunction with the accompanying drawings and examples, is provided to enable the invention and its various aspects and advantages to be better understood. However, the specific embodiments and examples described below are for illustrative purposes only and are not limiting of the invention.
In one aspect of the invention, the invention provides a system for treating waste electronic products, which comprises a pretreatment unit, a separation unit, a pyrolysis unit, a mixing unit, an oil-gas separation and purification unit and a calcium carbide production unit:
a, pretreatment: disassembling and crushing the waste electronic products in the pretreatment unit to obtain a pretreatment product;
b, separation: finely crushing, sorting and separating the pretreated product to obtain a non-metal product, wherein the particle size of the non-metal product is controlled to be 0.5-100 mm;
c, pyrolysis: uniformly feeding the non-metal product into a pyrolysis furnace for pyrolysis reaction at the pyrolysis temperature of 450-850 ℃ for 0.5-3h, generating high-temperature oil gas and solid carbon-containing substances after the pyrolysis reaction is completed, collecting the high-temperature oil gas through an oil gas pipeline arranged in the pyrolysis furnace, and discharging the solid carbon-containing substances through a sealed discharging device;
d, mixing: mixing the solid carbonaceous material with a calcium-based raw material to obtain a mixed product;
e, oil-gas separation and purification: and the high-temperature oil gas collected in the pyrolysis unit enters a separation and purification unit, and the separation and purification comprises one or more of direct cooling, indirect cooling, halogen and other acidic harmful gas removal, electric tar capture, desulfurization and oil-water separation, so that clean pyrolysis gas and pyrolysis oil are obtained. The pyrolysis gas is collected and sent into a carbide production unit, the yield of the pyrolysis gas is 5% -15%, and the pyrolysis gas is rich in hydrogen, methane, carbon monoxide and the like and can be directly combusted to supply heat. The pyrolysis oil is collected and sold as fuel oil or chemical products, and the yield of the pyrolysis oil is 10-25%;
f, calcium carbide production: because the nonmetal in the waste electronic product is mostly high molecular organic materials such as epoxy resin, the solid carbonaceous material ash content after pyrolysis is low, the fixed carbon content is high, and the method is suitable for being used as a carbon-based raw material for calcium carbide production. Mixing the solid carbonaceous material from the pyrolysis unit with a calcium-based raw material (one or a mixture of lime, limestone, hydrated lime or carbide slag) and feeding the mixture into a calcium carbide furnace, wherein the hot feeding temperature of the solid carbonaceous material is 350 ℃ and 750 ℃. The calcium carbide furnace adopts a combination of a plurality of electrodes and a plurality of burners to provide a heat source for calcium carbide raw materials. The combustor is used as a supplementary heat source of the electrode, the fuel is pyrolysis gas from the oil-gas separation and purification unit, supplementary combustion-supporting gas is combusted, the pyrolysis gas is rich in hydrogen, methane and carbon monoxide, combustion products are ash-free, and the quality of calcium carbide products cannot be reduced. The temperature of the calcium carbide furnace is 1700-.
The invention will now be described with reference to specific examples, which are intended to be illustrative only and not to be limiting in any way.
Example 1
This embodiment provides a system for handle old and useless electronic product, this system includes preprocessing unit, separation element, pyrolysis unit, mixing unit, oil-gas separation purification unit and carbide production unit:
a, pretreatment: and in the pretreatment unit, the waste electronic products are disassembled and crushed to obtain a pretreatment product.
B, separation: finely crushing the pretreated product, magnetically separating ferromagnetic metal, and performing air separation and electrostatic separation to obtain other metals, glass fiber and non-metallic organic matter, wherein the content of the non-metallic organic matter is 37%, and the particle size of the non-metallic organic matter is controlled to be 100 mm.
C, pyrolysis: and feeding the nonmetal products into a pyrolysis furnace uniformly for carrying out pyrolysis reaction, wherein the pyrolysis temperature is 550 ℃, the pyrolysis time is 3 hours, high-temperature oil gas and solid carbon-containing substances are generated after the pyrolysis reaction is completed, the high-temperature oil gas is collected through an oil gas pipeline arranged in the pyrolysis furnace, and the solid carbon-containing substances are discharged through a sealed discharging device.
TABLE 1 solid carbonaceous essential Properties
D, mixing: and mixing the solid carbonaceous material with a lime raw material to obtain a mixed product.
E, oil-gas separation and purification: the high-temperature oil gas collected in the pyrolysis unit enters a separation and purification unit, is separated into non-condensable gas and condensable liquid through direct cooling, the non-condensable gas is subjected to alkali washing to remove acidic harmful gases such as halogen and the like, and the pyrolysis gas is obtained after electric coking. The condensable liquid enters an oil-water separation tank to obtain pyrolysis oil, and the separated pyrolysis water is partially recycled as direct cooling spray. The pyrolysis gas is collected and sent into a carbide production unit, the yield of the pyrolysis gas is 15%, and the pyrolysis gas is rich in hydrogen, methane, carbon monoxide and the like and can be directly combusted to supply heat. The pyrolysis oil is collected and sold as fuel oil or chemical products, and the yield of the pyrolysis oil is 15%. The content of the pyrolysis gas is as follows:
TABLE 2 pyrolysis gas composition and heating value
| Hydrogen/%) | Methane/% | Carbon monoxide/%) | Carbon dioxide/%) | CnHm/％ | Calorific value kcal/Nm3 |
| 41.47 | 11.63 | 10.27 | 35.47 | 1.16 | 2635 |
F, calcium carbide production: the temperature of the mixed product heat sent to the calcium carbide furnace is 350 ℃. The calcium carbide furnace adopts a combination of a plurality of electrodes and a plurality of burners to provide a heat source for calcium carbide raw materials. The combustor is used as a supplementary heat source of the electrode, the fuel is pyrolysis gas from the oil-gas separation and purification unit, supplementary combustion-supporting gas is combusted, the pyrolysis gas is rich in hydrogen, methane and carbon monoxide, combustion products are ash-free, and the quality of calcium carbide products cannot be reduced. The temperature of the calcium carbide furnace is 1700 ℃, the reaction time is 50min, the calcium carbide tail gas enters the gas purification and dust removal unit, the calcium carbide product is discharged from the discharge hole, the calcium carbide content in the calcium carbide product is 78.43%, and the gas evolution quantity is 287L/kg.
Example 2
This example is the same as the system used in example 1 above, but with different process conditions, as follows:
a, pretreatment: and in the pretreatment unit, the waste electronic products are disassembled and crushed to obtain a pretreatment product.
B, separation: finely crushing the pretreated product, magnetically separating ferromagnetic metal, and performing air separation and electrostatic separation to obtain other metals, glass fiber and non-metallic organic matter, wherein the content of the non-metallic organic matter is 38%, and the particle size of the non-metallic organic matter is controlled to be 50 mm.
C, pyrolysis: and feeding the nonmetal products into a pyrolysis furnace uniformly for carrying out pyrolysis reaction, wherein the pyrolysis temperature is 450 ℃, the pyrolysis time is 2 hours, high-temperature oil gas and solid carbon-containing substances are generated after the pyrolysis reaction is completed, the high-temperature oil gas is collected through an oil gas pipeline arranged in the pyrolysis furnace, and the solid carbon-containing substances are discharged through a sealed discharging device.
TABLE 3 solid carbonaceous principal Properties
| Item | Unit of | Numerical value | Remarks for note |
| Moisture content | wt％ | 1.21 | Received base |
| Fixed carbon | wt％ | 83.97 | Received base |
| Volatile component | wt％ | 9.33 | Received base |
| Ash content | wt％ | 5.49 | Received base |
D, mixing: and mixing the solid carbonaceous material with the carbide slag raw material to obtain a mixed product.
E, oil-gas separation and purification: the high-temperature oil gas collected in the pyrolysis unit enters a separation and purification unit, is separated into non-condensable gas and condensable liquid through direct cooling, the non-condensable gas is subjected to alkali washing to remove acidic harmful gases such as halogen and the like, and the pyrolysis gas is obtained after electric coking. The condensable liquid enters an oil-water separation tank to obtain pyrolysis oil, and the separated pyrolysis water is partially recycled as direct cooling spray. The pyrolysis gas is collected and sent into a carbide production unit, the yield of the pyrolysis gas is 7 percent, and the pyrolysis gas is rich in hydrogen, methane, carbon monoxide and the like and can be directly combusted to supply heat. The pyrolysis oil is collected and sold as fuel oil or chemical products, and the yield of the pyrolysis oil is 18%. The content of the pyrolysis gas is as follows:
TABLE 4 pyrolysis gas composition and heating value
| Hydrogen/%) | Methane/% | Carbon monoxide/%) | Carbon dioxide/%) | CnHm/％ | Calorific value kcal/Nm3 |
| 43.01 | 10.68 | 10.02 | 34.67 | 1.62 | 2638 |
F, calcium carbide production: the temperature of the mixed product heat to the calcium carbide furnace is 450 ℃. The calcium carbide furnace adopts a combination of a plurality of electrodes and a plurality of burners to provide a heat source for calcium carbide raw materials. The combustor is used as a supplementary heat source of the electrode, the fuel is pyrolysis gas from the oil-gas separation and purification unit, supplementary combustion-supporting gas is combusted, the pyrolysis gas is rich in hydrogen, methane and carbon monoxide, combustion products are ash-free, and the quality of calcium carbide products cannot be reduced. The temperature of the calcium carbide furnace is 1900 ℃, the reaction time is 30min, the calcium carbide tail gas enters the gas purification and dust removal unit, and the calcium carbide product is discharged from the discharge hole, wherein the calcium carbide content in the calcium carbide product is 78.88%, and the gas evolution quantity is 286L/kg.
Example 3
This example is the same as the system used in example 1 above, but with different process conditions, as follows:
a, pretreatment: and in the pretreatment unit, the waste electronic products are disassembled and crushed to obtain a pretreatment product.
B, separation: finely crushing the pretreated product, magnetically separating ferromagnetic metal, and performing air separation and electrostatic separation to obtain other metals, glass fiber and non-metallic organic matters, wherein the content of the non-metallic organic matters is 36%, and the particle size of the non-metallic organic matters is controlled to be 20 mm.
C, pyrolysis: and feeding the nonmetal products into a pyrolysis furnace uniformly for pyrolysis reaction, wherein the pyrolysis temperature is 850 ℃, the pyrolysis time is 0.5h, high-temperature oil gas and solid carbon-containing substances are generated after the pyrolysis reaction is completed, the high-temperature oil gas is collected through an oil gas pipeline arranged in the pyrolysis furnace, and the solid carbon-containing substances are discharged through a sealed discharging device.
TABLE 5 solid carbonaceous essential Properties
| Item | Unit of | Numerical value | Remarks for note |
| Moisture content | wt％ | 1.09 | Received base |
| Fixed carbon | wt％ | 83.69 | Received base |
| Volatile component | wt％ | 9.47 | Received base |
| Ash content | wt％ | 5.75 | Received base |
D, mixing: and mixing the solid carbonaceous material with a limestone raw material to obtain a mixed product.
E, oil-gas separation and purification: the high-temperature oil gas collected in the pyrolysis unit enters a separation and purification unit, is separated into non-condensable gas and condensable liquid through direct cooling, the non-condensable gas is subjected to alkali washing to remove acidic harmful gases such as halogen and the like, and the pyrolysis gas is obtained after electric coking. The condensable liquid enters an oil-water separation tank to obtain pyrolysis oil, and the separated pyrolysis water is partially recycled as direct cooling spray. The pyrolysis gas is collected and sent into a carbide production unit, the yield of the pyrolysis gas is 9 percent, and the pyrolysis gas is rich in hydrogen, methane, carbon monoxide and the like and can be directly combusted to supply heat. The pyrolysis oil is collected and sold as fuel oil or chemical products, and the yield of the pyrolysis oil is 17%. The content of the pyrolysis gas is as follows:
TABLE 6 pyrolysis gas composition and heating value
| Hydrogen/%) | Methane/% | Carbon monoxide/%) | Carbon dioxide/%) | CnHm/％ | Calorific value kcal/Nm3 |
| 41.55 | 11.12 | 9.88 | 36.04 | 1.41 | 2641 |
F, calcium carbide production: the temperature of the mixed product heat sent to the calcium carbide furnace is 650 ℃. The calcium carbide furnace adopts a combination of a plurality of electrodes and a plurality of burners to provide a heat source for calcium carbide raw materials. The combustor is used as a supplementary heat source of the electrode, the fuel is pyrolysis gas from the oil-gas separation and purification unit, supplementary combustion-supporting gas is combusted, the pyrolysis gas is rich in hydrogen, methane and carbon monoxide, combustion products are ash-free, and the quality of calcium carbide products cannot be reduced. The temperature of the calcium carbide furnace is 2000 ℃, the reaction time is 5min, the calcium carbide tail gas enters the gas purification and dust removal unit, the calcium carbide product is discharged from the discharge hole, the calcium carbide content in the calcium carbide product is 79.25%, and the gas evolution quantity is 288L/kg.
Example 4
This example is the same as the system used in example 1 above, but with different process conditions, as follows:
a, pretreatment: and in the pretreatment unit, the waste electronic products are disassembled and crushed to obtain a pretreatment product.
B, separation: finely crushing the pretreated product, magnetically separating ferromagnetic metal, and performing air separation and electrostatic separation to obtain other metals, glass fiber and non-metallic organic matter, wherein the content of the non-metallic organic matter is 40%, and the particle size of the non-metallic organic matter is controlled to be 0.5 mm.
C, pyrolysis: and feeding the nonmetal products into a pyrolysis furnace uniformly for pyrolysis reaction, wherein the pyrolysis temperature is 650 ℃, the pyrolysis time is 1h, high-temperature oil gas and solid carbon-containing substances are generated after the pyrolysis reaction is completed, the high-temperature oil gas is collected through an oil gas pipeline arranged in the pyrolysis furnace, and the solid carbon-containing substances are discharged through a sealed discharging device.
TABLE 7 main properties of solid carbonaceous materials
| Item | Unit of | Numerical value | Remarks for note |
| Moisture content | wt％ | 1.21 | Received base |
| Fixed carbon | wt％ | 82.65 | Received base |
| Volatile component | wt％ | 10.51 | Received base |
| Ash content | wt％ | 5.63 | Received base |
D, mixing: and mixing the solid carbonaceous material with a hydrated lime raw material to obtain a mixed product.
E, oil-gas separation and purification: the high-temperature oil gas collected in the pyrolysis unit enters a separation and purification unit, is separated into non-condensable gas and condensable liquid through direct cooling, the non-condensable gas is subjected to alkali washing to remove acidic harmful gases such as halogen and the like, and the pyrolysis gas is obtained after electric coking. The condensable liquid enters an oil-water separation tank to obtain pyrolysis oil, and the separated pyrolysis water is partially recycled as direct cooling spray. The pyrolysis gas is collected and sent into a carbide production unit, the yield of the pyrolysis gas is 10 percent, and the pyrolysis gas is rich in hydrogen, methane, carbon monoxide and the like and can be directly combusted to supply heat. The pyrolysis oil is collected and sold as fuel oil or chemical products, and the yield of the pyrolysis oil is 15%. The content of the pyrolysis gas is as follows:
TABLE 8 pyrolysis gas composition and heating value
| Hydrogen/%) | Methane/% | Carbon monoxide/%) | Carbon dioxide/%) | CnHm/％ | Calorific value kcal/Nm3 |
| 42.41 | 12.34 | 10.2 | 33.87 | 1.18 | 2611 |
F, calcium carbide production: the temperature of the mixed product heat sent to the calcium carbide furnace is 750 ℃. The calcium carbide furnace adopts a combination of a plurality of electrodes and a plurality of burners to provide a heat source for calcium carbide raw materials. The combustor is used as a supplementary heat source of the electrode, the fuel is pyrolysis gas from the oil-gas separation and purification unit, supplementary combustion-supporting gas is combusted, the pyrolysis gas is rich in hydrogen, methane and carbon monoxide, combustion products are ash-free, and the quality of calcium carbide products cannot be reduced. The temperature of the calcium carbide furnace is 2200 ℃, the reaction time is 20min, the calcium carbide tail gas enters the gas purification and dust removal unit, and the calcium carbide product is discharged from a discharge hole, wherein the content of calcium carbide in the calcium carbide product is 80.1 percent, and the gas evolution quantity is 287L/kg.
The embodiment shows that the invention realizes the clean and efficient resource treatment of the waste electronic products and the high-value utilization of the pyrolysis products of the waste electronic products; the yield of pyrolysis oil gas products is improved; the raw materials with low price can be used, so that the cost of the raw materials for calcium carbide production is reduced; the byproduct pyrolysis gas is burnt to be used as a supplementary heat source for calcium carbide generation, so that the power consumption is reduced; the pyrolysis solid product is thermally sent into a calcium carbide furnace, so that the heating energy consumption is reduced; the combustion pyrolysis gas has no ash content, and has no influence on the quality of the calcium carbide product; the waste electronic product pyrolysis oil has good oil product and high economy, and the process economic benefit is improved by selling the pyrolysis oil.
Although embodiments of the present invention have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that variations, modifications, substitutions and alterations can be made to the above embodiments by those of ordinary skill in the art within the scope of the present invention.
The disclosure of the present application is directed to exemplary embodiments, and various changes and modifications may be made in the various embodiments of the present application without departing from the scope of the invention as defined in the appended claims. Accordingly, the described embodiments are intended to embrace all such alterations, modifications and variations that fall within the scope of the appended claims. Furthermore, unless the context indicates otherwise, words that appear in the singular include the plural and vice versa. Additionally, all or a portion of any embodiment may be utilized with all or a portion of any other embodiment, unless stated otherwise.
Claims (10)
1. A system for treating waste electronic products comprises a pretreatment unit, a separation unit, a pyrolysis unit, a mixing unit, an oil-gas separation and purification unit and a calcium carbide production unit; wherein,
the pretreatment unit comprises a disassembly unit and a crushing unit, the disassembly unit comprises a waste electronic product inlet and a disassembly product outlet, the crushing unit comprises a disassembly product inlet and a pretreatment product outlet, and the disassembly product inlet is connected with the disassembly product outlet;
the separation unit comprises a pretreatment product inlet and a nonmetal product outlet, and the pretreatment product inlet is connected with the pretreatment product outlet;
the pyrolysis unit comprises a non-metal product inlet, a solid carbon-containing substance outlet and a high-temperature oil gas outlet, and the non-metal product inlet is connected with the non-metal product outlet;
the mixing unit comprises a solid carbonaceous inlet, a calcium-based raw material inlet and a mixed product outlet, and the solid carbonaceous inlet is connected with the solid carbonaceous outlet;
the oil-gas separation and purification unit comprises a high-temperature oil-gas inlet and a pyrolysis gas outlet, and the high-temperature oil-gas inlet is connected with the high-temperature oil-gas outlet;
the calcium carbide production unit comprises a pyrolysis gas inlet, a mixed product inlet and a calcium carbide product outlet, wherein the pyrolysis gas inlet is connected with the pyrolysis gas outlet, and the mixed product inlet is connected with the mixed product outlet.
2. The system of claim 1, wherein the separation unit is one of an air separation unit, a magnetic separation unit, or an electrostatic separation unit, or a combination thereof; and a sealed discharging device is arranged at the solid carbon-containing substance outlet.
3. The system of claim 1, wherein the calcium carbide production unit comprises a calcium carbide tail gas outlet; the system further comprises a gas purification and dust removal unit, wherein the gas purification and dust removal unit comprises a calcium carbide tail gas inlet, and the calcium carbide tail gas inlet is connected with the calcium carbide tail gas outlet.
4. The system of claim 1, wherein the calcium carbide production unit further comprises an oxidant gas inlet through which oxidant gas is introduced into the auxiliary pyrolysis gas for combustion.
5. The system of claim 1, wherein the oil-gas separation purification unit further comprises a pyrolysis oil outlet.
6. A method for processing waste electronic products using the system of any one of claims 1 to 5, comprising the steps of:
a, pretreatment: disassembling and crushing the waste electronic products in the pretreatment unit to obtain a pretreatment product;
b, separation: finely crushing, sorting and separating the pretreated product to obtain a nonmetal product;
c, pyrolysis: feeding the nonmetal products into the pyrolysis unit for pyrolysis reaction to generate high-temperature oil gas and solid carbon-containing substances, wherein the high-temperature oil gas is collected through an oil gas pipeline arranged in the pyrolysis furnace, and the solid carbon-containing substances are discharged through an outlet;
d, mixing: mixing the solid carbonaceous material with a calcium-based raw material to obtain a mixed product;
e, oil-gas separation and purification: separating the high-temperature oil gas into non-condensable gas and condensable liquid through direct cooling or indirect cooling in the oil-gas separation and purification unit, wherein the non-condensable gas is treated to obtain pyrolysis gas;
f, calcium carbide production: and (3) feeding the mixed product into a calcium carbide furnace for reaction to obtain the calcium carbide after the reaction is finished.
7. The method according to claim 6, wherein in the step F, the pyrolysis gas in the step E is used as fuel, and a plurality of electrodes and a plurality of burners are combined to be used as a heat source of the calcium carbide furnace to perform reaction in the calcium carbide furnace; and adding combustion-supporting gas into the pyrolysis gas to assist combustion.
8. The method according to claim 6, wherein the particle size of the non-metal product in step B is controlled to 0.5-100 mm; and D, the calcium-based raw material in the step D is one or more selected from lime, limestone, hydrated lime or carbide slag.
9. The method as claimed in claim 6, wherein the temperature of the pyrolysis reaction in step C is 450-850 ℃, and the pyrolysis time is 0.5-3 h; and F, controlling the reaction temperature of the calcium carbide furnace to be 1700-2200 ℃ and the reaction time to be 5-50 min.
10. The method according to claim 6, characterized in that the pyrolysis gas in the step E is obtained by alkali washing the non-condensable gas to remove acidic harmful gases such as halogen and the like and electrically capturing coke; and F, the temperature of the mixed product heat delivered to the calcium carbide furnace is 350-750 ℃.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103708461A (en) * | 2013-12-25 | 2014-04-09 | 北京神雾环境能源科技集团股份有限公司 | Method for preparing calcium carbide |
| CN103708455A (en) * | 2013-12-25 | 2014-04-09 | 北京神雾环境能源科技集团股份有限公司 | Method for preparing calcium carbide |
| CN105858660A (en) * | 2016-03-30 | 2016-08-17 | 神雾环保技术股份有限公司 | System and method for preparing calcium carbide |
| CN206051565U (en) * | 2016-08-29 | 2017-03-29 | 北京神雾环境能源科技集团股份有限公司 | A kind of system for processing Waste ammunition |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103708461A (en) * | 2013-12-25 | 2014-04-09 | 北京神雾环境能源科技集团股份有限公司 | Method for preparing calcium carbide |
| CN103708455A (en) * | 2013-12-25 | 2014-04-09 | 北京神雾环境能源科技集团股份有限公司 | Method for preparing calcium carbide |
| CN105858660A (en) * | 2016-03-30 | 2016-08-17 | 神雾环保技术股份有限公司 | System and method for preparing calcium carbide |
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