Patent Application
20220356067
The invention relates to a recovery technology for collaborative treatment and high-value utilization of waste circuit boards smelting ash and pyrolysis residues, especially relating to a new method for using the coke in waste circuit boards pyrolysis residues to reduce crude bromine salt obtained from waste circuit boards smelting ash.
Waste circuit boards is the most valuable part in waste electronic appliances, but it is difficult to be treated, and its treatment is the core of high value utilization of electronic appliances. At present, the main treatment methods are physical separation, pyrometallurgy treatment and hydrometallurgy treatment, as well as gradually developing biological treatment technologies. The treatment characteristics of these recovery technologies are shown in table 1. Among them, metal and nonmetal enrichment can be obtained by physical separation, hydrometallurgy and biometallurgy are mostly focused on the recovery of metals in circuit boards, while metal alloy can be quickly obtained and nonmetal resources can be used by smelting and pyrolysis in pyrometallurgy technology, which has a good volume reduction effect. Pyrometallurgy and pyrolysis technology are considered to be the most effective technology for high value utilization of waste circuit boards, which can effectively recover metal, resin and fiberglass.
With the progress of technologies, advanced and dissolvable smelting technology has been applied to the treatment of waste circuit boards and has been regarded as the mainstream technology for the treatment of waste circuit boards in Europe, America, Japan and other developed countries. Typically, Umicore uses ISA top blowing smelting technology to treat waste circuit boards and copper concentrates, and Boliden uses Kaldor furnace and Ausmelt top blowing smelting technology to treat mobile phone and computer circuit boards et al are successful cases of whole-body utilization. The successful implementation of this technology is conducive to fundamentally changing the traditional incineration mode and reducing the environmental problems caused by incineration. Due to the large amount of brominated flame retardant contained in circuit boards, there are a lot of bromides in the waste circuit board smelting ash. Application No. 201711490199.0 proposed a method of enriching the bromides in the smelting ash by sulphating roasting-alkali washing spray method to obtain crude bromine salt. This method has good effect on removing and enriching bromides in the waste circuit boards smelting ash, but the obtained crude bromine salt has not been further purified and its high value utilization needs to be further studied.
The waste circuit boards are heated to a certain temperature (>650 K) in the presence or absence of oxygen by pyrolysis technology of waste circuit boards to decompose the organic matters, such as epoxy resin, into gas and liquid pyrolysis oil, while the metal, coke and fiberglass together form solid waste (pyrolysis residues). For the pyrolysis residues from pyrolysis, the current research mainly focuses on the comprehensive recovery of gas and oil and the recycling of metal in the pyrolysis products, while the research on the recovery of nonmetal in the pyrolysis residues is less. The method of preparing polypropylene composites using fiberglass in waste circuit boards pyrolysis residues application proposed in No. CN201010529818.4 realizes the high value utilization of fiberglass in pyrolysis residues, but the coke was directly incinerated without realizing its secondary utilization.
The crude bromide salt is a by-product obtained from waste circuit boards smelting ash through sulphating roasting-alkali washing-neutralization precipitation and evaporation crystallization, which contains NaBr, NaBrO and NaBrO3. The traditional treatment method of crude bromide salt is to add pure reducing agent to get sodium bromide solution by heating reduction, and then bromine is obtained by electrodialysis membrane process or chlorination process, which has the disadvantages of high cost and complex operating environment. The recovery of waste circuit boards pyrolysis residues often focuses on the recovery of metal and fiberglass, while the coke in which is often directly calcined, which wastes its resource value. In conclusion, in view of the characteristics of smelting and pyrolysis technology of waste circuit boards in China, as well as the treatment situation of secondary waste produced in the recovery process, it is urgent to develop full component recovery technology of waste circuit boards smelting ash and pyrolysis residues. The invention proposes a new method for reducing the crude bromine salt using the coke in waste circuit boards pyrolysis residues, and pure sodium bromide (NaBr) is obtained through carbonization conversion, water dissolution, filtration, and concentrated crystallization under vacuum heating. It realizes the resource coupling and integrated utilization of the two wastes, having the advantages of simple operation, high resource utilization rate, environment-friendly, etc.
The purpose of the invention is mainly to solve the problem of high value utilization of waste circuit boards smelting ash and waste circuit boards pyrolysis residues. A new method for the production and purification of sodium bromide from bromine salt by using the coke as a reducing agent was proposed. It realizes the resource coupling and integrated utilization of the two wastes, and has the characteristics of simple operation, high resource utilization rate, environment-friendly, etc.
The method for producing and purifying sodium bromide using the coke from waste circuit boards pyrolysis residues as reducing agent is as follows:
(1) Carbonization conversion: the crude bromine salt is mixed with the coke separated from the waste circuit boards pyrolysis residues to obtain a mixture. The crude bromide salt is a by-product obtained from waste circuit boards smelting ash through sulphating roasting-alkali washing-neutralization precipitation and evaporation crystallization, which contains NaBr, NaBrO and NaBrO3. Then the mixture is heated to obtain carbon monoxide and the primary product of sodium bromide (containing NaBr and C from coke). The carbon monoxide is collected and used as raw material of water gas. During mixing, the mass of the coke is 0.1˜1.0 kg per kilogram of crude bromine salt, the temperature is 250˜450° C., and the time is 1.0˜ 2.0 h;
(2) Water dissolution and filtration: the primary product of sodium bromide obtained in step (1) is added to distilled water for dissolution and filtration to obtain insoluble impurities (containing C) and NaBr-containing leachate. During the water dissolution and filtration, the liquid-solid volume mass ratio (distilled water to primary product of sodium bromide) is 8:1˜3:1 (L/kg), the temperature is 50˜80° C., and the time is 20˜60 min;
(3) Concentrated crystallization under vacuum heating: the NaBr-containing leachate obtained in step (2) is concentrated and crystallized by vacuum heating to obtain sodium bromide (NaBr). During the concentrated crystallization, the time is 30˜60 min and the temperature is 60˜150° C. This step is carried out in a vacuum evaporation device, which includes an evaporator, a solvent collecting tank and a vacuum system. The evaporator is communicated with the solvent collecting tank and the vacuum system respectively, a condenser and a material head tank are arranged on the evaporator and respectively communicated with the same, and the vacuum system is communicated with the condenser and the solvent collecting tank respectively, so that pressure in the condenser can be kept balanced with that of the solvent colleting tank and liquefied solvent in the condenser flows into the solvent collecting tank automatically.
Compared with the prior art, the present invention uses one kind of waste generated in the recycling process of waste circuit boards to treat another kind of waste. This is a new recycling method with the coke in the waste circuit boards pyrolysis residues as reducing agent to reduce the crude bromine salt obtained in the waste circuit boards smelting ash, so as to reduce the high valence bromate in the crude bromine salt to produce pure sodium bromide without additional reducing agent in the implementation process and no other impurities is introduced. It realizes the resource coupling and integrated utilization of the two wastes, and having the characteristics of simple operation, high resource utilization rate, environment-friendly, etc.
The following exemplary embodiments are intended to further illustrate the invention rather than limit it.
The recovery steps are as follows:
(1) Carbonization conversion: the crude bromine salt is mixed with the coke separated from the waste circuit boards pyrolysis residues to obtain a mixture. The crude bromide salt is a by-product obtained from waste circuit boards smelting ash through sulphating roasting-alkali washing-neutralization precipitation and evaporation crystallization, which contains NaBr, NaBrO and NaBrO3. Then the mixture is heated to obtain carbon monoxide and the primary product of sodium bromide (containing NaBr and C from coke). The carbon monoxide is collected and used as raw material of water gas. During mixing, the mass of the coke is 0.1 kg per kilogram of crude bromine salt, the temperature is 250° C., and the time is 1.0 h;
(2) Water dissolution and filtration: the primary product of sodium bromide obtained in step (1) is added to distilled water for dissolution and filtration to obtain insoluble impurities (containing C) and NaBr-containing leachate. During the water dissolution and filtration, the liquid-solid volume mass ratio (distilled water to primary product of sodium bromide) is 8:1 (L/kg), the temperature is 50° C., and the time is 20 min;
(3) Concentrated crystallization under vacuum heating: the NaBr-containing leachate obtained in step (2) is concentrated and crystallized by vacuum heating to obtain sodium bromide (NaBr). During the concentrated crystallization, the time is 60 min and the temperature is 60° C. This step is carried out in a vacuum evaporation device, which includes an evaporator, a solvent collecting tank and a vacuum system. The evaporator is communicated with the solvent collecting tank and the vacuum system respectively, a condenser and a material head tank are arranged on the evaporator and respectively communicated with the same, and the vacuum system is communicated with the condenser and the solvent collecting tank respectively, so that pressure in the condenser can be kept balanced with that of the solvent colleting tank and liquefied solvent in the condenser flows into the solvent collecting tank automatically.
The purity of the obtained sodium bromide is 98.6%, which meets the standard of the first grade sodium bromide (NaBr≥98.5%) in the standard HG/T 3809-2006 of State Ministry of Chemical Industry.
The recovery steps are as follows:
(1) Carbonization conversion: the crude bromine salt is mixed with the coke separated from the waste circuit boards pyrolysis residues to obtain a mixture. The crude bromide salt is a by-product obtained from waste circuit boards smelting ash through sulphating roasting-alkali washing-neutralization precipitation and evaporation crystallization, which contains NaBr, NaBrO and NaBrO3. Then the mixture is heated to obtain carbon monoxide and the primary product of sodium bromide (containing NaBr and C from coke). The carbon monoxide is collected and used as raw material of water gas. During mixing, the mass of the coke is 1.0 kg per kilogram of crude bromine salt, the temperature is 450° C., and the time is 2.0 h;
(2) Water dissolution and filtration: the primary product of sodium bromide obtained in step (1) is added to distilled water for dissolution and filtration to obtain insoluble impurities (containing C) and NaBr-containing leachate. During the water dissolution and filtration, the liquid-solid volume mass ratio (distilled water to primary product of sodium bromide) is 3:1 (L/kg), the temperature is 80° C., and the time is 60 min;
(3) Concentrated crystallization under vacuum heating: the NaBr-containing leachate obtained in step (2) is concentrated and crystallized by vacuum heating to obtain sodium bromide (NaBr). During the concentrated crystallization, the time is 30 min and the temperature is 150° C. This step is carried out in a vacuum evaporation device, which includes an evaporator, a solvent collecting tank and a vacuum system. The evaporator is communicated with the solvent collecting tank and the vacuum system respectively, a condenser and a material head tank are arranged on the evaporator and respectively communicated with the same, and the vacuum system is communicated with the condenser and the solvent collecting tank respectively, so that pressure in the condenser can be kept balanced with that of the solvent colleting tank and liquefied solvent in the condenser flows into the solvent collecting tank automatically.
The purity of the obtained sodium bromide is 99.4%, which meets the standard of the superior product sodium bromide (NaBr≥99%) in the standard HG/T 3809-2006 of State Ministry of Chemical Industry.
The recovery steps are as follows:
(1) Carbonization conversion: the crude bromine salt is mixed with the coke separated from the waste circuit boards pyrolysis residues to obtain a mixture. The crude bromide salt is a by-product obtained from waste circuit boards smelting ash through sulphating roasting-alkali washing-neutralization precipitation and evaporation crystallization, which contains NaBr, NaBrO and NaBrO3. Then the mixture is heated to obtain carbon monoxide and the primary product of sodium bromide (containing NaBr and C from coke). The carbon monoxide is collected and used as raw material of water gas. During mixing, the mass of the coke is 0.4 kg per kilogram of crude bromine salt, the temperature is 300° C., and the time is 1.2 h;
(2) Water dissolution and filtration: the primary product of sodium bromide obtained in step (1) is added to distilled water for dissolution and filtration to obtain insoluble impurities (containing C) and NaBr-containing leachate. During the water dissolution and filtration, the liquid-solid volume mass ratio (distilled water to primary product of sodium bromide) is 7:1 (L/kg), the temperature is 60° C., and the time is 25 min;
(3) Concentrated crystallization under vacuum heating: the NaBr-containing leachate obtained in step (2) is concentrated and crystallized by vacuum heating to obtain sodium bromide (NaBr). During the concentrated crystallization, the time is 50 min and the temperature is 100° C. This step is carried out in a vacuum evaporation device, which includes an evaporator, a solvent collecting tank and a vacuum system. The evaporator is communicated with the solvent collecting tank and the vacuum system respectively, a condenser and a material head tank are arranged on the evaporator and respectively communicated with the same, and the vacuum system is communicated with the condenser and the solvent collecting tank respectively, so that pressure in the condenser can be kept balanced with that of the solvent colleting tank and liquefied solvent in the condenser flows into the solvent collecting tank automatically.
The purity of the obtained sodium bromide is 98.8%, which meets the standard of the first grade sodium bromide (NaBr≥98.5%) in the standard HG/T 3809-2006 of State Ministry of Chemical Industry.
The recovery steps are as follows:
(1) Carbonization conversion: the crude bromine salt is mixed with the coke separated from the waste circuit boards pyrolysis residues to obtain a mixture. The crude bromide salt is a by-product obtained from waste circuit boards smelting ash through sulphating roasting-alkali washing-neutralization precipitation and evaporation crystallization, which contains NaBr, NaBrO and NaBrO3. Then the mixture is heated to obtain carbon monoxide and the primary product of sodium bromide (containing NaBr and C from coke). The carbon monoxide is collected and used as raw material of water gas. During mixing, the mass of the coke is 0.8 kg per kilogram of crude bromine salt, the temperature is 400° C., and the time is 1.8 h;
(2) Water dissolution and filtration: the primary product of sodium bromide obtained in step (1) is added to distilled water for dissolution and filtration to obtain insoluble impurities (containing C) and NaBr-containing leachate. During the water dissolution and filtration, the liquid-solid volume mass ratio (distilled water to primary product of sodium bromide) is 6:1 (L/kg), the temperature is 75° C., and the time is 50 min;
(3) Concentrated crystallization under vacuum heating: the NaBr-containing leachate obtained in step (2) is concentrated and crystallized by vacuum heating to obtain sodium bromide (NaBr). During the concentrated crystallization, the time is 40 min and the temperature is 130° C. This step is carried out in a vacuum evaporation device, which includes an evaporator, a solvent collecting tank and a vacuum system. The evaporator is communicated with the solvent collecting tank and the vacuum system respectively, a condenser and a material head tank are arranged on the evaporator and respectively communicated with the same, and the vacuum system is communicated with the condenser and the solvent collecting tank respectively, so that pressure in the condenser can be kept balanced with that of the solvent colleting tank and liquefied solvent in the condenser flows into the solvent collecting tank automatically.
The purity of the obtained sodium bromide is 99.2%, which meets the standard of the superior product sodium bromide (NaBr≥99%) in the standard HG/T 3809-2006 of State Ministry of Chemical Industry.
The recovery steps are as follows:
(1) Carbonization conversion: the crude bromine salt is mixed with the coke separated from the waste circuit boards pyrolysis residues to obtain a mixture. The crude bromide salt is a by-product obtained from waste circuit boards smelting ash through sulphating roasting-alkali washing-neutralization precipitation and evaporation crystallization, which contains NaBr, NaBrO and NaBrO3. Then the mixture is heated to obtain carbon monoxide and the primary product of sodium bromide (containing NaBr and C from coke). The carbon monoxide is collected and used as raw material of water gas. During mixing, the mass of the coke is 0.5 kg per kilogram of crude bromine salt, the temperature is 350° C., and the time is 1.5 h;
(2) Water dissolution and filtration: the primary product of sodium bromide obtained in step (1) is added to distilled water for dissolution and filtration to obtain insoluble impurities (containing C) and NaBr-containing leachate. During the water dissolution and filtration, the liquid-solid volume mass ratio (distilled water to primary product of sodium bromide) is 4:1 (L/kg), the temperature is 70° C., and the time is 40 min;
(3) Concentrated crystallization under vacuum heating: the NaBr-containing leachate obtained in step (2) is concentrated and crystallized by vacuum heating to obtain sodium bromide (NaBr). During the concentrated crystallization, the time is 45 min and the temperature is 120° C. This step is carried out in a vacuum evaporation device, which includes an evaporator, a solvent collecting tank and a vacuum system. The evaporator is communicated with the solvent collecting tank and the vacuum system respectively, a condenser and a material head tank are arranged on the evaporator and respectively communicated with the same, and the vacuum system is communicated with the condenser and the solvent collecting tank respectively, so that pressure in the condenser can be kept balanced with that of the solvent colleting tank and liquefied solvent in the condenser flows into the solvent collecting tank automatically.
The purity of the obtained sodium bromide is 98.9%, which meets the standard of the first grade sodium bromide (NaBr≥98.5%) in the standard HG/T 3809-2006 of State Ministry of Chemical Industry.
The recovery steps are as follows:
(1) Carbonization conversion: the crude bromine salt is mixed with the coke separated from the waste circuit boards pyrolysis residues to obtain a mixture. The crude bromide salt is a by-product obtained from waste circuit boards smelting ash through sulphating roasting-alkali washing-neutralization precipitation and evaporation crystallization, which contains NaBr, NaBrO and NaBrO3. Then the mixture is heated to obtain carbon monoxide and the primary product of sodium bromide (containing NaBr and C from coke). The carbon monoxide is collected and used as raw material of water gas. During mixing, the mass of the coke is 0.6 kg per kilogram of crude bromine salt, the temperature is 350° C., and the time is 16 h;
(2) Water dissolution and filtration: the primary product of sodium bromide obtained in step (1) is added to distilled water for dissolution and filtration to obtain insoluble impurities (containing C) and NaBr-containing leachate. During the water dissolution and filtration, the liquid-solid volume mass ratio (distilled water to primary product of sodium bromide) is 5:1 (L/kg), the temperature is 70° C., and the time is 45 min;
(3) Concentrated crystallization under vacuum heating: the NaBr-containing leachate obtained in step (2) is concentrated and crystallized by vacuum heating to obtain sodium bromide (NaBr). During the concentrated crystallization, the time is 30 min and the temperature is 80° C. This step is carried out in a vacuum evaporation device, which includes an evaporator, a solvent collecting tank and a vacuum system. The evaporator is communicated with the solvent collecting tank and the vacuum system respectively, a condenser and a material head tank are arranged on the evaporator and respectively communicated with the same, and the vacuum system is communicated with the condenser and the solvent collecting tank respectively, so that pressure in the condenser can be kept balanced with that of the solvent colleting tank and liquefied solvent in the condenser flows into the solvent collecting tank automatically.
The purity of the obtained sodium bromide is 99.1%, which meets the standard of the superior product sodium bromide (NaBr≥99.0%) in the standard HG/T 3809-2006 of State Ministry of Chemical Industry.
The above embodiments are only used to illustrate the preferred embodiments of the invention, but the invention is not limited to the above embodiments. Within the scope of knowledge possessed by those skilled in the art and on the premise of not departing from the science and design spirit in the invention, the modifications, equivalent substitutions and improvements et al. made on the spirit and principles of the invention shall be regarded as in the scope of protection of the application.
| Number | Date | Country | Kind |
|---|---|---|---|
| 201911359343.6 | Dec 2019 | CN | national |
This application is continuation-in-part of application Ser. No. 17/351,083, filed on Jun. 17, 2021, which is a continuation of International Application No. PCT/CN2020/127972, filed on Nov. 11, 2020, which in turn claims priority to Chinese Patent Application No. 201911359343.6, filed on Dec. 25, 2019, the contents of the above applications are hereby incorporated by reference in their entireties.
| Number | Date | Country | |
|---|---|---|---|
| Parent | PCT/CN2020/127972 | Nov 2020 | US |
| Child | 17351083 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 17351083 | Jun 2021 | US |
| Child | 17867618 | US |
