CN103771534A - Method and equipment for recycling fluoride in iron-containing compound production - Google Patents

Method and equipment for recycling fluoride in iron-containing compound production Download PDF

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CN103771534A
CN103771534A CN201410066435.6A CN201410066435A CN103771534A CN 103771534 A CN103771534 A CN 103771534A CN 201410066435 A CN201410066435 A CN 201410066435A CN 103771534 A CN103771534 A CN 103771534A
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fluorochemical
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CN103771534B (en
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杨先金
章林
刘瑞
史春华
龚龙江
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GUIZHOU WANFANG ALUMINUM SCIENCE AND TECHNOLOGY DEVELOPMENT Co Ltd
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Abstract

The invention relates to the field of fluoride recycling, and particularly relates to a method and equipment for recycling fluoride in iron-containing compound production. The method comprises the following steps of mixing the raw material of Fe-containing oxide with solid-state fluoride to form a mixture; calcining the mixture, wherein the Fe<3+> in the Fe-containing oxide and the F<-> in the fluoride generate a first product FeF3 gas, and the O<2-> in the Fe-containing oxide and the cation in the fluoride generate a second product; introducing water vapor into the first product and enabling reaction to form a gas-solid mixture containing solid-state Fe2O3 and gas-state HF; separating the gas-solid mixture to obtain the first gas phase containing unreacted water vapor and gas-state HF and solid-state Fe2O3; enabling the first gas phase to react with the second product to obtain solid-state fluoride again. According to the method and equipment provided by the invention, the cost is lowered through the recycling of fluoride, and the environmental pollution caused by fluoride is also avoided.

Description

The method and apparatus of fluorochemical recycle in a kind of iron containing compounds production
Technical field
The present invention relates to fluorochemical recycling field, the method and apparatus of fluorochemical recycle in producing in particular to a kind of iron containing compounds.
Background technology
Fluorine in fluorine chemical product mainly comes from fluorite, and fluorite is Nonrenewable resources, is a kind of strategic resource simultaneously.Efficiently utilize existing fluorine resource and save existing fluorite resource and become an important directions of fluorine chemical industry Sustainable development.Fluorochemical in use can produce multiple waste now, waste residue fluorine iron perchloride and the fluorine-containing breeze of electrolytic iron production process by-product etc. that such as Neutral ammonium fluoride, ammonium bifluoride produce as etching reagent; Electrolytic process produces the dust such as the gas such as a large amount of hydrofluoric acid and three ferric fluorides and ferric fluoride, Calcium Fluoride (Fluorspan) for another example; Copper metallurgy process adopts fluorite (CaF 2) make fusing assistant, so contain the objectionable impuritiess such as a large amount of Calcium Fluoride (Fluorspan), hydrogen fluoride in flue dust; Magnesium, iron also produce hydrogen fluoride and three ferric fluorides etc. in casting; These fluorochemicals long-term storage or directly emit not only and pollute the environment, and reduced the utilization ratio of these fluorochemicalss.
Summary of the invention
The object of the present invention is to provide the method and apparatus of fluorochemical recycle in a kind of iron containing compounds production, to solve the above problems.
The embodiment of the present invention provides the method for fluorochemical recycle in a kind of iron containing compounds production, comprises the following steps:
(A) raw material containing Fe oxide compound is mixed with solid-state fluorochemical, form mixture;
(B) mixture is calcined, wherein containing the Fe in Fe oxide compound 3+with the F in fluorochemical -generate the first product FeF 3gas, containing the O in Fe oxide compound 2-generate the second product with the positively charged ion in fluorochemical;
(C) the first product passed into water vapour and reacts, making it to form and contain solid-state Fe 2o 3gas-solid mixture with gaseous state HF;
(D) after being separated, gas-solid mixture obtains the first gas phase and the solid-state Fe that contain unreacted water vapour and gaseous state HF 2o 3;
(E) the first gas phase is reacted with the second product, again obtain solid-state fluorochemical.
Preferably, the reaction conditions of step (E) is to react 1-5h at 100-600 ℃ of temperature.
Preferably, step (E) is specially:
First the first gas phase cooling is obtained to hydrofluoric acid, more mixed to hydrofluoric acid and the second product being incorporated at 100-600 ℃ of temperature reacted to 1-5h, obtain fluorochemical;
Or
First the first gas phase is mixed with the second product, then the first gas phase cooling is obtained to hydrofluoric acid, finally hydrofluoric acid is reacted to 1-5h with the second product at 100-600 ℃ of temperature, obtain fluorochemical.
The condition of preferably, calcining in step (B) for to calcine 1-5h at 600-1300 ℃.
Preferably, the temperature 970-1300 ℃ of reaction in step (C).
Preferably, step (D) is specially:
Gas-solid mixture is cooled to 100-280 ℃ and obtains the first gas phase and the solid-state Fe that contain unreacted water vapour and gaseous state HF after separating 2o 3; Adopt tetrafluoroethylene pipeline transport the first gas phase and mix with the second product.
The embodiment of the present invention also provides the equipment of fluorochemical recycle in a kind of iron containing compounds production, comprising: the first reactor, the second reactor, the 3rd reactor and separator;
The first reactor is for calcining mixture, wherein containing the Fe in Fe oxide compound 3+with the F in fluorochemical -generate the first product FeF 3gas, containing the O in Fe oxide compound 2-generate the second product with the positively charged ion in fluorochemical;
The second reactor, for the first product is passed into water vapour and reacts, makes it to form and contains solid-state Fe 2o 3gas-solid mixture with gaseous state HF;
First gas phase and the solid-state Fe of separator for obtaining after gas-solid mixture is separated containing unreacted water vapour and gaseous state HF 2o 3;
The 3rd reactor is for reacting the first gas phase again to obtain fluorochemical with the second product.
Preferably, separator is sack cleaner or cyclonic separator.
Preferably, also comprise interchanger, interchanger is for obtaining hydrofluoric acid by the first gas phase cooling.
Preferably, also comprise recirculated water coil pipe, the casing of the 3rd reactor has recirculated water coil pipe, and recirculated water coil pipe is for obtaining hydrofluoric acid by the first gas phase cooling.
The method and apparatus of fluorochemical recycle in a kind of iron containing compounds production that the embodiment of the present invention provides, first after fluorochemical being mixed with ferrous metal mineral and ferrous metal oxide compound, react, generating under high temperature is three ferric fluorides and first reaction product of gaseous state, three of recycling gaseous state is fluoridized molten iron solution and is generated ferric oxide and hydrogen fluoride gas, finally by hydrogen fluoride gas again with the first reaction, again obtain fluorochemical.The method of this recycle fluorochemical, has not only been reduced cost but also has been avoided the pollution of fluorochemical to environment by the iterative cycles utilization to fluorochemical.
Accompanying drawing explanation
The iron containing compounds that Fig. 1-3 show the embodiment of the present invention produce in the process flow sheet of method of fluorochemical recycle;
The iron containing compounds that Fig. 4 shows the embodiment of the present invention produce in the method flow diagram of fluorochemical recycle;
1 first reactor, 2 second reactors, 3 separators, 4 the 3rd reactors, 5 interchanger.
Embodiment
Also by reference to the accompanying drawings the present invention is described in further detail below by specific embodiment.
The embodiment of the present invention provides the method for fluorochemical recycle in a kind of iron containing compounds production, as shown in Figure 4, comprises the following steps:
Step (A): the raw material containing Fe oxide compound is mixed with solid-state fluorochemical, form mixture, wherein the massfraction of solid-state fluorochemical is 20%-80% in mixture, is preferably not more than 7mm, because react more abundant after the less mixing of particle diameter containing the particle diameter of Fe oxide compound.
Preferably, containing the raw material of Fe oxide compound comprise following one or more: Fe 2o 3coarse particles, iron-bearing mineral, contain Fe 2o 3mixture or contain Fe 2o 3waste material etc., wherein contain Fe 2o 3mixture comprise following one or more: the silicate mine of ilmenite, magnetite, rhombohedral iron ore, limonite, spathic iron ore, sulfurous iron ore or iron etc.
Preferably, solid-state fluorochemical comprise following one or more: NaF, NH 4f, NH 4hF 2, CaF 2, AlF 3.
Preferably, be mixed to form in mixture by the raw material containing Fe oxide compound and solid-state fluorochemical, the massfraction of solid-state fluorochemical is preferably 20%-80%.Can make so more Fe participate in reaction, contribute to improve productive rate.
Concrete array mode containing the raw material of Fe oxide compound and solid-state fluorochemical sees the following form 1:
Table 1 is containing kind and the addition of the raw material of Fe oxide compound and solid-state fluorochemical
Figure BDA0000470063620000041
Step (B), calcines mixture, wherein containing the Fe in Fe oxide compound 3+with the F in fluorochemical -generate the first product FeF 3gas, containing the O in Fe oxide compound 2-generate the second product with the positively charged ion in fluorochemical;
Due to when temperature is lower than 600 ℃, possibly cannot generate the FeF of gaseous state 3if temperature, higher than 1300 ℃, may generate more by product, therefore preferably the condition of the middle calcining of step (B) for calcining 1-5h at 600-1300 ℃, and the chemical reaction that this step occurs is: MxOynFe 2o 3+ AFz → MxOy+A 2oz+FeF 3(1), specifically the concrete numerical value of this step temperature, time parameter sees the following form 2.
Step (C), passes into the first product water vapour and reacts, and makes it to form to contain solid-state Fe 2o 3with the gas-solid mixture of gaseous state HF, in order better to control Fe 2o 3the particle diameter of product, the therefore temperature 970-1300 ℃ of reaction in step (C) preferably, specifically the concrete numerical value of this step temperature parameter sees the following form 2;
The chemical reaction that this step occurs is: 2FeF 3+ 3H 2o → Fe 2o 3+ 6HF(2)
Step (D), obtains the first gas phase that contains gaseous state HF and contains solid-state Fe after gas-solid mixture is separated 2o 3the first solid phase, by separate after the first gas phase send in the 3rd reactor with polyfluortetraethylene pipe.
Preferably, step (D) is specially: gas-solid mixture is cooled to 100-280 ℃ and obtains the first gas phase and the solid-state Fe that contain unreacted water vapour and gaseous state HF after separating 2o 3; Adopt tetrafluoroethylene pipeline transport the first gas phase and mix with the second product, because HF is that corrosive gases transports with corrosion resistant material tetrafluoroethylene pipeline while therefore transporting, but this material heatproof value is the highest 280 ℃ of left and right, therefore need after gas-solid mixture cooling, to transport with tetrafluoroethylene pipeline.
Step (E), reacts the first gas phase with the second product, again obtain solid-state fluorochemical, by the second product A generating in hydrogen fluoride gas and calcining 2o zreaction, regenerates fluorochemical AF z, reaction conditions is preferably under 100-600 ℃ of condition and reacts 1-5 hour.
React and regenerate before fluorochemical with the second product in the first gas phase, need first the first gas phase to be cooled to liquid phase hydrofluoric acid, therefore preferably step (E) is specially: first the first gas phase cooling is obtained to hydrofluoric acid, again mixed to hydrofluoric acid and the second product being incorporated at 100-600 ℃ of temperature reacted to 1-5h, obtain fluorochemical; Or first the first gas phase is mixed with the second product, then the first gas phase cooling is obtained to hydrofluoric acid, finally hydrofluoric acid is reacted to 1-5h with the second product at 100-600 ℃ of temperature, obtain fluorochemical.
The reaction that this step occurs is: A 2o z+ HF → AF z+ H 2o (3)
By this step, can realize the recycle of fluorochemical, the concrete data of actual temp, time parameter see the following form 2.
Table 2 step 102,103 and 105 temperature, the concrete numerical value of time parameter
Figure BDA0000470063620000071
The embodiment of the present invention provides the equipment of a kind of method of fluorochemical recycle in iron containing compounds production, as shown in Figure 1, comprising: the first reactor 1, the second reactor 2, the 3rd reactor 4 and separator 3;
The first reactor 1 is for calcining mixture, wherein containing the Fe in Fe oxide compound 3+generate the first product FeF with the F-in fluorochemical 3gas, containing the O in Fe oxide compound 2 -generate the second product with the positively charged ion in fluorochemical;
Preferably, the first reactor 1 of the embodiment of the present invention is calcining furnace, and calcining furnace quick heating is applicable to gas-solid reaction, but is not limited to calcining furnace, any equipment that can realize this function all can, all within protection scope of the present invention.
The second reactor 2, for the first product is passed into water vapour and reacts, makes it to form and contains solid-state Fe 2o 3gas-solid mixture with gaseous state HF;
First gas phase and the solid-state Fe of separator 3 for obtaining after gas-solid mixture is separated containing unreacted water vapour and gaseous state HF 2o 3;
The 3rd reactor 4 is for reacting the first gas phase again to obtain fluorochemical with the second product.
In iron containing compounds production of the present invention, the equipment of the method for fluorochemical recycle can be realized the recycle of fluorochemical, has not only been reduced cost but also has been avoided the pollution of fluorochemical to environment by the iterative cycles utilization to fluorochemical.
Preferably, separator 3 is sack cleaner or cyclonic separator, and these two kinds of separators belong to common separating device, fully meeting in separation condition situation of the present invention, have the advantages such as cost is lower, easy to use.
Preferably, as shown in Figure 3, also comprise interchanger 5, interchanger 5 is for obtaining hydrofluoric acid by the first gas phase cooling.
Preferably, as shown in Figure 2, also comprise recirculated water coil pipe, the casing of the 3rd reactor has recirculated water coil pipe, and recirculated water coil pipe is for obtaining hydrofluoric acid by the first gas phase cooling.
Next, be described in detail by 4 specific embodiments:
Embodiment 1:
Will be containing Fe 2o 3waste material and CaF 2mix and obtain mixture, Fe 2o 3with CaF 2particle diameter be below 3mm, CaF in gained mixture 2mass percent be 80%.Mixture, the temperature lower calcination of 1150 ℃ of the first reactors 1 hour, is generated to CaO and FeF 3, FeF 3under high temperature, be gaseous state, from solid reactant, overflow.By the FeF overflowing 3introduce in the second reactor, and be hydrolyzed at the temperature of 1250 ℃, generate Fe 2o 3with HF gas.The HF gas that hydrolysis is produced is transported in the 3rd reactor with tetrafluoroethylene pipeline, reacts 2.5 hours at 600 ℃ with reaction product CaO, again obtains CaF 2thereby, realize CaF 2be cycled to repeat utilization.Reaction equation is as follows:
Fe 2O 3+3CaF 2→3CaO+2FeF 3 （4）
2FeF 3+3H 2O→Fe 2O 3+6HF （5）
CaO+2HF→CaF 2+H 2O （6）
Embodiment 2:
By magnetite (Fe 2o 3mSiO 2) and AlF 3mix and obtain mixture, magnetite and AlF 3particle diameter be below 5mm, AlF in gained mixture 3mass percent be 60%.By mixture temperature lower calcination 3 hours of 1300 ℃ in the first reactor, generate Al 2o 3with gaseous state FeF 3and gaseous state SiF 4, by gaseous state SiF 4low ternperature separation process is out hydrolyzed and makes silicon-dioxide and hydrogen fluoride afterwards.By FeF 3from solid reactant, distillation is overflowed.By the FeF overflowing 3introduce in the second reactor, and hydrolysis generates Fe at the temperature of 1300 ℃ 2o 3with HF gas.The HF gas that hydrolysis is produced is transported in the 3rd reactor with tetrafluoroethylene pipeline, with reaction product Al 2o 3100 ℃ of reactions 5 hours, again obtain AlF 3thereby, realize AlF 3be cycled to repeat utilization.Reaction equation is as follows:
Fe 2O 3+2AlF 3→Al 2O 3+2FeF 3 （7）
3SiO 2+4AlF 3→3SiF 4+2Al 2O 3 （8）
FeF 3+3H 2O→Fe 2O 3+6HF （9）
Al 2O 3+6HF→2AlF 3+3H 2O （10）
Embodiment 3:
By Fe 2o 3coarse particles and NH 4hF 2mix Fe 2o 3with NH 4hF 2particle diameter be below 7mm, NH in gained mixture 4hF 2mass percent be 40%.By mixture temperature lower calcination 5 hours of 600 ℃ in the first reactor, generate NH 3, H 2o and FeF 3, FeF 3from solid, overflow.By the FeF overflowing 3introduce in the second reactor, and hydrolysis generates Fe at the temperature of 1100 ℃ 2o 3with HF gas.The HF gas that hydrolysis is produced is transported in the 3rd reactor with tetrafluoroethylene pipeline, with reaction product NH 3and H 2o, 150 ℃ of reactions 4.5 hours, obtains NH again 4hF 2thereby, realize NH 4hF 2be cycled to repeat utilization.Reaction equation is as follows:
Fe 2O 3+3NH 4HF 2→2FeF 3+3NH 3+3H 2O （11）
FeF 3+3H 2O→Fe 2O 3+6HF （12）
NH 3·H 2O+2HF→NH 4HF 2+H 2O （13）
Embodiment 4:
By limonite and NH 4f mixes, Fe 2o 3with the particle diameter of fluorochemical be below 3mm, NH in gained mixture 4the mass percent of F is 30%.By mixture temperature lower calcination 4.5 hours of 810 ℃ in the first reactor, generate NH 3, H 2o and FeF 3, by FeF 3from solid, distillation is overflowed.By the FeF overflowing 3introduce in the second reactor, and hydrolysis generates Fe at the temperature of 970 ℃ 2o 3with HF gas.The HF gas that hydrolysis is produced is transported in the 3rd reactor with tetrafluoroethylene pipeline, with reaction product NH 3and H 2o, 200 ℃ of reactions 1 hour, obtains NH again 4f, thus realize NH 4f is cycled to repeat utilization.Reaction equation is as follows:
Fe 2O 3+6NH 4F→2FeF 3+6NH 3+3H 2O （14）
2FeF 3+3H 2O→Fe 2O 3+6HF （15）
NH 3·H 2O+HF→NH 4F+H 2O （16）
The utilization ratio that the concrete numerical value of the parameters in embodiment 1-4 and the circulation of fluorochemical are reclaimed sees the following form 3:
The concrete numerical value of parameter of the each embodiment of table 3 and the rate of recovery of fluorochemical
Figure BDA0000470063620000101
Figure BDA0000470063620000111
The embodiment of the present invention provides a kind of method of efficiently utilizing fluorochemicals, belongs to inorganic fluorine Chemicals production technical field.Utilize F element and metal the first product (M in fluorine-containing material (AFz) xo ynFe 2o 3) in close fluorine element Al react, generate another kind of high-purity fluorochemicals, high-purity the first product is made in the hydrolysis that recycles this fluorine-containing material, and the HF finally reaction being generated reacts with the metallic element in fluorine-containing material, change again former fluorine-containing material into, and can return to technical process.High-purity fluorine compound only, as the intermediate product of reaction process, is nonexpendable in theory, thereby has realized the efficient utilization of fluorochemical, and the environmental pollution of avoiding fluorine element to cause.This method is reused fluorochemical, will produce good economic benefit and social benefit.The method processing step is few, and cost is low.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for a person skilled in the art, the present invention can have various modifications and variations.Within the spirit and principles in the present invention all, any modification of doing, be equal to replacement, improvement etc., within all should being included in protection scope of the present invention.

Claims (10)

1. a method for fluorochemical recycle in iron containing compounds production, is characterized in that, comprises the following steps:
(A) raw material containing Fe oxide compound is mixed with solid-state fluorochemical, form mixture;
(B) described mixture is calcined, wherein said containing the Fe in Fe oxide compound 3+with the F in described fluorochemical -generate the first product FeF 3gas, described containing the O in Fe oxide compound 2-generate the second product with the positively charged ion in described fluorochemical;
(C) described the first product passed into water vapour and reacts, making it to form and contain solid-state Fe 2o 3gas-solid mixture with gaseous state HF;
(D) after being separated, described gas-solid mixture obtains the first gas phase and the solid-state Fe that contain unreacted water vapour and gaseous state HF 2o 3;
(E) described the first gas phase is reacted with described the second product, again obtain described solid-state fluorochemical.
2. the method for fluorochemical recycle in a kind of iron containing compounds production according to claim 1, is characterized in that, the reaction conditions of described step (E) is to react 1-5h at 100-600 ℃ of temperature.
3. the method for fluorochemical recycle in a kind of iron containing compounds production according to claim 1, is characterized in that, described step (E) is specially:
First described the first gas phase cooling is obtained to hydrofluoric acid, more mixed to described hydrofluoric acid and described the second product being incorporated at 100-600 ℃ of temperature reacted to 1-5h, obtain described fluorochemical;
Or
First described the first gas phase is mixed with described the second product, more described the first gas phase cooling is obtained to hydrofluoric acid, finally described hydrofluoric acid is reacted to 1-5h with described the second product at 100-600 ℃ of temperature, obtain described fluorochemical.
4. the method for fluorochemical recycle in a kind of iron containing compounds production according to claim 1, is characterized in that, in described step (B), the condition of calcining for to calcine 1-5h at 600-1300 ℃.
5. the method for fluorochemical recycle in a kind of iron containing compounds production according to claim 1, is characterized in that the temperature 970-1300 ℃ of reaction in described step (C).
6. the method for fluorochemical recycle in a kind of iron containing compounds production according to claim 1, is characterized in that, described step (D) is specially:
Described gas-solid mixture is cooled to 100-280 ℃ and obtains the first gas phase and the solid-state Fe that contain unreacted water vapour and gaseous state HF after separating 2o 3; Adopt tetrafluoroethylene pipeline transport point state the first gas phase and mix with the second product.
7. the equipment of the method for fluorochemical recycle in a kind of iron containing compounds production as claimed in claim 1, is characterized in that, comprising: the first reactor, the second reactor, the 3rd reactor and separator;
Described the first reactor is for described mixture is calcined, wherein said containing the Fe in Fe oxide compound 3+with the F in described fluorochemical -generate the first product FeF 3gas, described containing the O in Fe oxide compound 2-generate the second product with the positively charged ion in described fluorochemical;
Described the second reactor, for described the first product is passed into water vapour and reacts, makes it to form and contains solid-state Fe 2o 3gas-solid mixture with gaseous state HF;
First gas phase and the solid-state Fe of described separator for obtaining after described gas-solid mixture is separated containing unreacted water vapour and gaseous state HF 2o 3;
Described the 3rd reactor is for reacting described the first gas phase again to obtain described fluorochemical with described the second product.
8. the equipment of the method for fluorochemical recycle in a kind of iron containing compounds production according to claim 7, is characterized in that, described separator is sack cleaner or cyclonic separator.
9. the equipment of the method for fluorochemical recycle in a kind of iron containing compounds production according to claim 7, is characterized in that, also comprises interchanger, and described interchanger is for obtaining hydrofluoric acid by described the first gas phase cooling.
10. the equipment of the method for fluorochemical recycle in a kind of iron containing compounds production according to claim 7, it is characterized in that, also comprise recirculated water coil pipe, the casing of described the 3rd reactor has recirculated water coil pipe, and described recirculated water coil pipe is for obtaining hydrofluoric acid by described the first gas phase cooling.
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