CN104211092A - Production process for preparing sodium pyrosulfite from pyrites - Google Patents
Production process for preparing sodium pyrosulfite from pyrites Download PDFInfo
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- CN104211092A CN104211092A CN201410418249.4A CN201410418249A CN104211092A CN 104211092 A CN104211092 A CN 104211092A CN 201410418249 A CN201410418249 A CN 201410418249A CN 104211092 A CN104211092 A CN 104211092A
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Abstract
The invention discloses a production process for preparing sodium pyrosulfite from pyrites. The production process comprises the following steps: roasting the pyrites used as a raw material in a fluidized bed furnace at 850-900 DEG C to generate sulfur dioxide gas; and removing dust by virtue of an electric dust remover, performing acid cleaning purification, and then sequentially performing back flow absorption reactions between the sulfur dioxide gas and a sodium carbonate saturated solution in first-stage, second-stage and third-stage reaction kettles under the condition that the solution temperature is controlled at 60+/-5 DEG C, thereby obtaining a sodium pyrosulfite product in the first-stage reaction kettle. The production process disclosed by the invention has simple steps, provides a new production process for preparing the sodium pyrosulfite, and can be used for producing sodium pyrosulfite by using the pyrites, and expanding the selection range of the raw materials for preparing the sodium pyrosulfite.
Description
Technical field
The present invention relates to pyrosulphite process for producing sodium field, mainly a kind of sulfurous iron ore produces pyrosulphite process for producing sodium.
Background technology
Sodium Pyrosulfite is white or yellow crystalline powder or little crystallization, with strong SO
2smell, proportion 1.4, water-soluble, the aqueous solution is acid, molecular formula: Na
2s
2o
5, mainly for the production of the raw material of vat powder etc., be used as reductive agent in industries such as organic intermediate, dyestuff, process hides, in grocery trade, be used as sanitas, SYNTHETIC OPTICAL WHITNER etc.
The production technique of current domestic Sodium Pyrosulfite generally adopts sulphur to be raw material, is burnt and generates sulfur dioxide gas, then react with soda ash solution and produce Sodium Pyrosulfite.
summary of the inventiontechnical problem to be solved by this invention is to provide a kind of sulfurous iron ore and produces pyrosulphite process for producing sodium, its processing step is simple, producing of Sodium Pyrosulfite adds a kind of new production technique, sulfurous iron ore can be utilized to produce Sodium Pyrosulfite, expand and produce Sodium Pyrosulfite to raw-material range of choice.
For solving the problems of the technologies described above, the technical solution used in the present invention is:
A kind of sulfurous iron ore produces pyrosulphite process for producing sodium, it is characterized in that: comprise the following steps:
(1), joining in fluidizing furnace by sulfurous iron ore and air, is carry out the roasting of weak oxygen magnetic under the condition of 850 DEG C in temperature, produce containing concentration of SO 2 gas be 10%(volumetric concentration) furnace gas;
(2) sulfur dioxide mixture gas being, 850 DEG C by the temperature that step (1) produces first cools to 380 DEG C by waste heat boiler; This furnace gas enters whirlwind again, electric precipitator carries out dry method dust, and after dedusting, furnace gas temperature is 300 DEG C, dust-laden is 0.2g/Nm3; Enter high energy scrubber again, stuffing washing tower two weak acid scrubbings purify further dedusting cooling after furnace gas temperature be 35 DEG C, dust-laden≤1mg/Nm3; Again through two-stage electrostatic precipitator and 92% vitriol oil paddle dryer tower remove portion SO
3acid mist and moisture content, now furnace gas temperature is 40 DEG C, SO
3acid mist 0.005 g/Nm3, moisture content 0.1 g/Nm3.
(3), the sulfur dioxide gas after step (2) dedusting and purification is carried out counter-current absorption reaction with saturated soda ash solution to sulfur dioxide gas in third order reaction still, main process is as follows: the sulfur dioxide gas after purification is sent in first, second and third order reaction still successively through blower fan, and concentration of SO 2 gas reduces step by step; Soda ash solution is added by third stage reactor, enter second more successively, first step reactor, three, the liquid phase of second order reaction still is mainly sodium sulfite solution, because in first step reactor, concentration of SO 2 gas is the highest, sulfurous gas can be made to carry out excessive reaction, and when first step reactor pH value reaches 4, absorption reaction reaches terminal, and generating Sodium Pyrosulfite crystallization suspension, each temperature of reaction kettle should control at 60 ± 5 DEG C.Third stage reactor tail gas out discharges with after alkali liquor absorption again, and tail gas sulphur dioxide concentration is less than 50ppm, joins second stage reactor and participate in reaction when absorption liquid pH value reaches 6.5.
(4) the Sodium Pyrosulfite suspension, obtained step (3) carries out centrifuge dehydration and is drying to obtain Sodium Pyrosulfite product.
Advantage of the present invention is:
Present invention process step is simple, and producing of Sodium Pyrosulfite adds a kind of new production technique, sulfurous iron ore can be utilized to produce Sodium Pyrosulfite, expand and produce Sodium Pyrosulfite to raw-material range of choice.
Accompanying drawing explanation
Fig. 1 is present invention process schema.
Embodiment
See Fig. 1, a kind of sulfurous iron ore produces pyrosulphite process for producing sodium, comprises the following steps:
(1), joining in fluidizing furnace by sulfurous iron ore and air, is carry out the roasting of weak oxygen magnetic under the condition of 850 DEG C in temperature, produce containing concentration of SO 2 gas be 10%(volumetric concentration) furnace gas;
(2) sulfur dioxide mixture gas being, 850 DEG C by the temperature that step (1) produces first cools to 380 DEG C by waste heat boiler; This furnace gas enters whirlwind again, electric precipitator carries out dry method dust, and after dedusting, furnace gas temperature is 300 DEG C, dust-laden is 0.2g/Nm3; Enter high energy scrubber again, stuffing washing tower two weak acid scrubbings purify further dedusting cooling after furnace gas temperature be 35 DEG C, dust-laden≤1mg/Nm3; Again through two-stage electrostatic precipitator and 92% vitriol oil paddle dryer tower remove portion SO
3acid mist and moisture content, now furnace gas temperature is 40 DEG C, SO
3acid mist 0.005 g/Nm3, moisture content 0.1 g/Nm3.
(3), the sulfur dioxide gas after step (2) dedusting and purification is carried out counter-current absorption reaction with saturated soda ash solution to sulfur dioxide gas in third order reaction still, main process is as follows: the sulfur dioxide gas after purification is sent in first, second and third order reaction still successively through blower fan, and concentration of SO 2 gas reduces step by step; Soda ash solution is added by third stage reactor, enter second more successively, first step reactor, three, the liquid phase of second order reaction still is mainly sodium sulfite solution, because in first step reactor, concentration of SO 2 gas is the highest, sulfurous gas can be made to carry out excessive reaction, and when first step reactor pH value reaches 4, absorption reaction reaches terminal, and generating Sodium Pyrosulfite crystallization suspension, each temperature of reaction kettle should control at 60 ± 5 DEG C.Third stage reactor tail gas out discharges with after alkali liquor absorption again, and tail gas sulphur dioxide concentration is less than 50ppm, joins second stage reactor and participate in reaction when absorption liquid pH value reaches 6.5.
(4) the Sodium Pyrosulfite suspension, obtained step (3) carries out centrifuge dehydration and is drying to obtain Sodium Pyrosulfite product.
Claims (1)
1. sulfurous iron ore produces a pyrosulphite process for producing sodium, it is characterized in that comprising the following steps:
(1), joining in fluidizing furnace by the sulfurous iron ore and air that are less than 4mm, is carry out the roasting of weak oxygen magnetic under the condition of 850 ~ 900 DEG C in temperature, produce containing concentration of SO 2 gas be 10%(volumetric concentration) furnace gas;
(2) the sulfurous gas furnace gas being, 850 DEG C by the temperature that step (1) produces first cools to 380 DEG C by waste heat boiler; This furnace gas enters whirlwind again, electric precipitator carries out dry method dust, and after dedusting, furnace gas temperature is 300 DEG C, dust-laden is 0.2g/Nm3; Enter high energy scrubber again, stuffing washing tower two weak acid scrubbings purify further dedusting cooling after furnace gas temperature be 35 DEG C, dust-laden≤1mg/Nm3; Again through two-stage electrostatic precipitator and 92% vitriol oil paddle dryer tower remove portion SO
3acid mist and moisture content, now furnace gas temperature is 40 DEG C, SO
3acid mist is 0.005 g/Nm3, moisture content 0.1 g/Nm3;
(3), the sulfur dioxide gas after step (2) dedusting and purification is carried out counter-current absorption reaction with saturated soda ash solution to sulfur dioxide gas in third order reaction still, main process is as follows: the sulfur dioxide gas after purification is sent in first, second and third order reaction still successively through blower fan, and concentration of SO 2 gas reduces step by step; Soda ash solution is added by third stage reactor, enter second more successively, first step reactor, three, the liquid phase of second order reaction still is mainly sodium sulfite solution, because in first step reactor, concentration of SO 2 gas is the highest, sulfurous gas can be made to carry out excessive reaction, and when first step reactor pH value reaches 4, absorption reaction reaches terminal, and generating Sodium Pyrosulfite crystallization suspension, each temperature of reaction kettle should control at 60 ± 5 DEG C;
Third stage reactor tail gas out discharges with after alkali liquor absorption again, and tail gas sulphur dioxide concentration is less than 50ppm, joins second stage reactor and participate in reaction when absorption liquid pH value reaches 6.5;
(4) the Sodium Pyrosulfite suspension, obtained step (3) carries out centrifuge dehydration and is drying to obtain Sodium Pyrosulfite product.
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105565343A (en) * | 2015-12-28 | 2016-05-11 | 宣城市楷昂化工有限公司 | Sodium metabisulfite production method |
| CN105565344A (en) * | 2015-12-28 | 2016-05-11 | 宣城市楷昂化工有限公司 | Sodium metabisulfite production system |
| CN107089671A (en) * | 2016-02-18 | 2017-08-25 | 金昌正旭工贸有限责任公司 | A kind of wet process technique of sodium pyrosulfite |
| CN107792867A (en) * | 2017-11-21 | 2018-03-13 | 合肥四方磷复肥有限责任公司 | A kind of sodium pyrosulfite preparation technology utilized based on feedstock circulation |
| CN108328582A (en) * | 2018-03-13 | 2018-07-27 | 王东阳 | A kind of preparation method of medical-grade sodium pyrosulfite |
| CN109607575A (en) * | 2018-01-25 | 2019-04-12 | 朱华东 | A method of sodium pyrosulfite is produced using coking desulfurization waste liquor and thick sulphur |
| CN109970081A (en) * | 2019-03-22 | 2019-07-05 | 扬州康龙环保工程有限公司 | A method of sodium pyrosulfite is prepared using coking sulphur cream |
| WO2021004122A1 (en) * | 2019-07-10 | 2021-01-14 | 南京杰科丰环保技术装备研究院有限公司 | Device and method for preparing sulfite |
| WO2021114851A1 (en) * | 2019-12-13 | 2021-06-17 | 江苏德义通环保科技有限公司 | System for producing sodium pyrosulfite |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5976485A (en) * | 1996-10-07 | 1999-11-02 | Solvay Minerals, Inc. | Sodium metabisulfite process |
| CN102659142A (en) * | 2012-04-17 | 2012-09-12 | 伍立君 | Preparation device and preparation method of sodium pyrosulfite and anhydrous sodium sulphite |
-
2014
- 2014-08-22 CN CN201410418249.4A patent/CN104211092A/en active Pending
Patent Citations (2)
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|---|---|---|---|---|
| US5976485A (en) * | 1996-10-07 | 1999-11-02 | Solvay Minerals, Inc. | Sodium metabisulfite process |
| CN102659142A (en) * | 2012-04-17 | 2012-09-12 | 伍立君 | Preparation device and preparation method of sodium pyrosulfite and anhydrous sodium sulphite |
Non-Patent Citations (1)
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| 孙轶: "焦亚硫酸钠及其生产工艺", 《化工生产与技术》 * |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105565343A (en) * | 2015-12-28 | 2016-05-11 | 宣城市楷昂化工有限公司 | Sodium metabisulfite production method |
| CN105565344A (en) * | 2015-12-28 | 2016-05-11 | 宣城市楷昂化工有限公司 | Sodium metabisulfite production system |
| CN107089671A (en) * | 2016-02-18 | 2017-08-25 | 金昌正旭工贸有限责任公司 | A kind of wet process technique of sodium pyrosulfite |
| CN107792867A (en) * | 2017-11-21 | 2018-03-13 | 合肥四方磷复肥有限责任公司 | A kind of sodium pyrosulfite preparation technology utilized based on feedstock circulation |
| CN109607575A (en) * | 2018-01-25 | 2019-04-12 | 朱华东 | A method of sodium pyrosulfite is produced using coking desulfurization waste liquor and thick sulphur |
| CN108328582A (en) * | 2018-03-13 | 2018-07-27 | 王东阳 | A kind of preparation method of medical-grade sodium pyrosulfite |
| CN109970081A (en) * | 2019-03-22 | 2019-07-05 | 扬州康龙环保工程有限公司 | A method of sodium pyrosulfite is prepared using coking sulphur cream |
| WO2021004122A1 (en) * | 2019-07-10 | 2021-01-14 | 南京杰科丰环保技术装备研究院有限公司 | Device and method for preparing sulfite |
| WO2021114851A1 (en) * | 2019-12-13 | 2021-06-17 | 江苏德义通环保科技有限公司 | System for producing sodium pyrosulfite |
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