CN204039299U - A kind of purifying plant of high-purity sodium formate - Google Patents
A kind of purifying plant of high-purity sodium formate Download PDFInfo
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- CN204039299U CN204039299U CN201420426640.4U CN201420426640U CN204039299U CN 204039299 U CN204039299 U CN 204039299U CN 201420426640 U CN201420426640 U CN 201420426640U CN 204039299 U CN204039299 U CN 204039299U
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Abstract
The utility model discloses a kind of purifying plant of high-purity sodium formate, comprise the first whizzer, dissolving vessel, vacuum centrifuge, airtight rake type dryer, sedimentation precipitation tank, the 3rd whizzer, vaporizer, crystallisation by cooling tank, the 4th whizzer, recrystallization tank, bleacher, filter press device, recirculated water cooling condenser, water ice condenser, solvent receiving tank, solvent feed tank and solvent delivery pump.Sodium formiate is purified to 99.5% or higher by the utility model, and has reclaimed part tetramethylolmethane.With traditional from tetramethylolmethane compared with purifying formic acid sodium, this system achieves the raising of sodium formiate purity on the one hand, also achieves the recycle of raw material on the other hand, and this technical process is simple, workable, is worthy to be popularized.
Description
Technical field
The utility model relates to a kind of purifying plant of high-purity sodium formate.
Background technology
Sodium formiate is a kind of important organic raw material, has another name called sodium formate, and outward appearance is white crystalline powder.Sodium formiate is widely used in printing and dyeing, the chemical production field such as organic synthesis, medicine, as can be used as the rawhide treatment agent of leather industry, the dye leveller of dope dyeing industry, the promotor of electroplating industry, the matting agent etc. of artificial silk industry, also can be used as the main raw material producing formic acid and oxalic acid, is also the raw material producing vat powder.It is reported that national sodium formiate ultimate production is about 200KT.Current sodium formiate main production process has carbon monoxide synthesis method and byproduct of polyhydric alcohol method.
Carbon monoxide synthesis method: use coke is raw material, through the technique such as gas making dedusting, washing, decarburization, again dedusting, obtain the CO (carbon monoxide converter) gas needed for technique, then after heating and pressurizing and sodium hydroxide are reacted and generated sodium formate solution, through evaporation, be separated, dryly generate solid phase prod sodium formiate.This technique is the technique of professional production sodium formiate.Advantage is due to not containing other alcohols, produces carboxylic acid Yield high; The colourity of this process purity more than 97% is also relatively good, and export volume is larger.But due to coal resources reason, its industrial scale is restricted, processing unit is backward, product is single, water power vapour cost is high, lack competitiveness.
Byproduct of polyhydric alcohol method: adopt acetaldehyde/butyraldehyde-n/isobutyric aldehyde and formalin and excessive formaldehyde that Cannizzaro's reaction occurs to intersect under basic conditions and generate the polyvalent alcohol of tetramethylolmethane/TriMethylolPropane(TMP)/neopentyl glycol.Along with developing rapidly of China's polyvalent alcohol industry, the amount of whole nation neopentyl glycol, tetramethylolmethane, TriMethylolPropane(TMP) byproduct sodium formiate is more than 80,000 tons, and polyvalent alcohol production plant to the processing mode that polyvalent alcohol mother liquor is conventional is: through concentrated, crystallization, centrifugation, obtain sodium formiate solid.For sodium formiate, traditional employing sodium legal system gets tetramethylolmethane and byproduct, wherein, the byproduct that sodium formiate produces for sodium method production tetramethylolmethane, Production of pentaerythritol technique is got in sodium legal system, due to the restriction of tripping device and condition, the sodium formiate content separated is 88%-92%, the moisture controlled of sodium formiate is about 1.5%, other organism tetramethylolmethane and dipentaerythritol content are 3%-10%, the organism such as tetramethylolmethane and dipentaerythritol is not separated, and is present in sodium formiate product with the form of impurity.Tetramethylolmethane in sodium formiate is separated into the difficult point that sodium method produces a kind of key of tetramethylolmethane, the existence one of tetramethylolmethane is the lifting having a strong impact on sodium formiate product content, this thick sodium formiate solid color is darker, be generally tawny, with strong organism smell, easy caking, can not unrestricted flow.Two is that a large amount of tetramethylolmethanes is taken away by sodium formiate product, and sodium formiate product, well below the price of tetramethylolmethane, brings serious financial loss to enterprise.Therefore; it is high to there is energy consumption in current employing byproduct of polyhydric alcohol sodium formiate production technique; production cost is high; sodium formiate content can not meet the demand in market; the market competitiveness is poor, and along with the growing tension of world resource, the strategy of sustainable development is more and more paid attention to; country also promotes recycling economy energetically and reduces energy consumption, reserved resource.Given this improve sodium formiate content further and reduce production cost and have great meaning to enterprise's raising market competitiveness.
Utility model content
In order to overcome deficiency of the prior art, the utility model provides a kind of purifying plant of high-purity sodium formate.
For solving the problem, the utility model adopts following technical scheme:
A purifying plant for high-purity sodium formate, is characterized in that: comprise the first whizzer, dissolving vessel, vacuum centrifuge, airtight rake type dryer, sedimentation precipitation tank, the 3rd whizzer, vaporizer, crystallisation by cooling tank, the 4th whizzer, recrystallization tank, bleacher, filter press device, recirculated water cooling condenser, water ice condenser, solvent receiving tank, solvent feed tank and solvent delivery pump;
First whizzer, dissolving vessel, vacuum centrifuge and airtight rake type dryer pipeline communication in turn;
First whizzer, sedimentation separate out tank, the 3rd whizzer, vaporizer, crystallisation by cooling tank, the 4th whizzer and recrystallization tank pipeline communication in turn;
Tank pipeline communication is separated out in vacuum centrifuge and sedimentation; 3rd whizzer and dissolving vessel pipeline communication;
Tank pipeline communication is in turn separated out in 4th whizzer, bleacher, filter press device and sedimentation;
Recirculated water cooling condenser and water ice condenser pipeline communication, dissolving vessel, airtight rake type dryer and vaporizer respectively with circulating water condensing device pipeline communication;
Recirculated water cooling condenser and water ice condenser respectively with solvent receiving tank pipeline communication, solvent receiving tank, solvent feed tank, solvent delivery pump and dissolving vessel pipeline communication in turn.
When said apparatus uses, the centrifuging while hot of the first whizzer is first used after residual mother liquor high-temperature pressure-reduction is concentrated, obtain the first filtrate and the first filter cake, first filter cake is the sodium formiate of 88%-92%, first filter cake enters dissolving vessel, with the impurity organism contained by alcohol, ketone, ethers organism dissolving sodium formiate, by centrifugal for gained mixture vacuum centrifuge, obtain the second filter cake and the second filtrate, second filtrate is transferred to sedimentation and separates out tank, and the second filter cake then obtains the sodium formiate product that content is greater than 99.5% to airtight rake type dryer drying, first filtrate pumps into sedimentation and separates out tank, first filtrate and the second filtrate are separated out after tank sedimentation through sedimentation and are sent to the 3rd centrifuge, obtain the 3rd filter cake (sodium formiate that purity is greater than 85%) and the 3rd filtrate, 3rd filter cake flows to dissolving vessel and enters downstream in company with the material in dissolving vessel, but be transferred to vaporizer when moisture is more than 20% in the 3rd filtrate, after evaporation concentration, solution is transferred to crystallisation by cooling tank and stirs lower crystallisation by cooling, the 4th centrifuge is transferred to after crystallisation by cooling, obtain the 4th filtrate and the 4th filter cake, 4th filter cake is the organism such as tetramethylolmethane and dipentaerythritol, be sent to recrystallization tank recrystallization, 4th filtrate is decoloured 2 hours at being transferred to bleacher activated carbon 60-75 DEG C, destainer is by after filter press device press filtration removing activated carbon, filtrate returns sedimentation and separates out tank, the material of separating out in tank in company with sedimentation enters downstream.The gas that the drying of vacuum centrifuge, rake type dryer, dissolving vessel and vaporizer produce in the course of the work all leads to recirculated water cooling condenser, recirculated water cooling condenser link ice water condensation apparatus, the condensate outlet of recirculated water cooling condenser and water ice condenser links with solvent receiving tank.
After above-mentioned 4th centrifuge mother liquor by the recrystallization that adds water, centrifugally reclaim out tetramethylolmethane, the mother liquor after recentrifuge then to decolour etc. and to return sedimentation after process and separate out tank and be made into sodium formiate raw material.Improve the yield of tetramethylolmethane and sodium formiate.
The production equipment structure of the utility model high-purity sodium formate is simple, easily implement, easy to control, the purity that can improve byproduct sodium formiate is greater than 99.5%, adds tetramethylolmethane output simultaneously, reduces the steam energy consumption of technique.
The purifying plant of above-mentioned high-purity sodium formate, also comprises liquid-ring vacuum pump and emptying water ice condenser, water ice condenser, liquid-ring vacuum pump and emptying water ice condenser pipeline communication in turn; Emptying water ice condenser and solvent receiving tank pipeline communication.Further condensation can be played by waste gas like this, the recovery utilization rate of waste gas is provided, deduction and exemption atmospheric pollution, non-condensable gases emptying after liquid-ring vacuum pump high velocity flow band.
Flow control valve is equipped with on the pipeline that recirculated water cooling condenser is communicated with water ice condenser and on the pipeline that is communicated with liquid-ring vacuum pump of water ice condenser.Carry out the opening degree of adjust flux variable valve according to actual condensation situations, avoid the waste of the energy.
Preferably, the connecting pipe between each parts is equipped with variable valve.
Plate Filtration pump is provided with between bleacher and filter press device.Facilitate mass transport like this, other place of this device also can arrange various transferpump as required certainly.
The pipeline that 3rd whizzer is communicated with vaporizer branches into two-way after the 3rd whizzer is drawn, and a-road-through returns sedimentation separate out tank to vaporizer, another road.Can select the 3rd filtrate to be entered vaporizer according to practical situation so is still back in sedimentation precipitation tank, the back amount of sodium formiate and tetramethylolmethane in mother liquor can be made so significantly to reduce, separating formic sodium and tetramethylolmethane respectively, decrease influencing each other when recrystallization between them, and then reduce system evaporation load, reduce evaporation energy consumption simultaneously.
Vacuum centrifuge and circulating water condensing device pipeline communication.The gas produced in vacuum centrifuge can be made like this to obtain reuse, avoid the pollution of air simultaneously.
Dissolving vessel is located at the below of the first whizzer and the 3rd whizzer; Airtight rake type dryer is located at the below of vacuum centrifuge; Recrystallization tank is located at the below of the 4th whizzer.Each like this filter cake, without the need to by under the effect of other external force, can flow into next equipment smoothly.
The NM technology of the utility model is prior art.
The purifying plant of the utility model high-purity sodium formate achieves separating formic sodium and tetramethylolmethane type organic from low levels sodium formiate product, improves sodium formiate product content and quality, expands the Application Areas of sodium formiate, improves sodium formiate selling price; Increase tetramethylolmethane output, reduce steam energy consumption, reduce the production cost of tetramethylolmethane technique on the whole, strengthen market competitiveness of enterprises; With traditional from compared with tetramethylolmethane byproduct sodium formate, the present invention not only effectively purifying formic acid sodium purity to more than 99.5%, simultaneously, part tetramethylolmethane has directly been reclaimed from mother liquor, mother liquor back amount is significantly reduced, reduces system evaporation load, reduce evaporation energy consumption simultaneously, and in the sepn process of waste liquid purifying formic acid sodium, achieve zero release, for realizing Business Economic Benefit and environmental benefit has great meaning; With traditional from tetramethylolmethane compared with purifying formic acid sodium, this system achieves the raising of sodium formiate purity on the one hand, also achieves the recycle of raw material on the other hand, and this technical process is simple, workable, is worthy to be popularized.
Accompanying drawing explanation
Fig. 1 is the purifying plant structural representation of the utility model high-purity sodium formate.
In figure, 1 is the first whizzer, 2 is dissolving vessel, 3 is vacuum centrifuge, 4 is airtight rake type dryer, 5 is sedimentation precipitation tank, 6 is the 3rd whizzer, 7 is vaporizer, 8 is crystallisation by cooling tank, 9 is the 4th whizzer, 10 attach most importance to crystallizer, 11 is bleacher, 12 is filter press device, 13 is recirculated water cooling condenser, 14 is water ice condenser, 15 is solvent receiving tank, 16 is liquid-ring vacuum pump, 17 is emptying water ice condenser, 18 is solvent feed tank, 19 is Plate Filtration pump, 20 is solvent delivery pump, 21 is the first filtrate, 22 is the first filter cake, 23 is the second filtrate, 24 is the second filter cake, 25 is the 3rd filtrate, 26 is the 3rd filter cake, 27 is the 4th filtrate, 28 is the 4th filter cake, 29 emptying, 30 high-purity sodium formates.
Embodiment
In order to understand the utility model better, illustrate content of the present utility model further below in conjunction with embodiment, but content of the present utility model is not only confined to the following examples.
Embodiment 1
The purifying plant of high-purity sodium formate as shown in Figure 1, comprises the first whizzer, dissolving vessel, vacuum centrifuge, airtight rake type dryer, sedimentation precipitation tank, the 3rd whizzer, vaporizer, crystallisation by cooling tank, the 4th whizzer, recrystallization tank, bleacher, filter press device, recirculated water cooling condenser, water ice condenser, solvent receiving tank, solvent feed tank, solvent delivery pump, liquid-ring vacuum pump and emptying water ice condenser; First whizzer, dissolving vessel, vacuum centrifuge and airtight rake type dryer pipeline communication in turn; First whizzer, sedimentation separate out tank, the 3rd whizzer, vaporizer, crystallisation by cooling tank, the 4th whizzer and recrystallization tank pipeline communication in turn; The pipeline that 3rd whizzer is communicated with vaporizer branches into two-way after the 3rd whizzer is drawn, and a-road-through returns sedimentation separate out tank to vaporizer, another road.Tank pipeline communication is separated out in vacuum centrifuge and sedimentation; 3rd whizzer and dissolving vessel pipeline communication; Tank pipeline communication is in turn separated out in 4th whizzer, bleacher, filter press device and sedimentation, is provided with Plate Filtration pump between bleacher and filter press device.Recirculated water cooling condenser, water ice condenser, liquid-ring vacuum pump and emptying water ice condenser pipeline communication in turn, vacuum centrifuge, dissolving vessel, airtight rake type dryer and vaporizer respectively with circulating water condensing device pipeline communication; Emptying water ice condenser, recirculated water cooling condenser and water ice condenser respectively with solvent receiving tank pipeline communication, solvent receiving tank, solvent feed tank, solvent delivery pump and dissolving vessel pipeline communication in turn.Flow control valve is equipped with on the pipeline that recirculated water cooling condenser is communicated with water ice condenser and on the pipeline that is communicated with liquid-ring vacuum pump of water ice condenser.Dissolving vessel is located at the below of the first whizzer and the 3rd whizzer; Airtight rake type dryer is located at the below of vacuum centrifuge; Recrystallization tank is located at the below of the 4th whizzer.
When said apparatus uses, the centrifuging while hot of the first whizzer is first used after residual mother liquor high-temperature pressure-reduction is concentrated, obtain the first filtrate and the first filter cake, first filter cake is the sodium formiate of 88%-92%, first filter cake enters dissolving vessel, with the impurity organism contained by alcohol, ketone, ethers organism dissolving sodium formiate, by centrifugal for gained mixture vacuum centrifuge, obtain the second filter cake and the second filtrate, second filtrate is transferred to sedimentation and separates out tank, and the second filter cake then obtains the sodium formiate product that content is greater than 99.5% to airtight rake type dryer drying, first filtrate pumps into sedimentation and separates out tank, first filtrate and the second filtrate are separated out after tank sedimentation through sedimentation and are sent to the 3rd centrifuge, obtain the 3rd filter cake (sodium formiate that purity is greater than 85%) and the 3rd filtrate, 3rd filter cake flows to dissolving vessel and enters downstream in company with the material in dissolving vessel, but be transferred to vaporizer when moisture is more than 20% in the 3rd filtrate, after evaporation concentration, solution is transferred to crystallisation by cooling tank and stirs lower crystallisation by cooling, the 4th centrifuge is transferred to after crystallisation by cooling, obtain the 4th filtrate and the 4th filter cake, 4th filter cake is the organism such as tetramethylolmethane and dipentaerythritol, be sent to recrystallization tank recrystallization, 4th filtrate is decoloured 2 hours at being transferred to bleacher activated carbon 60-75 DEG C, destainer is by after filter press device press filtration removing activated carbon, filtrate returns sedimentation and separates out tank, the material of separating out in tank in company with sedimentation enters downstream.The gas that the drying of vacuum centrifuge, rake type dryer, dissolving vessel and vaporizer produce in the course of the work all leads to recirculated water cooling condenser, recirculated water cooling condenser link ice water condensation apparatus, the condensate outlet of recirculated water cooling condenser and water ice condenser links with solvent receiving tank.
Claims (7)
1. a purifying plant for high-purity sodium formate, is characterized in that: comprise the first whizzer, dissolving vessel, vacuum centrifuge, airtight rake type dryer, sedimentation precipitation tank, the 3rd whizzer, vaporizer, crystallisation by cooling tank, the 4th whizzer, recrystallization tank, bleacher, filter press device, recirculated water cooling condenser, water ice condenser, solvent receiving tank, solvent feed tank and solvent delivery pump;
First whizzer, dissolving vessel, vacuum centrifuge and airtight rake type dryer pipeline communication in turn;
First whizzer, sedimentation separate out tank, the 3rd whizzer, vaporizer, crystallisation by cooling tank, the 4th whizzer and recrystallization tank pipeline communication in turn;
Tank pipeline communication is separated out in vacuum centrifuge and sedimentation; 3rd whizzer and dissolving vessel pipeline communication;
Tank pipeline communication is in turn separated out in 4th whizzer, bleacher, filter press device and sedimentation;
Recirculated water cooling condenser and water ice condenser pipeline communication, dissolving vessel, airtight rake type dryer and vaporizer respectively with circulating water condensing device pipeline communication;
Recirculated water cooling condenser and water ice condenser respectively with solvent receiving tank pipeline communication, solvent receiving tank, solvent feed tank, solvent delivery pump and dissolving vessel pipeline communication in turn.
2. the purifying plant of high-purity sodium formate as claimed in claim 1, is characterized in that: also comprise liquid-ring vacuum pump and emptying water ice condenser, water ice condenser, liquid-ring vacuum pump and emptying water ice condenser pipeline communication in turn; Emptying water ice condenser and solvent receiving tank pipeline communication.
3. the purifying plant of high-purity sodium formate as claimed in claim 2, is characterized in that: be equipped with flow control valve on the pipeline that recirculated water cooling condenser is communicated with water ice condenser and on the pipeline that is communicated with liquid-ring vacuum pump of water ice condenser.
4. the purifying plant of the high-purity sodium formate as described in claim 1-3 any one, is characterized in that: be provided with Plate Filtration pump between bleacher and filter press device.
5. the purifying plant of the high-purity sodium formate as described in claim 1-3 any one, is characterized in that: the pipeline that the 3rd whizzer is communicated with vaporizer branches into two-way after the 3rd whizzer is drawn, and a-road-through returns sedimentation separate out tank to vaporizer, another road.
6. the purifying plant of the high-purity sodium formate as described in claim 1-3 any one, is characterized in that: vacuum centrifuge and circulating water condensing device pipeline communication.
7. the purifying plant of the high-purity sodium formate as described in claim 1-3 any one, is characterized in that: dissolving vessel is located at the below of the first whizzer and the 3rd whizzer; Airtight rake type dryer is located at the below of vacuum centrifuge; Recrystallization tank is located at the below of the 4th whizzer.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106699587A (en) * | 2016-12-19 | 2017-05-24 | 宜昌三峡制药有限公司 | Isoleucine crystallizing and washing method and device |
| CN109704949A (en) * | 2018-12-10 | 2019-05-03 | 安徽金禾实业股份有限公司 | The separation method of sodium formate in a kind of production of neopentyl glycol |
| CN110194715A (en) * | 2019-05-16 | 2019-09-03 | 湖北楚星化工股份有限公司 | A kind of production method of sodium formate |
-
2014
- 2014-07-30 CN CN201420426640.4U patent/CN204039299U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106699587A (en) * | 2016-12-19 | 2017-05-24 | 宜昌三峡制药有限公司 | Isoleucine crystallizing and washing method and device |
| CN109704949A (en) * | 2018-12-10 | 2019-05-03 | 安徽金禾实业股份有限公司 | The separation method of sodium formate in a kind of production of neopentyl glycol |
| CN110194715A (en) * | 2019-05-16 | 2019-09-03 | 湖北楚星化工股份有限公司 | A kind of production method of sodium formate |
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| C14 | Grant of patent or utility model | ||
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| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20141224 Termination date: 20190730 |