CN204428875U - The complete continuous crystallisation production process equipment of a kind of methenamine - Google Patents
The complete continuous crystallisation production process equipment of a kind of methenamine Download PDFInfo
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- CN204428875U CN204428875U CN201520004704.6U CN201520004704U CN204428875U CN 204428875 U CN204428875 U CN 204428875U CN 201520004704 U CN201520004704 U CN 201520004704U CN 204428875 U CN204428875 U CN 204428875U
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Abstract
The utility model discloses the complete continuous crystallisation production process equipment of a kind of methenamine, this equipment comprises the evaporation concentrator, vapour liquid separator, steaming liquid feeder and the crystallizing evaporator that are connected successively by pipeline, and vacuum extractor and heat exchanger.The utility model is linked up with dual evaporation crystallization one-level evaporation, through the further continuous crystallisation of dual evaporation crystallizer, the comparatively megacryst formed in evaporation process is because of the first sedimentation of gravitate, thin crystalline substance and solution up further concentrated, thus formed mend continuous extraction after comparatively megacryst settles down after remove moisture content, therefore, the utility model realizes the continuous seepage of methenamine evaporative crystallization, while reducing production cost, floor space and labour intensity, improve quality and the stability of product, and reduce steam consumption.
Description
Technical field
The utility model belongs to chemical production technology and equipment technical field, relates generally to methenamine continuous production device.
Background technology
Existing methenamine generally concentrates through twice.One-level is that negative pressure rises film or falling film evaporation, and secondary is that negative pressure is by tank evaporative crystallization.Two-stage all uses primary steam as thermal source.Its Problems existing is: 1, two-stage all uses Steam Heating, and secondary vapour is directly absorbed or condensation, causes the cooling water inflow that very large steam use amount is large and needs are larger.2, single tank is interrupted evaporative crystallization and needs a lot of jar, and take up an area comparatively large and unstable quality, amount of investment is also large.3, owing to not having crystal seed in tank before single tank evaporative crystallization, cause thin crystalline substance many, particle is uneven, centrifugal bad from, moisture is high.4, often steam a tank needs workman to keep in the feed supplement of tank limit and observation situation always, and constantly adjust liquid level and add heat and vacuum, tank is too many, and labour intensity is large, and man's activity is comparatively large, and between batch, quality differs.The workman needed is many and labour intensity is large.5, continuous seepage, yield in unit time increases.Administration measure.
Utility model content
Utility model object: for above-mentioned Problems existing and defect, the utility model provides the complete continuous crystallisation production process equipment of a kind of methenamine, realize methenamine continuous crystallisation to produce, reduce production cost and floor space, while labour intensity, improve quality and the stability of product.
Technical scheme: for realizing above-mentioned utility model object, the utility model is by the following technical solutions: the complete continuous crystallisation production process equipment of a kind of methenamine, comprise the evaporation concentrator, vapour liquid separator, steaming liquid feeder and the crystallizing evaporator that are connected successively by pipeline, also comprise vacuum extractor and heat exchanger, the gaseous phase outlet of described vapour liquid separator is connected with vacuum extractor, wherein:
Described crystallizing evaporator comprises tower body, it is the inlet of tangential direction that described tower body is provided with tower body, the upper and lower of inlet is respectively vapor-liquid separation section and crystallized region, described vapor-liquid separation section is blank pipe section, and top is provided with demister, the mozzle for the liquid to be concentrated that circulates is provided with in the middle of the cylindrical shell of described crystallized region, this mozzle is near the bottom of crystallized region and the port of export is provided with distributor that liquid to be concentrated is flowed out from port of export side, the bottom of described crystallized region is for leaving standstill district, and mozzle outside is flotation area, and the top of flotation area is also provided with liquid outlet, form circulation by circulating pump and pipeline communication between described liquid outlet and inlet, and described heat exchanger is located at this circulating line, the top of described vapor-liquid separation section is also provided with indirect steam outlet and is connected with the entrance of evaporation concentrator by pipeline, thus provides thermal source to evaporation concentrator.
Such scheme is lost no time further, between the gaseous phase outlet of described vapour liquid separator and vacuum extractor, is also provided with condenser.
As preferably, described evaporation concentrator is climbing-film evaporation inspissator or falling film evaporation inspissator.
Beneficial effect: compared with prior art, the utility model has the following advantages: the continuous seepage realizing methenamine evaporative crystallization, while reducing production cost, floor space and labour intensity, improve quality and the stability of product, and reduce steam consumption.
Accompanying drawing explanation
Fig. 1 is the structural representation of the complete continuous crystallisation production process equipment of methenamine described in the utility model;
Fig. 2 is the structural representation of crystallizing evaporator described in the utility model;
Fig. 3 is A-A direction top view in Fig. 2.
Wherein, vacuum extractor 1, evaporation concentrator 2, first vapour liquid separator 3, steaming liquid feeder 4, crystallizing evaporator 5, inlet 51, gas-liquid separation section 52, crystallized region 53, demister 54, mozzle 55, distributor 56, flotation area 57, standing district 58, liquid outlet 59, indirect steam outlet 510, heat exchanger 6, condenser 7, condensate storage 8, second gas-liquid separator 9, liquid collection trough 10.
Detailed description of the invention
Below in conjunction with the drawings and specific embodiments, illustrate the utility model further, these embodiments should be understood and be only not used in restriction scope of the present utility model for illustration of the utility model, after having read the utility model, the amendment of those skilled in the art to the various equivalent form of value of the present utility model has all fallen within the application's claims limited range.
As shown in Figure 1, the complete continuous crystallisation production process equipment of a kind of methenamine, comprise the evaporation concentrator, vapour liquid separator, steaming liquid feeder and the crystallizing evaporator that are connected successively by pipeline, also comprise vacuum extractor and heat exchanger, the gaseous phase outlet of described vapour liquid separator is connected with vacuum extractor, wherein:
During work, the tube side that the methenamine solution of the dilute concentration of about 20% enters evaporation concentrator carries out one-level evaporation, and under the effect of vapour liquid separator vapor-liquid separation, obtain the solution of 40 ~ 50% concentration, in this process, methenamine has 40 ~ 50 DEG C to be heated to 70 ~ 80 DEG C, and provides thermal source close to the indirect steam of 100 DEG C.Denseer methenamine solution, after collecting, after mixing, then enters continuous crystallisation in crystallizing evaporator, finally obtain methenamine crystalline solid as fresh concentrate with the liquid of crystallizing evaporator liquid outlet after heat exchanger heating
As shown in Figures 2 and 3, the utility model crystallizing evaporator comprises tower body, it is the inlet of tangential direction that described tower body is provided with tower body, the upper and lower of inlet is respectively vapor-liquid separation section and crystallized region, described vapor-liquid separation section is blank pipe section, and top is provided with demister, the mozzle for the liquid to be concentrated that circulates is provided with in the middle of the cylindrical shell of described crystallized region, this mozzle is near the bottom of crystallized region and the port of export is provided with distributor that liquid to be concentrated is flowed out from port of export side, the bottom of described crystallized region is for leaving standstill district, and mozzle outside is flotation area, and the top of flotation area is also provided with liquid outlet, form circulation by circulating pump and pipeline communication between described liquid outlet and inlet, and described heat exchanger is located at this circulating line, the top of described vapor-liquid separation section is also provided with indirect steam outlet and is connected with the entrance of evaporation concentrator by pipeline, thus provides thermal source to evaporation concentrator.The liquid level of the liquid in crystallizing tower flushes with inlet substantially, liquid to be crystallized enters tower body inside from inlet tangential direction, isolate the gas of flash distillation, flash gas is sent as indirect steam can recycle as low grade heat source from the outlet at top, this process at utmost can reduce hydraulic shock and enter gas-liquid separation section, adopts tangential direction can reduce the effect of impacting and improving vapor-liquid separation simultaneously.Liquid after separation enters crystallized region with comparatively low velocity by mozzle, and under distributor effect near the port of export, liquid is flowed out from side surrounding, finally enter flotation area, larger crystalline particle is settled down to standing district and extraction under gravity, and less crystallization and solution are to flotation area ionized motion, finally squeeze into the further concentrate of heater through circulating pump together with fresh feed liquid.And so forth, thus realize continuous crystallisation.
This technique is linked up with dual evaporation crystallization one-level evaporation, and dual evaporation crystallization Steam Heating, the secondary vapour of one-level evaporation dual evaporation is as thermal source.One-level evaporation falling liquid film or climbing film evaporator, the dual evaporation crystallizer evaporimeter with larger crystallization expansion chamber of.The comparatively megacryst formed in evaporation process is because of the first sedimentation of gravitate, thin brilliant and solution is up concentrates further, thus formed mend continuous extraction after comparatively megacryst settles down after remove moisture content.
Claims (3)
1. the complete continuous crystallisation production process equipment of methenamine, it is characterized in that: comprise the evaporation concentrator, vapour liquid separator, steaming liquid feeder and the crystallizing evaporator that are connected successively by pipeline, also comprise vacuum extractor and heat exchanger, the gaseous phase outlet of described vapour liquid separator is connected with vacuum extractor, wherein:
Described crystallizing evaporator comprises tower body, it is the inlet of tangential direction that described tower body is provided with tower body, the upper and lower of inlet is respectively vapor-liquid separation section and crystallized region, described vapor-liquid separation section is blank pipe section, and top is provided with demister, the mozzle for the liquid to be concentrated that circulates is provided with in the middle of the cylindrical shell of described crystallized region, this mozzle is near the bottom of crystallized region and the port of export is provided with distributor that liquid to be concentrated is flowed out from port of export side, the bottom of described crystallized region is for leaving standstill district, and mozzle outside is flotation area, and the top of flotation area is also provided with liquid outlet, form circulation by circulating pump and pipeline communication between described liquid outlet and inlet, and described heat exchanger is located at this circulating line, the top of described vapor-liquid separation section is also provided with indirect steam outlet and is connected with the entrance of evaporation concentrator by pipeline, thus provides thermal source to evaporation concentrator.
2. the complete continuous crystallisation production process equipment of methenamine according to claim 1, is characterized in that: be also provided with condenser between the gaseous phase outlet of described vapour liquid separator and vacuum extractor.
3. the complete continuous crystallisation production process equipment of methenamine according to claim 1, is characterized in that: described evaporation concentrator is climbing-film evaporation inspissator or falling film evaporation inspissator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520004704.6U CN204428875U (en) | 2015-01-06 | 2015-01-06 | The complete continuous crystallisation production process equipment of a kind of methenamine |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520004704.6U CN204428875U (en) | 2015-01-06 | 2015-01-06 | The complete continuous crystallisation production process equipment of a kind of methenamine |
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| CN204428875U true CN204428875U (en) | 2015-07-01 |
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| CN201520004704.6U Expired - Fee Related CN204428875U (en) | 2015-01-06 | 2015-01-06 | The complete continuous crystallisation production process equipment of a kind of methenamine |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104524806A (en) * | 2015-01-06 | 2015-04-22 | 江苏凯茂石化科技有限公司 | Urotropin complete continuous crystallization production technology and equipment |
| CN108245921A (en) * | 2018-03-20 | 2018-07-06 | 河北鑫淘源环保科技有限公司 | The evaporation and crystallization system and process of one kind 5,5- Dimethyl Hydan mother liquors |
-
2015
- 2015-01-06 CN CN201520004704.6U patent/CN204428875U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104524806A (en) * | 2015-01-06 | 2015-04-22 | 江苏凯茂石化科技有限公司 | Urotropin complete continuous crystallization production technology and equipment |
| CN104524806B (en) * | 2015-01-06 | 2016-08-24 | 江苏凯茂石化科技有限公司 | A kind of hexamethylenamine complete continuous crystallisation production technology and equipments |
| CN108245921A (en) * | 2018-03-20 | 2018-07-06 | 河北鑫淘源环保科技有限公司 | The evaporation and crystallization system and process of one kind 5,5- Dimethyl Hydan mother liquors |
| CN108245921B (en) * | 2018-03-20 | 2024-03-12 | 河北鑫淘沅医药科技有限公司 | Evaporation crystallization system and process method of 5, 5-dimethyl hydantoin mother liquor |
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Legal Events
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| 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: 20150701 Termination date: 20190106 |