CN214299941U - Concentrated heat pump rectification equipment of propargyl alcohol and butynediol aqueous solution system - Google Patents
Concentrated heat pump rectification equipment of propargyl alcohol and butynediol aqueous solution system Download PDFInfo
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Abstract
The utility model relates to a concentrated heat pump rectifying device of a propiolic alcohol and butynediol aqueous solution system, which comprises a rectifying tower, a preheater, a material reboiler, a heating medium reboiler, a condenser, a reflux tank, a compressor, a reflux pump and a tower bottom pump; the feed inlet of rectifying column is connected with the pre-heater, the liquid phase mouth at the bottom of the tower of rectifying column is connected with the heat medium reboiler, the gaseous phase of heat medium reboiler evaporation returns rectifying column bottom gas phase space, the liquid phase mouth at the bottom of the tower of rectifying column is connected with the pump at the bottom of the tower simultaneously, pump outlet connection at the bottom of the tower is to material reboiler cold junction import and outward pipeline, material reboiler cold junction exit linkage to rectifying column bottom gas phase space, rectifying column top gas phase mouth is connected with the compressor, compressor exit linkage to material reboiler hot junction import simultaneously, material reboiler hot junction exit linkage to reflux drum, reflux drum gas phase export is connected with the condenser, reflux drum liquid phase mouth is connected with the reflux pump, reflux drum export is connected to rectifying column top reflux mouth and outward pipeline simultaneously.
Description
Technical Field
The utility model relates to a concentrated heat pump rectification equipment of propiolic alcohol, butynediol aqueous solution system is applied to the concentration of propiolic alcohol, butynediol aqueous solution.
Background
Formaldehyde and acetylene are used as raw materials, water is used as a solvent, and under the action of a catalyst, certain temperature and pressure are reached to react to generate propiolic alcohol and butynediol. By controlling the reaction conditions, the ratio of the reaction selectivity between propargyl alcohol and butynediol can be controlled to be 4 to 0.25. The non-condensable gas dissolved in the reaction product is removed by decompression, the solid catalyst is removed by filtration, the remaining main component is about 90 percent of water, and the other components are the mixed product of propiolic alcohol and butynediol.
The conventional separation flow comprises the following steps: firstly separating out the concentrated butynediol water solution, then separating out the concentrated propynediol water solution, and recycling the separated waste water. The process of concentrating butynediol and propargyl alcohol consumes a large amount of heat due to the large enthalpy of water.
On the basis of the conventional separation process, the multi-effect evaporation and the multi-effect rectification process are combined, so that the energy consumption can be obviously reduced, but the energy consumption is still the main energy consumption point in the whole process.
The following studies have proposed new process schemes:
CN102728090A, Wake-Yong et al, proposes a fractionating apparatus and method for separating propargyl alcohol, which is applied in the field of chemical separation, and comprises a double-wall tower, a rectifying tower stripping section, a rectifying tower rectifying section, a rectifying tower condenser, a vacuum evaporator, a rectifying tower tail cooler, a reflux tank, a heater, a vacuum evaporator cooler, etc. The double-wall tower is composed of a stripping section, the top of the double-wall tower is provided with an alkali liquor feed port, the rectifying tower is composed of a rectifying tower stripping section and a rectifying tower rectifying section, and a mixture feed port and a demister are arranged between the rectifying tower stripping section and the rectifying tower rectifying section. The double-walled tower is coupled with the rectifying tower, the double-walled tower and the rectifying tower are respectively connected with a heater, the rectifying tower is connected with a rectifying tower condenser, the rectifying tower condenser is connected with a rectifying tower tail cooler and a reflux tank, and the reflux tank is connected with the top of the rectifying tower through a first pipeline and is connected with a propiolic alcohol extraction pipeline. The utility model discloses a cancellation concentration process realizes concentrating and propiolic alcohol concentration integration, simplifies the separation process of propiolic alcohol and butynediol, improves production efficiency, adopts multiple-effect energy-saving techniques such as thermal coupling and heat supply network, and product quality can improve. The utility model discloses a well material of separating is propiolic alcohol, butynediol aqueous solution together, though cancelled concentrated process, has realized concentration and propiolic alcohol concentration integration, has used the flow of double-layered wall tower, but this flow is lengthy complicated, and the automatic operation degree of difficulty is great, and does not solve the high problem of aqueous system separation energy consumption.
In CN104387236A, Wujia et al propose a method for the triple-production continuous production of propiolic alcohol, 1, 4-butynediol and urotropine, and belong to the technical field of chemical industry. The utility model discloses use formalin (10% -37% wt) and acetylene to synthesize propiolic alcohol as the raw materials, coproduction 1, 4-butynediol and urotropine, reaction temperature is 80-120 ℃, and pressure is 1.0-2.5Mpa, can obtain propiolic alcohol, butynediol aqueous solution and urotropine aqueous solution that the purity is more than 99.5%, and the conversion rate of whole technology formaldehyde can reach 100%, has the advantage of safety ring protects. The process for separating the reaction product is not deeply described in the patent, the separation process is more conventional, but the propargyl alcohol is further concentrated in a rectification mode after the butynediol is concentrated in an evaporation mode, and no energy-saving technical innovation is provided.
Disclosure of Invention
The utility model aims at providing a heat pump rectification technology and equipment, which are applied to the concentration of propargyl alcohol and butynediol aqueous solution. The utility model provides a very big energy consumption when technology and equipment fully consider the separation of aqueous system utilizes heat pump technology to be used for the material heating at the bottom of the tower behind the gas compression at the bottom of the tower, and comprehensive energy consumption only is 5-8% of traditional separation technology, only is 10-13% of double-wall tower technology, and the running cost is showing and is reducing, and can guarantee complete automation mechanized operation.
The technical scheme of the utility model as follows:
a concentrated heat pump rectification device of a propargyl alcohol and butynediol aqueous solution system comprises a rectification tower, a preheater, a material reboiler, a heating medium reboiler, a condenser, a reflux tank, a compressor, a reflux pump and a tower bottom pump; the feed inlet of rectifying column is connected with the pre-heater, the liquid phase mouth at the bottom of the tower of rectifying column is connected with the heat medium reboiler, the gaseous phase of heat medium reboiler evaporation returns rectifying column bottom gas phase space, the liquid phase mouth at the bottom of the tower of rectifying column is connected with the pump at the bottom of the tower simultaneously, pump outlet connection at the bottom of the tower is to material reboiler cold junction import and outward pipeline, material reboiler cold junction exit linkage to rectifying column bottom gas phase space, rectifying column top gas phase mouth is connected with the compressor, compressor exit linkage to material reboiler hot junction import simultaneously, material reboiler hot junction exit linkage to reflux drum, reflux drum gas phase export is connected with the condenser, reflux drum liquid phase mouth is connected with the reflux pump, reflux drum export is connected to rectifying column top reflux mouth and outward pipeline simultaneously.
The rectifying tower consists of a rectifying section and a stripping section, and a filler or a tower plate is arranged in the tower.
The material reboiler has small heat exchange temperature difference and adopts a falling film mode.
The compressor adopts a centrifugal type, a Roots type or a screw type and continuously operates.
The utility model discloses a concentrated heat pump rectification technology of propiolic alcohol, butynediol aqueous solution system, the raw materials that comes from the reaction unit is behind desorption gaseous phase and solid phase, and propiolic alcohol, water, the misce bene material of butynediol get into the rectifying column through the pre-heater, sets up two reboilers at the bottom of the tower, a material reboiler for utilizing bottom of the tower pump auxiliary cycle, a heat medium reboiler for supplementing the heat, gaseous phase after the reboiler vaporization gets into the compressor from the top of the tower. After pressurization and temperature rise, the liquid phase material enters a material reboiler to exchange heat with the material in the tower kettle, the liquid phase material is condensed into a liquid phase and then enters a reflux tank, the tail gas of the reflux tank is discharged to a tail gas system after the material is recovered by a condenser, and the liquid phase material in the reflux tank is partially extracted as a propiolic alcohol solution product after being pressurized by a reflux pump, is discharged after exchanging heat with the feed material, and is partially conveyed to the top of the tower to be refluxed; the butynediol solution at the bottom of the tower is extracted after a pump at the bottom of the tower.
The feeding flow rate of the mixed material is 2-40 t/h, wherein the water content is 70-95%, the propiolic alcohol content is 1-15%, the feeding temperature is 20-60 ℃, and the feeding pressure is 0-1.0 Mpag.
The operating pressure of the rectifying tower is-0.09 Mpag to 0.4Mpag, the temperature of the top of the rectifying tower is 30 ℃ to 160 ℃, and the temperature of the bottom of the rectifying tower is 40 ℃ to 170 ℃.
After the mixed material is concentrated, the concentration of butynediol extracted from the bottom of the tower is 10-80%.
The heat medium reboiler adopts steam or heat conducting oil as a heat source, and the condenser adopts circulating water or 7-degree water as a cold source.
The utility model is applied to the equipment for the concentration and heat pump rectification of the water solution of propiolic alcohol and butynediol, the feed inlet of the rectification tower is connected with the preheater, and the heat exchange between the feed and the material extracted from the top of the tower can be realized; the tower bottom liquid phase port of the rectifying tower is connected with a heating medium reboiler, so that the continuous vaporization of the tower bottom liquid phase through the heating medium reboiler can be realized, and the vaporized gas phase returns to the tower bottom gas phase space of the rectifying tower; a tower bottom liquid phase port of the rectifying tower is simultaneously connected with a tower bottom pump, a tower bottom pump outlet is connected to a cold end inlet of a material reboiler and an outward delivery pipeline, so that the tower bottom liquid phase can be continuously conveyed to the cold end of the material reboiler through the tower bottom pump for heat exchange, and the cold end outlet of the material reboiler is connected to a tower bottom gas phase space of the rectifying tower; the gas phase port at the top of the rectifying tower is connected with a compressor, and the outlet of the compressor is connected to the inlet of the hot end of the material reboiler, so that the gas phase at the top of the rectifying tower is pressurized by the compressor and then is conveyed to the hot end of the material reboiler for heat exchange, and the outlet of the hot end of the material reboiler is connected to a reflux tank; the gas phase outlet of the reflux tank is connected with the condenser, so that the gas phase in the reflux tank can be condensed into a liquid phase by the condenser and then flows back to the reflux tank; the liquid phase port of the reflux tank is connected with a reflux pump, and the outlet of the reflux pump is connected to the reflux port at the top of the rectifying tower and an external conveying pipeline, so that the pump reflux and pump extraction of condensed materials can be realized.
Adopt the utility model discloses a propiolic alcohol, the concentrated heat pump rectification technology and the equipment of butynediol aqueous solution system, reboiler and compressor constitute heat transfer system, the top of the tower gaseous phase is after the compressor pressurization, get into reboiler hot junction material side, after the heat transfer with cold junction material side, the condensation is the liquid phase, get into reflux drum part flash distillation, flash distillation gas is tail gas of discharging behind the condenser, the condensate flows back after the pump pressurization, through control tail gas governing valve control reflux drum pressure, thereby control compressor exit pressure, make heat transfer system form the enough heat transfer difference in temperature, in order to maintain steady operation. The complete separation of the propiolic alcohol and the butynediol can be completed, and the material loss is less; the energy consumption is low and is only 5-8% of that of the conventional process; less equipment and investment.
Drawings
FIG. 1 is a schematic diagram of a concentrated heat pump distillation device of a propynol and butynediol aqueous solution system.
Detailed Description
Device connections are shown in fig. 1: the device is formed by connecting a rectifying tower (1), a preheater (2), a material reboiler (3), a heating medium reboiler (4), a condenser (5), a reflux tank (6), a compressor (7), a reflux pump (8) and a tower bottom pump (9). The feed inlet of the rectifying tower (1) is connected with the preheater (2), so that heat exchange between feed and materials extracted from the top of the tower can be realized; the tower bottom liquid phase port of the rectifying tower (1) is connected with the heating medium reboiler (4), so that the continuous vaporization of the tower bottom liquid phase through the heating medium reboiler (4) can be realized, and the vaporized gas phase returns to the tower bottom gas phase space of the rectifying tower (1); a tower bottom liquid phase port of the rectifying tower (1) is simultaneously connected with a tower bottom pump (9), an outlet of the tower bottom pump (9) is connected to a cold end inlet and an outward delivery pipeline of the material reboiler (3), so that the tower bottom liquid phase can be continuously conveyed to the cold end of the material reboiler (3) through the tower bottom pump (9) for heat exchange, and the cold end outlet of the material reboiler (3) is connected to a tower bottom gas phase space of the rectifying tower (1); a gas phase port at the top of the rectifying tower (1) is connected with a compressor (7), an outlet of the compressor (7) is connected to a hot end inlet of the material reboiler (3), so that the gas phase at the top of the rectifying tower can be pressurized by the compressor (7) and then conveyed to the hot end of the material reboiler (3) for heat exchange, and a hot end outlet of the material reboiler (3) is connected to a reflux tank (6); the gas phase outlet of the reflux tank (6) is connected with the condenser (5), so that the gas phase in the reflux tank can be condensed into a liquid phase by the condenser (5) and then flows back into the reflux tank (6); the liquid phase port of the reflux tank (6) is connected with a reflux pump (8), and the outlet of the reflux pump (8) is connected to the reflux port at the top of the rectifying tower (1) and an external conveying pipeline, so that the pump reflux and pump extraction of condensed materials can be realized.
The feeding flow rate of the reaction product is 2-40 t/h, wherein the water content is 70-95%, the propiolic alcohol content is 1-15%, the feeding temperature is 20-60 ℃, and the feeding pressure is 0-1.0 Mpag.
The rectifying tower (1) is composed of a rectifying section and a stripping section, a filler or a tower plate is arranged in the tower, the operating pressure is-0.09-0.4 Mpag, the temperature at the top of the tower is 30-160 ℃, the temperature at the bottom of the tower is 40-170 ℃, under the operating condition, steam or heat conducting oil is adopted as a heat source in a heat medium reboiler (4), and circulating water or 7-degree water is adopted as a cold source in a condenser (5).
After concentration, the concentration of butynediol extracted from the tower bottom is 10-80%.
Specific application examples are as follows:
example 1:
the feeding flow is 2t/h, the selectivity proportion of the reaction of the propiolic alcohol and the butynediol is 0.99, the water content is 89.3 percent, the feeding temperature is 35 ℃, and the pressure of the fed material reaches 0.2Mpag after the pressure of the fed material is increased by a pump.
2t/h of feed is heated to 58 ℃ after passing through a preheater (2), and is sent to the middle part of a rectifying tower (1), and the upper part in the rectifying tower is filled with 4 m-mesh corrugated structured packing to be used as a rectifying section; the lower part is provided with 4 layers of sieve plate tower trays as stripping sections. The diameter of the rectifying tower (1) is 900 mm. The operating pressure was controlled at-0.03 Mpag, the overhead temperature was 82.8 ℃ and the bottoms temperature was 92.3 ℃.
The gas phase at the top of the tower enters a compressor (7), the compressor (7) adopts a centrifugal mode, the compression ratio is 2.3, a fixed-frequency continuous operation mode is adopted, the outlet pressure of the compressor is 0.061Mpag, and the temperature is 121 ℃.
The material reboiler (3) adopts a vertical tube array falling film evaporation mode, materials on a circulating cold side pass a tube pass, high-temperature and high-pressure gas after compression passes a shell pass, the shell pass gas is condensed into liquid after continuous heat exchange, the temperature is about 98 ℃, and the liquid automatically flows into the reflux tank (6).
The pressure of the reflux tank (6) is maintained at 0.04Mpag, a small amount of high-temperature liquid is vaporized after entering the reflux tank and enters the condenser (5) for condensation, tail gas is not discharged during normal operation, and the reflux amount is stabilized at 0.2 t/h.
The heating medium reboiler (3) adopts 0.2Mpag saturated steam for heating, and the average adding amount of the steam is 0.22t/h in normal operation.
The extraction amount at the top of the tower is 1788.62kg/h, and the product is cooled to 45 ℃ after heat exchange by a preheater (2), wherein the butynediol content is 0.01%; the bottom yield was 211.38kg/h, with a butynediol content of 61.5%.
Example 2:
the feed flow is 4t/h, the selectivity ratio of the reaction of the propiolic alcohol and the butynediol is 0.67, the water content is 90.46 percent, the feed temperature is 35 ℃, and the pressure of the feed reaches 0.2Mpag after the feed is pumped and pressurized.
4t/h of feed is heated to 58 ℃ after passing through a preheater (2), and is sent to the middle part of a rectifying tower (1), and the upper part in the rectifying tower is filled with 4m of net corrugated structured packing to be used as a rectifying section; the lower part is provided with 4 layers of sieve plate tower trays as stripping sections. The diameter of the rectifying tower (1) is 1200 mm. The operating pressure was controlled at-0.03 Mpag, the overhead temperature was 82.8 ℃ and the bottoms temperature was 92.3 ℃.
The gas phase at the top of the tower enters a compressor (7), the compressor (7) adopts a centrifugal mode, the compression ratio is 2.3, a fixed-frequency continuous operation mode is adopted, the outlet pressure of the compressor is 0.061Mpag, and the temperature is 121 ℃.
The material reboiler (3) adopts a vertical tube array falling film evaporation mode, materials on a circulating cold side pass a tube pass, high-temperature and high-pressure gas after compression passes a shell pass, the shell pass gas is condensed into liquid after continuous heat exchange, the temperature is about 98 ℃, and the liquid automatically flows into the reflux tank (6).
The pressure of the reflux tank (6) is maintained at 0.04Mpag, a small amount of high-temperature liquid is vaporized after entering the reflux tank and enters the condenser (5) for condensation, tail gas is not discharged during normal operation, and the reflux amount is stabilized at 0.4 t/h.
The heating medium reboiler (3) adopts 0.2Mpag saturated steam for heating, and the average adding amount of the steam is 0.43t/h in normal operation.
The extraction amount at the top of the tower is 3498.06kg/h, and the propynol is cooled to 45 ℃ after heat exchange by the preheater (2), wherein the content of the propynol is 3.3%; the bottom yield was 501.94kg/h, with a butynediol content of 53%.
Example 3:
the feed flow is 6t/h, the selectivity ratio of the reaction of the propiolic alcohol and the butynediol is 1.54, the water content is 70 percent, the feed temperature is 20 ℃, and the pressure of the feed reaches 1.0Mpag after the feed is pumped and pressurized.
Feeding at a rate of 6t/h, heating to 48 ℃ after passing through a preheater (2), feeding into the middle part of a rectifying tower (1), and filling 5m of loose pall ring packing at the upper part in the rectifying tower to serve as a rectifying section; the lower part is filled with 1m of loose pall ring packing to be used as a stripping section. The diameter of the rectifying tower (1) is 1400 mm. The operating pressure was controlled at 0.4Mpag, the head temperature was 160 ℃ and the bottom temperature was 170 ℃.
The gas phase at the top of the tower enters a compressor (7), the compressor (7) adopts a Roots form, the compression ratio is 1.8, a fixed-frequency continuous operation mode is adopted, the outlet pressure of the compressor is 0.8Mpag, and the temperature is 205 ℃.
The material reboiler (3) adopts a vertical tube array falling film evaporation mode, materials on a circulating cold side pass a tube pass, high-temperature and high-pressure gas after compression passes a shell pass, the shell pass gas is condensed into liquid after continuous heat exchange, the temperature is about 176 ℃, and the liquid automatically flows into the reflux tank (6).
The pressure of the reflux tank (6) is maintained at 0.3Mpag, a small amount of high-temperature liquid is vaporized after entering the reflux tank and enters the condenser (5) for condensation, tail gas is not discharged during normal operation, and the reflux amount is stabilized at 0.6 t/h.
The heating medium reboiler (4) adopts 1.0Mpag saturated steam for heating, and the average adding amount of the steam is 0.61t/h in normal operation.
The overhead output is 4875kg/h, and the liquid is cooled to 35 ℃ after heat exchange by a preheater (2), wherein the butynediol content is 0%; the bottom yield is 1125kg/h, wherein the butynediol content is 80%.
Example 4:
the feed flow was 13.5t/h, the selectivity ratio of the reaction of propargyl alcohol with butynediol was 0.5, the water content therein was 90.59%, the feed temperature was 50 ℃ and the pressure of the feed after pumping was 0.1 Mpag.
13.5t/h of feed is heated to 63 ℃ after passing through a preheater (2) and is sent to the middle part of a rectifying tower (1), and 20 layers of float valve trays are arranged at the upper part in the rectifying tower to be used as a rectifying section; the lower part is provided with 4 layers of sieve plate tower trays as stripping sections. The diameter of the rectifying tower (1) is 2400 mm. The operating pressure was controlled at-0.06 Mpag, the overhead temperature was 68.7 ℃ and the bottoms temperature was 78.3 ℃.
The gas phase at the top of the tower enters a compressor (7), the compressor (7) adopts a screw rod form, the compression ratio is 2.5, a variable-frequency continuous operation mode is adopted, the outlet pressure of the compressor is 0Mpag, and the temperature is 121 ℃.
The material reboiler (3) adopts a horizontal tube array falling film evaporation mode, the material on the circulating cold side leaves a shell pass, the high-temperature and high-pressure gas after compression leaves a tube pass, the gas on the tube pass is condensed into liquid after continuous heat exchange, the temperature is about 81 ℃, and the liquid automatically flows into the reflux tank (6).
The pressure of the reflux tank (6) is maintained at-0.02 Mpag, a small amount of high-temperature liquid is vaporized after entering the reflux tank and enters the condenser (5) for condensation, tail gas is not discharged during normal operation, and the reflux amount is stabilized at 1.3 t/h.
The heating medium reboiler (3) adopts 0.1Mpag saturated steam for heating, and the average steam adding amount is 1.33t/h in normal operation.
The extraction amount at the top of the tower is 11954.69kg/h, and the propynol is cooled to 55 ℃ after heat exchange by a preheater (2), wherein the content of the propynol is 2.6%; the bottom yield is 1545.32kg/h, with a butynediol content of 62%.
Example 5:
the feed flow is 40t/h, the selectivity ratio of the reaction of the propiolic alcohol and the butynediol is 0.38, the water content is 95 percent, the feed temperature is 60 ℃, and the pressure of the feed reaches 0Mpag after the feed is pumped and pressurized.
Feeding at 40t/h, heating to 73 ℃ after passing through a preheater (2), feeding into the middle part of a rectifying tower (1), and installing 20 layers of float valve trays at the upper part in the rectifying tower as a rectifying section; the lower part is provided with 4 layers of sieve plate tower trays as stripping sections. The diameter of the rectifying tower (1) is 4100 mm. The operating pressure was controlled at-0.09 Mpag, the overhead temperature was 30 ℃ and the bottom temperature was 40 ℃.
The gas phase at the top of the tower enters a compressor (7), the compressor (7) adopts a screw rod form, the compression ratio is 3, a variable frequency continuous operation mode is adopted, the outlet pressure of the compressor is-0.07 Mpag, and the temperature is 64 ℃.
The material reboiler (3) adopts a horizontal type tube array falling film evaporation mode, the material on the circulating cold side passes through the shell pass, the high-temperature and high-pressure gas after compression passes through the tube pass, the gas on the tube pass is condensed into liquid after continuous heat exchange, the temperature is about 67 ℃, and the liquid automatically flows into the reflux tank (6).
The pressure of the reflux tank (6) is maintained at-0.08 Mpag, a small amount of high-temperature liquid is vaporized after entering the reflux tank and enters the condenser (5) for condensation, tail gas is not discharged during normal operation, and the reflux amount is stabilized at 4 t/h.
The heating medium reboiler (3) adopts 0.1Mpag saturated steam for heating, and the average adding amount of the steam is 3.9t/h in normal operation.
The extraction amount at the top of the tower is 24000kg/h, and the product is cooled to 65 ℃ after heat exchange by a preheater (2), wherein the butynediol content is 0.01 percent; the bottom yield is 16000kg/h, wherein the butynediol content is 10 percent.
The present invention provides a heat pump distillation apparatus for butynediol concentration, which has been described by way of example, it is obvious for the skilled person to change or properly change and combine the apparatus described herein without departing from the contents, spirit and scope of the present invention to realize the technology of the present invention. It is expressly intended that all such similar substitutes and modifications apparent to those skilled in the art are deemed to be within the spirit, scope and content of the invention.
Claims (4)
1. A concentrated heat pump rectification device of a propynol and butynediol aqueous solution system is characterized in that: comprises a rectifying tower, a preheater, a material reboiler, a heating medium reboiler, a condenser, a reflux tank, a compressor, a reflux pump and a tower bottom pump; the feed inlet of rectifying column is connected with the pre-heater, the liquid phase mouth at the bottom of the tower of rectifying column is connected with the heat medium reboiler, the gaseous phase of heat medium reboiler evaporation returns rectifying column bottom gas phase space, the liquid phase mouth at the bottom of the tower of rectifying column is connected with the pump at the bottom of the tower simultaneously, pump outlet connection at the bottom of the tower is to material reboiler cold junction import and outward pipeline, material reboiler cold junction exit linkage to rectifying column bottom gas phase space, rectifying column top gas phase mouth is connected with the compressor, compressor exit linkage to material reboiler hot junction import simultaneously, material reboiler hot junction exit linkage to reflux drum, reflux drum gas phase export is connected with the condenser, reflux drum liquid phase mouth is connected with the reflux pump, reflux drum export is connected to rectifying column top reflux mouth and outward pipeline simultaneously.
2. The apparatus of claim 1, wherein: the rectifying tower consists of rectifying section and stripping section, and inside the tower, stuffing or tower plate is installed.
3. The apparatus of claim 1, wherein: the material reboiler has small heat exchange temperature difference and adopts a falling film mode.
4. The apparatus of claim 1, wherein: the compressor is of a centrifugal type, a roots type or a screw type.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114146439A (en) * | 2021-12-10 | 2022-03-08 | 北京道思克矿山装备技术有限公司 | Double-falling-film evaporation rectifying tower system and rectifying method thereof |
| CN115286162A (en) * | 2022-08-22 | 2022-11-04 | 吴嘉 | Device and method for treating ammonia nitrogen wastewater easy to scale and recycling ammonia |
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2020
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114146439A (en) * | 2021-12-10 | 2022-03-08 | 北京道思克矿山装备技术有限公司 | Double-falling-film evaporation rectifying tower system and rectifying method thereof |
| CN115286162A (en) * | 2022-08-22 | 2022-11-04 | 吴嘉 | Device and method for treating ammonia nitrogen wastewater easy to scale and recycling ammonia |
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