CN211595043U - Sulfuric acid system production liquid SO3Practical safety device - Google Patents
Sulfuric acid system production liquid SO3Practical safety device Download PDFInfo
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- CN211595043U CN211595043U CN201921869549.9U CN201921869549U CN211595043U CN 211595043 U CN211595043 U CN 211595043U CN 201921869549 U CN201921869549 U CN 201921869549U CN 211595043 U CN211595043 U CN 211595043U
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Abstract
The utility model discloses a sulphuric acid system production liquid SO3The safe and practical device comprises a fuming sulfuric acid circulating tank, a spiral plate type cooler and SO3Absorption tower, spiral plate type preheater and SO3Evaporator, shower-type condenser and liquid SO3A finished product storage tank, wherein: the fuming sulfuric acid circulating tank is respectively connected with the spiral plate cooler and the spiral plate preheater through a circulating pump and a pipeline; the spiral plate cooler passes through the SO through the pipeline3The absorption tower is connected with a fuming sulfuric acid circulating tank; the spiral plate type preheater passes through the pipeRoad junction SO3The bottom of the evaporator; and SO3The top of the upper end socket of the evaporator is connected with a spray-falling type condenser through a pipeline, and the spray-falling type condenser is connected with the liquid SO through a pipeline3A finished product storage tank and an acid return pipe of the fuming sulfuric acid absorption tower. The utility model provides a sulphuric acid system production liquid SO3The safe and practical device realizes the cyclic utilization of system heat, greatly reduces the production cost, and effectively solves the problems of safety, high efficiency and insufficient evaporation heat of the condenser.
Description
Technical Field
The utility model relates to a sulphuric acid production technical field especially relates to a sulphuric acid system production liquid SO3The practical safety device of (1).
Background
Liquid SO3Mainly used as a sulfonating agent, which is an intermediate product for preparing high-concentration fuming sulfuric acid and chlorosulfonic acid. At present, a large amount of domestic sulfur trioxide is used for preparing sodium alkyl benzene sulfonate, sulfonated lubricating oil for preparing white oil, biological pharmacy and the like. The high-concentration oleum is mainly used as a sulfonating agent, a smoke bomb and the like for sulfonation reaction. SO (SO)3The liquid has strong volatility, is easy to freeze, cannot meet water and belongs to dangerous chemicals, so the production safety is very important.
The existing production method mainly has three problems: firstly, the heat required by evaporation is often insufficient, the evaporation and the yield are influenced, some steam heating with the pressure of about 0.8MPa has to be adopted, and the energy consumption also brings risks; secondly, the condensation capacity is small and restricted, the cooling water is large or is cooled, so that the solidification and blockage are easy to occur, and the treatment is very troublesome; cooling water is low or heat yield is affected, SO3The gas is influenced by the condensation speed, the amount of the gas entering the condenser is limited, the gas cannot directly pass through the condenser and must be condensed; the biggest problem is condensationThe efficient cooling and the safety of the device are considered, no good method exists, namely a high water cooling effect is required, water is feared to leak into the device to cause feared accidents, air cooling is usually adopted for safety, the efficiency is extremely low, and the effect is particularly obvious in summer. If water cooling is adopted in the risk, not only a danger source exists, but also a side leakage alarm needs to be installed and maintained, and the core is lifted.
SUMMERY OF THE UTILITY MODEL
The utility model provides a solution to the above problems in the prior art and provides a liquid SO produced by a sulfuric acid system3The practical safety device of (1).
In order to achieve the above purpose, the utility model adopts the following technical scheme:
the utility model provides a sulphuric acid system production liquid SO3The practical safety device comprises a fuming sulfuric acid circulating tank, a spiral plate type cooler and fuming sulfuric acid SO3Absorption tower, spiral plate type preheater and SO3Evaporimeter and double row slight slope drench and fall formula condenser, wherein:
the fuming sulfuric acid circulating tank is respectively connected with the spiral plate cooler and the spiral plate preheater through a circulating pump through pipelines so as to respectively convey the acid liquid in the fuming sulfuric acid circulating tank to the spiral plate cooler for cooling treatment and to the spiral plate preheater for preheating treatment;
the spiral plate cooler passes through the fuming sulfuric acid SO through a pipeline3The absorption tower is connected with the fuming sulfuric acid circulating tank to absorb the cooled acid liquid into high-concentration fuming sulfuric acid in a contact manner with the flue gas, and the high-concentration fuming sulfuric acid passes through the fuming sulfuric acid SO3The acid return pipe of the absorption tower reflows to the fuming sulfuric acid circulating tank to complete the acid liquor concentration circulation and continuous circulation;
the spiral plate type preheater is connected with the SO through a pipeline3The bottom of the evaporator is used for feeding the preheated acid liquid into the SO3The evaporator carries out evaporation treatment, and the evaporated acid liquid flows out from the side part of the upper end enclosure; the SO3The side part of the upper end socket of the evaporator is connected with the spiral plate type preheater through a pipeline SO as to evaporate SO3Conveying the high-temperature acid liquor with reduced concentration after gas to the spiral plate type pre-heaterHeat exchange is carried out between the acid liquor in the heater and the acid liquor before evaporation; and
the SO3The top of the upper end socket of the evaporator is connected with the double-row micro-slope sprinkling-falling type condenser through a pipeline SO as to evaporate SO3Conveying the gas into the double-row micro-slope sprinkling-falling type condenser for condensation treatment, and condensing SO3The liquid flows into the liquid SO through the pipeline3A finished product storage tank; uncondensed SO3Gas enters the fuming sulfuric acid SO through a pipeline3And after the acid return pipe of the absorption tower is contacted and absorbed with high-concentration oleum in the acid return pipe, the oleum flows into the oleum circulating tank together for recycling.
Further, via the SO3Introducing the smoke gas cooled by the evaporator into the fuming sulfuric acid SO3The absorption tower is absorbed by fuming acid liquor, and the absorbed flue gas is absorbed from the fuming sulfuric acid SO3The top of the absorption tower is discharged back to the sulfuric acid production system.
Further, the spiral plate type preheater is two and is arranged in series.
Further, a small amount of SO volatilized from the high-concentration oleum in the oleum circulating tank3Gas is conveyed to SO through a pipeline3The gas absorber is used for absorbing treatment and is utilized by a sulfuric acid production system.
Further, from said SO3Evaporating and separating SO from side part of upper end socket of evaporator3And introducing the high-temperature low-concentration acid liquid after gas into the two spiral plate type preheaters connected in series, exchanging heat with the high-concentration low-temperature acid liquid in the two spiral plate type preheaters connected in series, discharging the acid liquid out of the spiral plate type preheaters after cooling, connecting the acid liquid back into the fuming sulfuric acid circulating tank through a pipeline, and completing the concentration reduction circulating process of concentrated acid liquid-heat exchange-evaporation-heat exchange and continuously circulating.
Further, uncondensed SO3Gas enters the fuming sulfuric acid SO through a pipeline3And the acid return pipe of the absorption tower is contacted and absorbed with high-concentration fuming sulfuric acid in the acid return pipe, and then flows into the fuming sulfuric acid circulating groove together for recycling.
Further preferably, it isCondensed SO3Gas in oleum SO3The return acid pipe of the absorption tower is converged between 80 and 350mm below the elbow when entering the fuming sulfuric acid circulating tank, and is absorbed and dissolved by the high-concentration fuming sulfuric acid in the return acid pipe and then is sent to the fuming sulfuric acid circulating tank.
Further, the double-row micro-slope sprinkling-falling type condenser comprises sprinkling-falling water pipes, micro-slope pipelines and a water receiving tank which are sequentially arranged from top to bottom, wherein the micro-slope pipelines are formed by connecting two rows of straight pipes in series to form a steel single pipeline which has the gradient of 1-3 degrees and continuously descends back and forth, and the distance between the upper straight pipe and the lower straight pipe which are adjacent to each other on the micro-slope pipelines is 51-57 mm.
Preferably, the number of the sprinkling and precipitation pipes is two, a plurality of water outlet holes are uniformly distributed in the bottom of each sprinkling and precipitation pipe along the length direction of the sprinkling and precipitation pipe, the holes of the water outlet holes face downwards, the aperture is 5-15mm, and the distance between the water outlet holes and the top of the micro-slope pipeline is 20-40 mm.
Further preferably, the two sides of the micro-slope pipeline are respectively provided with an anti-splash water-retaining inclined fin plate, and the length direction of the anti-splash water-retaining inclined fin plate is consistent with the horizontal direction of the slope direction of the micro-slope pipeline.
Further preferably, the water in the water receiving tank flows into a water cooling tower of the sulfuric acid process system for circulation or is used as make-up water of the water cooling tower.
Further preferably, the SO3Evaporator, double-row micro-slope sprinkling type condenser and liquid SO3The horizontal heights of the finished product storage tank and the fuming sulfuric acid circulating tank are gradually reduced, and the SO is added3The liquid can flow automatically between the process flow devices without accumulating liquid.
The above technical scheme is adopted in the utility model, compared with the prior art, following technological effect has:
1) 2 spiral plate preheaters which are connected in series and have enough area and flow velocity are adopted to realize the full utilization of self heat and temperature rise, and the heated SO enters the shell3The evaporator is heated by the hot process flue gas of the sulfuric acid system and then heated, so that the boiling point of the nicotinic acid can be sufficiently reached for rapid evaporation, the heat of the hot process flue gas of the sulfuric acid system is fully utilized, the most convenient and energy-saving effect is realized, no extra energy consumption is realized, and the cost is lowest;
2) the adopted double-row micro-slope sprinkling type condenser is externally sprinkled with water and is not pressurized, and SO in the condenser is3Pressure, in case of leakage, SO3The water can not enter the condenser forever due to outward leakage, thus thoroughly avoiding the phenomenon that once the traditional shell and tube heat exchanger is leaked, the water enters SO3Violent reaction, heating and explosion accidents occur in the container storage tank and the pipeline, and the problems that the micro-seams of the traditional condenser tube array are immersed and corroded and are not easy to detect are solved; safe and can find the leakage point in time, once the double-row micro-slope descending condenser is exposed, because of SO3No matter the liquid or the gas is contacted with the air, white obvious smoke is generated immediately, and the treatment can be found quickly;
3) the double-row micro-slope sprinkling-falling type condenser can be completely cooled by water, namely, the water sprinkling-falling type condenser is extremely strong in effect compared with air cooling, and high in heat transfer coefficient, and the sprinkling-falling type condenser adopts the structure that the intermittent water-retaining fin plates are arranged on two sides, so that the water-moistening condition of the double-row pipes can be seen, the ventilation is not influenced, and water can be completely recovered while water splashing is prevented.
4) The double-row micro-slope sprinkling-falling type condenser with double rows of single-pipe runners and micro slopes which are closely arranged solves the problem of large volume of the condenser, the sprinkling is small, double rows of overflowing media can be the same in size through the single pipe, and the defects that the parallel connection of different flow rates is different and the condensation control is troublesome are avoided.
5) The outlet pipe of the double-row micro-slope sprinkling type condenser is connected with liquid SO3Finished product storage tank, fuming sulfuric acid SO also connected with nicotinic acid circulation tank3Acid return pipe of absorption tower, uncondensed SO3The gas can be flushed into the acid return pipe to be dissolved with the nicotinic acid in the pipe and reused, SO that the SO in the double-row micro-slope sprinkling-falling type condenser3The design accelerates the flow rate of the liquid, can completely liquefy only by increasing the water quantity, and has high capacity, high elasticity and high cooling efficiency;
6) in addition, even part of SO in the double-row micro-slope spraying-falling type condenser3Gas not being liquefied at all time, SO3The gas can be flushed into the acid return pipe for dissolution; the prior art only depends on the reduction of the condensation volume to the pushing speed and can not increase the water quantity toThe invention has the advantages of no freezing, small operation elasticity and low efficiency, is safe and reliable, breaks through the limitations and is a sulfuric acid system for producing liquid SO3The practical safety device of (1).
Drawings
FIG. 1 shows a process for producing liquid SO in a sulfuric acid system according to the present invention3The structure of the safety device is shown schematically;
FIG. 2 shows a process for producing liquid SO in a sulfuric acid system according to the present invention3The structural schematic diagram of the double-row micro-slope sprinkling-falling type condenser in the practical safety device;
wherein the reference symbols are:
1-fuming sulfuric acid circulation tank; 2-a circulating pump; 3-a spiral plate cooler; 4-oleum SO3An absorption tower; 5-spiral plate type preheater; 6-SO3An evaporator; 7-double row micro-slope sprinkling type condenser, 71-sprinkling type water-dropping pipe, 72-micro-slope pipeline, 73-water receiving tank and 74-splash-proof water-retaining inclined fin plate; 8-liquid SO3And (5) a finished product storage tank.
Detailed Description
The present invention will be described in detail and specifically with reference to specific embodiments so as to provide a better understanding of the present invention, but the following embodiments do not limit the scope of the present invention.
Example 1
Referring to FIG. 1, the present embodiment provides a sulfuric acid system for producing liquid SO3The practical safety device mainly comprises a fuming sulfuric acid circulating tank 1, a spiral plate type cooler 3 and fuming sulfuric acid SO3Absorption tower 4, spiral plate type preheater 5 and SO3An evaporator 6 and a double-row micro-slope sprinkling type condenser 7.
In this embodiment, the fuming sulfuric acid circulation tank 1 is connected with the spiral plate cooler 3 and the spiral plate preheater 5 through the circulating pump 2 via the pipeline, so as to respectively convey the acid liquid in the fuming sulfuric acid circulation tank to the spiral plate cooler 3 for cooling and to the spiral plate preheater 5 for preheating; the spiral plate cooler 3 passes through the fuming sulfuric acid SO through a pipeline3The absorption tower 4 is connected with the fuming sulfuric acid circulating tank 1 to cool the acidThe liquid is contacted with the flue gas to be absorbed into high-concentration oleum, and the high-concentration oleum passes through oleum SO3And an acid return pipe of the absorption tower 4 reflows to the fuming sulfuric acid circulating tank 1 to complete the acid liquor concentration circulation and continuous circulation.
In this embodiment, the spiral plate preheater 5 is connected to the SO through a pipe3The bottom of the evaporator 6 is used for feeding preheated concentrated fuming sulfuric acid liquid into the SO3The evaporator 6 carries out evaporation treatment, and the evaporated acid liquid flows out from the side part of the upper end enclosure; the SO3The side part of the upper end socket of the evaporator 6 is connected with two spiral plate type preheaters 5 which are connected in series through a pipeline SO as to evaporate SO from concentrated fuming sulfuric acid solution3The hot acid liquor with reduced concentration after gas is conveyed into the two spiral plate type preheaters 5 connected in series to exchange heat with the cold concentrated fuming sulfuric acid liquor before evaporation. The high-temperature hot acid liquid is cooled and then is discharged out of the spiral plate type preheater 5 and enters the fuming sulfuric acid circulating tank 1 through an acid return pipe. The SO3The top of the upper end socket of the evaporator 6 is connected with the double-row micro-slope sprinkling type condenser 7 through a pipeline SO as to evaporate SO3Conveying the gas into the double-row micro-slope sprinkling-falling type condenser 7 for condensation treatment, and condensing SO3The liquid flows into the liquid SO through the pipeline3A finished product storage tank 8; uncondensed SO3Gas enters the fuming sulfuric acid SO through a pipeline3And after the acid return pipe of the absorption tower is contacted and absorbed with high-concentration oleum in the acid return pipe, the oleum flows into the oleum circulating tank 1 together for recycling.
As a technical solution of this embodiment, as shown in FIG. 1, the SO3The flue gas cooled by the evaporator 6 is introduced into the fuming sulfuric acid SO3The absorption tower 4 is absorbed by fuming acid liquor, and the absorbed flue gas is absorbed from the fuming sulfuric acid SO3The top of the absorption tower 4 is discharged and enters a sulfuric acid production system for utilization. Furthermore, the SO3SO evaporated by the evaporator 63The acid foam is removed by the cyclone demister on the top of the cyclone demister, the acid foam is recycled, and the ratio of the pipe diameter of an outlet of the cyclone demister to the cylinder diameter of the cyclone demister is 2/7-1/3.
As a technical solution of the present embodiment, as shown in FIG. 1The spiral plate type preheater 5 has enough efficiency and area, and the spiral plate type preheater 5 is provided with two spiral plate type preheaters which are arranged in series. The two spiral plate type preheaters 5 which are arranged in series have better heat exchange effect, the self heat is fully utilized to increase the temperature, and the SO enters after the temperature is increased3The evaporator 6 is heated by the hot flue gas of the sulfuric acid system process and then heated, so that the boiling point of fuming sulfuric acid can be sufficiently reached for rapid evaporation, the heat of the hot flue gas of the sulfuric acid system process is fully utilized, the most convenient and energy-saving effect is achieved, and the cost is the lowest.
As a technical solution of this embodiment, a small amount of SO volatilized from high-concentration oleum in the oleum circulation tank 13Gas is conveyed to SO through a pipeline3The gas absorber is used for absorbing treatment and is utilized by a sulfuric acid production system.
As a technical solution of this embodiment, the SO3SO is evaporated and separated from the side part of the upper end socket of the evaporator 63And introducing the high-temperature low-concentration acid liquid after gas into the two spiral plate type preheaters 5 connected in series, exchanging heat with the acid liquid in the two spiral plate type preheaters 5 connected in series, and cooling the high-temperature acid liquid out of the spiral plate type preheaters 5 and then connecting the cooled high-temperature acid liquid back to the fuming sulfuric acid circulating tank 1 through a pipeline.
As a technical solution of this embodiment, the uncondensed SO3Gas enters the fuming sulfuric acid SO through a pipeline3In the acid return pipe of the absorption tower 4, the acid return pipe is contacted with high-concentration oleum in the acid return pipe for absorption, and then the acid return pipe and the high-concentration oleum flow into the oleum circulation tank 1 for cyclic utilization. Uncondensed SO3The gas is converged between 80 mm and 350mm below the elbow when the acid return pipe enters the fuming sulfuric acid circulating tank 1, and is absorbed and dissolved by high-concentration fuming sulfuric acid in the acid return pipe and then is sent to the fuming sulfuric acid circulating tank 1.
As a preferred technical solution of this embodiment, as shown in fig. 2, the double-row micro-slope shower-falling type condenser includes a shower-falling water pipe 71, a micro-slope pipeline 72 and a water receiving tank 73, which are sequentially arranged from top to bottom, wherein the micro-slope pipeline 72 is formed by two rows of steel single pipelines which are serially connected to form a continuous back-and-forth falling pipeline with a slope of 1 to 3 °, and the area corresponds to the capacity. Preferably, the first and second electrodes are formed of a metal,the gradient of the steel single pipeline is 1.5-2.5 degrees, and the upper end inlet of the micro-slope pipeline 72 is connected with the SO3The top end and the lower end of the evaporator 6 are respectively connected with the liquid SO3Finished product storage tank 8 and oleum SO3On the acid return pipe of the absorption tower 4.
As a preferable technical scheme of the embodiment, as shown in FIG. 2, the distance between the upper and lower adjacent straight pipes on the micro-slope pipeline 72 is 51 mm. Preferably, the distance between the adjacent upper and lower pipelines is 51mm, SO3The schematic diagram of the evaporator shown in the figure 2 has larger spacing, is used for illustrating the structure, has small actual spacing, and achieves the purposes of tight and compact structure and less splashing water when the shower water falls onto each pipe; the single-pipeline design can make the double-row medium size of overflowing the same, avoid parallelly connected each pipe flow volume to differ, the trouble disadvantage of condensation control.
As another preferable technical solution of this embodiment, the drenching precipitation liquid recovered in the water receiving tank 73 automatically flows into the cooling tower circulation tank or is used as water supplement of the cooling tower circulation tank.
Adopts a double-row micro-slope sprinkling type condenser, water is sprinkled outside, no pressure is generated, and SO in the condenser is generated3Pressure, in case of leakage, SO3The water can not enter the condenser forever due to outward leakage, thus thoroughly avoiding the phenomenon that once the traditional shell and tube heat exchanger is leaked, the water enters SO3The violent reaction, heating and explosion accidents occur in the container storage tank and the pipeline, the problem that the micro-slits of the traditional condenser tube nest are immersed and corroded and are not easy to be noticed is avoided, the leakage point can be safely and timely found, once the double-row micro-slope sprinkling type condenser is exposed, the SO is used for preventing the leakage of the condensed water3Treatment was soon discovered, whether liquid or gas was in contact with air, producing a visibly white smoke.
In addition, the both sides of double-row slight slope drenches and falls inclined finned plate 74 of splashproof water retaining of formula condenser 7, and this oblique finned plate 74 of splashproof water retaining is horizontal installation, and this oblique finned plate 74 of splashproof water retaining opens towards outside inclining to one side, just the length direction of the oblique finned plate 74 of splashproof water retaining with the horizontal direction of the slope direction of slight slope pipeline 72 is unanimous. The water wetting condition of the micro-slope pipeline 72 can be seen through the interval between the upper splash-proof water retaining inclined fin plates 74 and the lower splash-proof water retaining inclined fin plates 74, ventilation is not affected, water can be completely recycled while water splashing is prevented, the double-row micro-slope sprinkling-falling condenser can be completely cooled by water, namely, water sprinkling-falling cooling is greatly stronger than air cooling effect, heat transfer coefficient is high, the sprinkling condition can be directly observed, and inspection is convenient.
As a technical solution of this embodiment, there are two of the sprinkling and precipitation pipes 71, the bottom of each of the sprinkling and precipitation pipes 71 is provided with a plurality of uniformly distributed water outlet holes along the length direction thereof, the holes of the water outlet holes are downward, the aperture is 5-15mm, and the distance between the water outlet holes and the top of the micro-slope pipe 72 is 20-40 mm; preferably, the aperture of the water outlet hole is 8-12mm, the distance between the water outlet hole and the top of the micro-slope pipeline 72 is 25-32mm, the size of water can be seen, all the holes can uniformly discharge water simultaneously, the water pouring and descending pipe 71 is provided with a water regulating valve for controlling the size, and partial water discharge can be controlled according to needs.
In this example, the SO is described in the Process flow Equipment3Evaporator 6, double-row micro-slope sprinkling type condenser 7 and liquid SO3The finished product storage tank 8 and the fuming sulfuric acid circulating tank 1 are gradually reduced in level, and the SO is3Gas and/or SO3The liquid realizes self-flow among all process flow devices.
Production of liquid SO of this example3The practical safety device fully and efficiently realizes the utilization and cyclic utilization of system heat, and the anhydrous dry hot flue gas of the sulfuric acid system is utilized to safely heat SO3The evaporator and the circulating fuming sulfuric acid liquid carry out self sufficient heat exchange through improving the heat exchange capacity of the preheater, and particularly, a single-tube double-row sprinkling and descending type condenser is created for condensation, so that the production cost is greatly reduced, the reliability and the safety are improved, and the problems of insufficient evaporation heat and the safety and the high efficiency of the condenser are effectively solved.
The sulfuric acid system of this example produces liquid SO3The practical safety device comprises the following specific process flows:
in the process 1, hot flue gas generated by the sulfuric acid system process enters SO3In the evaporator 6, the SO3 is supplied with evaporation heat from the evaporator 6 via the SO3After heat exchange and temperature reduction of the evaporator 6, fuming sulfuric acid SO is introduced3In the absorption tower 4;
the first path of fuming acid liquid cooled by the spiral plate cooler 3 is conveyed to fuming sulfuric acid SO3An absorption tower 4 for absorbing the introduced fuming sulfuric acid SO3SO contained in flue gas in the absorption tower 43Returning the obtained high-concentration oleum to the oleum circulating tank 1 by the gas to supplement SO of the oleum circulating tank 1 with oleum3Content (c);
the second path of fuming acid liquor preheated and heated by the spiral plate type preheater 5 is conveyed to SO3The evaporator 6 is used for evaporating and separating out pure SO3The gas and the high-temperature fuming sulfuric acid liquid with reduced concentration after evaporation flow out through the spiral plate type preheater 5 and return to the fuming sulfuric acid circulating tank 1;
The above detailed description of the embodiments of the present invention is only for exemplary purposes, and the present invention is not limited to the above described embodiments. Any equivalent modifications and substitutions to those skilled in the art are also within the scope of the present invention. Accordingly, variations and modifications in equivalents may be made without departing from the spirit and scope of the invention, which is intended to be covered by the following claims.
Claims (10)
1. Sulfuric acid system production liquid SO3In practical useThe safety device is characterized by comprising a fuming sulfuric acid circulating tank (1), a spiral plate cooler (3) and fuming sulfuric acid SO3An absorption tower (4), a spiral plate type preheater (5) and SO3Evaporator (6) and double row micro-slope drench and drop condenser (7), wherein:
the fuming sulfuric acid circulating tank (1) is respectively connected with the spiral plate cooler (3) and the spiral plate preheater (5) through a circulating pump (2) through pipelines so as to respectively convey acid liquid in the fuming sulfuric acid circulating tank to the spiral plate cooler (3) for cooling treatment and to the spiral plate preheater (5) for preheating treatment;
the spiral plate cooler (3) passes through the fuming sulfuric acid SO through a pipeline3The absorption tower (4) is connected with the fuming sulfuric acid circulating tank (1) to absorb the cooled acid liquid into high-concentration fuming sulfuric acid through contact with the flue gas, and the high-concentration fuming sulfuric acid passes through fuming sulfuric acid SO3An acid return pipe of the absorption tower (4) reflows to the fuming sulfuric acid circulating tank (1) to complete the acid liquor concentration circulation and continuous circulation;
the spiral plate type preheater (5) is connected with the SO through a pipeline3The bottom of the evaporator (6) is used for feeding the preheated acid liquid into the SO3The evaporator (6) carries out evaporation treatment, and the evaporated acid liquid flows from the side part of the upper end enclosure; the SO3The side part of the upper end socket of the evaporator (6) is connected with the spiral plate type preheater (5) through a pipeline SO as to evaporate SO3Conveying the acid liquor with the concentration reduced after gas into the spiral plate type preheater (5) to exchange heat with the acid liquor before evaporation; and
the SO3The top of the upper end socket of the evaporator (6) is connected with the double-row micro-slope sprinkling type condenser (7) through a pipeline SO as to evaporate SO3The gas is conveyed into the double-row micro-slope sprinkling-falling type condenser (7) for condensation treatment, and the condensed SO3The liquid flows into the liquid SO through the pipeline3A finished product storage tank (8); uncondensed SO3Gas enters the fuming sulfuric acid SO through a pipeline3And after the acid return pipe of the absorption tower (4) is contacted and absorbed with high-concentration oleum in the acid return pipe, the oleum flows into the oleum circulating tank (1) together for recycling.
2. Sulfuric acid system production liquid SO according to claim 13The utility safety device is characterized in that the spiral plate type preheaters (5) are two and are arranged in series.
3. Sulfuric acid system production liquid SO according to claim 13The practical safety device of (A), characterized in that the SO3SO is evaporated and separated from the side part of the upper end socket of the evaporator (6)3And introducing the high-temperature low-concentration acid liquid after gas into the two spiral plate type preheaters (5) connected in series, exchanging heat with the acid liquid in the two spiral plate type preheaters (5) connected in series, and cooling the high-temperature acid liquid out of the spiral plate type preheaters (5) and connecting the cooled high-temperature acid liquid back to the fuming sulfuric acid circulating tank (1) through a pipeline.
4. Sulfuric acid system production liquid SO according to claim 13Is characterized in that the uncondensed SO is3Gas enters the fuming sulfuric acid SO through a pipeline3And the high-concentration oleum in the acid return pipe of the absorption tower (4) is contacted and absorbed with the oleum in the acid return pipe, and then the oleum flows into the oleum circulating tank (1) together for recycling.
5. Sulfuric acid system production liquid SO according to claim 43Is characterized in that the uncondensed SO is3Gas in oleum SO3The acid return pipe of the absorption tower (4) is converged between 80 mm and 350mm below the elbow when entering the fuming sulfuric acid circulating tank (1), and is absorbed and dissolved by high-concentration fuming sulfuric acid in the acid return pipe and then is sent to the fuming sulfuric acid circulating tank (1).
6. Sulfuric acid system production liquid SO according to claim 13The practical safety device is characterized in that the double-row micro-slope sprinkling-falling type condenser (7) comprises a sprinkling-falling water pipe (71), a micro-slope pipeline (72) and a water receiving tank (73) which are sequentially arranged from top to bottom, wherein the micro-slope pipeline (72) is formed by serially connecting two rows of straight pipes into a continuous pipeline with a slope of 1-3 degreesThe steel single pipeline which descends back and forth is formed, and the distance between the upper straight pipe and the lower straight pipe which are adjacent to each other on the micro-slope pipeline (72) is 51-57 mm.
7. Sulfuric acid system production liquid SO according to claim 63The practical safety device is characterized in that the number of the sprinkling and precipitation pipes (71) is two, each sprinkling and precipitation pipe (71) is provided with a plurality of uniformly distributed water outlet holes along the length direction, the holes of the water outlet holes are downward, the hole diameter is 5-15mm, and the distance between the water outlet holes and the top of the micro-slope pipeline (72) is 20-40 mm.
8. Sulfuric acid system production liquid SO according to claim 63The utility model discloses a practical safety device, its characterized in that, the both sides of slight slope pipeline (72) are provided with splashproof manger plate oblique finned plate (74) respectively, the length direction of splashproof manger plate oblique finned plate (74) with the horizontal direction of the slope direction of slight slope pipeline (72) is unanimous.
9. Sulfuric acid system production liquid SO according to claim 63The practical safety device is characterized in that the water in the water receiving tank (73) flows into a water cooling tower of a sulfuric acid process system for circulation or is used as make-up water of the water cooling tower.
10. Sulfuric acid system production liquid SO according to claim 13The practical safety device of (A), characterized in that the SO3An evaporator (6), a double-row micro-slope sprinkling type condenser (7) and liquid SO3The horizontal heights of the finished product storage tank (8) and the fuming sulfuric acid circulating tank (1) are gradually reduced, and the SO3The liquid can automatically flow between the process flow devices without accumulating liquid.
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| CN201921869549.9U CN211595043U (en) | 2019-11-01 | 2019-11-01 | Sulfuric acid system production liquid SO3Practical safety device |
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| CN201921869549.9U CN211595043U (en) | 2019-11-01 | 2019-11-01 | Sulfuric acid system production liquid SO3Practical safety device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113546437A (en) * | 2021-08-10 | 2021-10-26 | 联仕(昆山)化学材料有限公司 | Electronic-grade sulfuric acid production system and production process |
| CN113800479A (en) * | 2021-10-29 | 2021-12-17 | 山东京博众诚清洁能源有限公司 | Process for preparing electronic-grade sulfuric acid by cyclic absorption method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113546437A (en) * | 2021-08-10 | 2021-10-26 | 联仕(昆山)化学材料有限公司 | Electronic-grade sulfuric acid production system and production process |
| CN113800479A (en) * | 2021-10-29 | 2021-12-17 | 山东京博众诚清洁能源有限公司 | Process for preparing electronic-grade sulfuric acid by cyclic absorption method |
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