CN220633012U - Efficient and energy-saving sulfuric acid evaporation concentration system - Google Patents
Efficient and energy-saving sulfuric acid evaporation concentration system Download PDFInfo
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- CN220633012U CN220633012U CN202322216253.XU CN202322216253U CN220633012U CN 220633012 U CN220633012 U CN 220633012U CN 202322216253 U CN202322216253 U CN 202322216253U CN 220633012 U CN220633012 U CN 220633012U
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- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title claims abstract description 140
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- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
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- 238000010793 Steam injection (oil industry) Methods 0.000 description 2
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- WBIQQQGBSDOWNP-UHFFFAOYSA-N 2-dodecylbenzenesulfonic acid Chemical compound CCCCCCCCCCCCC1=CC=CC=C1S(O)(=O)=O WBIQQQGBSDOWNP-UHFFFAOYSA-N 0.000 description 1
- QTWJRLJHJPIABL-UHFFFAOYSA-N 2-methylphenol;3-methylphenol;4-methylphenol Chemical compound CC1=CC=C(O)C=C1.CC1=CC=CC(O)=C1.CC1=CC=CC=C1O QTWJRLJHJPIABL-UHFFFAOYSA-N 0.000 description 1
- QNPCBWPVEZKWQU-UHFFFAOYSA-N 2-methylprop-1-ene;sulfuric acid Chemical compound CC(C)=C.OS(O)(=O)=O QNPCBWPVEZKWQU-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
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- NHTMVDHEPJAVLT-UHFFFAOYSA-N Isooctane Chemical compound CC(C)CC(C)(C)C NHTMVDHEPJAVLT-UHFFFAOYSA-N 0.000 description 1
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- 235000011941 Tilia x europaea Nutrition 0.000 description 1
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- JVSWJIKNEAIKJW-UHFFFAOYSA-N dimethyl-hexane Natural products CCCCCC(C)C JVSWJIKNEAIKJW-UHFFFAOYSA-N 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
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- 239000000986 disperse dye Substances 0.000 description 1
- 229940060296 dodecylbenzenesulfonic acid Drugs 0.000 description 1
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- DXXKDZKHPQGAPM-UHFFFAOYSA-N formic acid;sulfuric acid Chemical compound OC=O.OC=O.OS(O)(=O)=O DXXKDZKHPQGAPM-UHFFFAOYSA-N 0.000 description 1
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- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 1
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- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 1
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- LNOPIUAQISRISI-UHFFFAOYSA-N n'-hydroxy-2-propan-2-ylsulfonylethanimidamide Chemical compound CC(C)S(=O)(=O)CC(N)=NO LNOPIUAQISRISI-UHFFFAOYSA-N 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
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- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 229930195735 unsaturated hydrocarbon Natural products 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 239000011701 zinc Substances 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses a high-efficiency energy-saving sulfuric acid evaporation concentration system, which comprises a falling film heat exchange absorption tower, a concentration evaporator, a raw material acid storage tank, a concentrated acid storage tank, a tower top gas phase condenser, a vacuum system and a wastewater tank; the falling film heat exchange absorption tower consists of an upper tower and a lower tower, wherein the upper tower and the lower tower are separated by a tube plate I, and the side surface of the lower end of the upper tower is provided with a raw material acid inlet; a plurality of falling film heat exchange absorption pipes are longitudinally arranged in the upper tower, a falling film device is arranged at the top of each falling film heat exchange absorption pipe, and the lower ends of the falling film heat exchange absorption pipes penetrate through the first tube plate and then extend into the lower tower and are connected with the second tube plate arranged at the bottom of the lower tower; the bottom end of the lower tower is a sulfuric acid outlet, and a concentrated acid inlet and a concentrated acid outlet are arranged on the side face of the lower tower between the tube plate I and the tube plate II. The utility model has the characteristics of high efficiency, energy conservation, compact system, low equipment investment cost, high concentration of sulfuric acid and high purity of discharged waste gas.
Description
Technical Field
The utility model relates to a sulfuric acid evaporation concentration system, in particular to a high-efficiency and energy-saving sulfuric acid evaporation concentration system.
Background
The yield and amount of sulfuric acid represent a state of the art in the chemical industry, and other industries, in addition to the fertilizer industry, have the production of spent sulfuric acid in sulfuric acid applications. Such as: the non-ferrous metal industry, the waste sulfuric acid with the concentration of about 10% is produced in the process of producing acid and purifying the copper, lead and zinc smelting flue gas; the waste sulfuric acid in the titanium dioxide industry is derived from filtrate after titanium liquid hydrolysis and washing liquid during primary washing, and 1 ton of titanium dioxide is produced to produce 8t of waste sulfuric acid with the concentration of about 20%; in the production process of the steel and metal pickling industry, the surface is generally cleaned by dilute sulfuric acid with the concentration of about 18 percent, waste sulfuric acid (the content of which is 6 percent) containing ferrous sulfate and ferric sulfate is generated, and according to the general pickling process, about 100kg of waste sulfuric acid is generated per ton of cleaned steel; in petroleum refining, concentrated sulfuric acid is used for removing impurities (sulfides and unsaturated hydrocarbons) in gasoline and lubricating oil, 1.08 kg of sulfuric acid is needed for refining each ton of crude oil, isooctane is produced by catalyzing isobutene sulfuric acid, and 80-90 kg of waste sulfuric acid with the content of 85-90% is needed for producing each ton of products; the chlorine drying section in the chlor-alkali industry utilizes the dehydration property of 98% concentrated sulfuric acid to dry and dehydrate wet chlorine generated by an electrolytic tank, and the 98% sulfuric acid absorbs water and then is reduced to about 75%, and 13-21 kg of waste sulfuric acid is generated per ton of chlor-alkali; waste sulfuric acid is generated in the production processes of dye and intermediate disperse dye, reactive dye, amphoteric dye, neutral dye and cationic dye; the organic chemical industry such as citric acid, sulfamic acid, oxalic acid, sulfuric acid diformic acid, synthesized cresol, dodecyl benzene sulfonic acid and other products, and sulfonation, nitration, alkylation, esterification and other chemical reaction units, to produce 20-60% waste sulfuric acid.
The traditional waste acid treatment mainly comprises the steps of discharging or adopting lime for neutralization, so that the waste of resources is greatly caused, and the environment is polluted due to improper treatment. Along with the increase of the national supervision force of dangerous chemicals and the enhancement of the management force of dangerous wastes, many enterprises select to send waste sulfuric acid outwards for treatment, but the potential safety hazard of the sending treatment is very large, and if a treatment link is problematic, the normal production of the enterprises is likely to be affected. Therefore, the concentration, purification and regeneration of the waste sulfuric acid are the best direction for fundamentally solving the problem of the waste sulfuric acid.
The existing waste sulfuric acid concentration process mainly comprises evaporation concentration, an evaporation concentration system mainly comprises an evaporator, a preheating part, a steam treatment part and other devices, the waste sulfuric acid is sent into the evaporator to be heated and evaporated after being preheated, most of water is discharged, so that the dilute waste sulfuric acid is changed into concentrated sulfuric acid, and secondary steam generated by evaporation is exhausted after being treated by the steam treatment device. However, concentrated sulfuric acid after evaporation and concentration and generated secondary steam all contain a large amount of heat, and direct discharge of the concentrated system can cause great energy waste, and as the heating temperature of raw material acid is generally higher than 160 ℃, the secondary steam contains acid mist besides water vapor, and the acid mist can cause sulfuric acid loss if not recycled, and the secondary steam containing the acid mist is troublesome in treatment. In order to absorb acid mist in the secondary steam and recover heat of the secondary steam and concentrated sulfuric acid, in the prior report, a part of systems are additionally provided with waste heat recovery and acid mist recovery systems, but the defects of huge systems and complex equipment exist; in addition, the single-effect evaporator is difficult to prepare concentrated sulfuric acid with concentration of more than 98%, and in order to improve the concentration of the concentrated sulfuric acid, the multiple-effect evaporator is adopted to perform evaporation concentration at present, which definitely further expands the system, so that the system is more complex and equipment investment is larger.
Disclosure of Invention
The utility model aims to provide an efficient and energy-saving sulfuric acid evaporation concentration system. The utility model has the characteristics of high efficiency, energy conservation, compact system, low equipment investment cost, high concentration of sulfuric acid and high purity of discharged waste gas.
The technical scheme of the utility model is as follows: an efficient and energy-saving sulfuric acid evaporation concentration system comprises a falling film heat exchange absorption tower, a concentration evaporator, a raw material acid storage tank, a concentrated acid storage tank, a tower top gas phase condenser, a vacuum system and a wastewater tank;
the falling film heat exchange absorption tower consists of an upper tower and a lower tower, the upper tower and the lower tower are separated by a tube plate, a raw material acid inlet is arranged on the side surface of the lower end of the upper tower, and the raw material acid inlet is connected with the raw material acid storage tank; the top of the upper tower is provided with a secondary steam outlet which is connected with the tower top gas-phase condenser; a plurality of falling film heat exchange absorption pipes are longitudinally arranged in the upper tower, a falling film device is arranged at the top of each falling film heat exchange absorption pipe, and the lower ends of the falling film heat exchange absorption pipes penetrate through the first tube plate and then extend into the lower tower and are connected with the second tube plate arranged at the bottom of the lower tower; the bottom end of the lower tower is a sulfuric acid outlet and is connected with an evaporator secondary steam outlet arranged on the concentrating evaporator, a concentrated acid inlet and a concentrated acid outlet are arranged on the side face of the lower tower between the first tube plate and the second tube plate, the concentrated acid outlet is connected with the concentrated acid storage tank, and the concentrated acid inlet is connected with an evaporator concentrated acid outlet arranged on the concentrating evaporator.
According to the scheme, the falling film heat exchange absorption tower is integrated and connected with the concentrating evaporator, the falling film heat exchange absorption tower is arranged as an upper tower and a lower tower, falling film heat exchange absorption pipes are arranged in the upper tower and the lower tower in a penetrating manner, a falling film device is arranged at the top end of the falling film heat exchange absorption pipe, high-temperature secondary steam directly enters the falling film heat exchange absorption pipe after coming out of the concentrating evaporator and contacts with a raw material acid liquid film in the falling film heat exchange absorption pipe, the low-temperature raw material acid is used for absorbing acid mist in the secondary steam while contact heat exchange is completed, the purity of waste gas is improved, and in an upper tower section, the secondary steam performs wall-separating heat exchange with the raw material acid outside the falling film heat exchange absorption pipe, so that the preheating in the secondary steam is further absorbed, the waste heat recovery rate is improved, and the energy consumption is saved; the high-temperature concentrated sulfuric acid discharged from the concentrating evaporator passes through the lower tower and then exchanges heat with the raw material acid in the falling film heat exchange absorption tube in the lower tower, so that the preheating in the concentrated sulfuric acid is further absorbed, and the energy consumption is saved; in addition, the falling film heat exchange absorption tower of the scheme completes the procedures of waste heat recovery, acid mist absorption and primary evaporation, so that the system is greatly simplified while the heat recovery rate is high, and the cost input of equipment is reduced.
In a preferred scheme, the efficient and energy-saving sulfuric acid evaporation concentration system is characterized in that the concentration evaporator is horizontal and comprises an evaporator shell, a steam inlet and a steam condensate outlet are respectively arranged at the outer sides of two ends of the evaporator shell, a tube plate III and a tube plate IV are respectively arranged at the inner sides of the evaporator shell, and a plurality of heat exchange tubes are arranged between the tube plate III and the tube plate IV; an evaporator shell between the tube plate III and the tube plate IV is provided with an evaporator secondary steam outlet and an evaporator concentrated acid outlet, wherein the evaporator secondary steam outlet is close to one end of the steam inlet, and the evaporator concentrated acid outlet is close to one end of the steam condensate outlet; a plurality of groups of clapboards are distributed in the evaporator shell between the evaporator secondary steam outlet and the evaporator concentrated acid outlet, the upper ends of the clapboards are fluid channels, the heights of all the clapboards are consistent, overflow plates are arranged between adjacent clapboards, the height of the upper end faces of the overflow plates is lower than that of the upper end faces of the clapboards, the upper ends of the overflow plates are fluid channels, and the heights of the upper ends of the overflow plates are gradually reduced along with the flowing direction of fluid.
According to the scheme, through the structure of the optimized concentration evaporator, multistage continuous evaporation concentration is realized in one concentration evaporator, the concentration of sulfuric acid is greatly improved, concentrated sulfuric acid with the concentration of more than 98% can be produced, meanwhile, the system is further simplified, and the cost input of equipment is reduced. The height of the overflow plate is set to be a certain gradient, so that the overflow plate can be gradually lowered, on one hand, backflow can be prevented, and on the other hand, the concentration of sulfuric acid concentrated in the later stage can be further ensured, so that the concentration of sulfuric acid reaches above the required concentration.
In a preferred scheme, the efficient and energy-saving sulfuric acid evaporation concentration system is characterized in that the concentration evaporator is further connected with an overflow tank, the bottom of the overflow tank is connected with the concentrated acid outlet of the evaporator through an inverted U-shaped overflow pipe, and the water discharge level of the inverted U-shaped overflow pipe is consistent with the height of the upper end face of the last overflow plate; the top of the overflow tank is connected with a pressure balance port arranged on the evaporator shell; the side of the overflow tank is connected with a concentrated acid inlet.
According to the scheme, the overflow tank and the inverted U-shaped overflow pipe are further arranged, so that the liquid level in the concentration evaporator is always at a fixed height, and the sulfuric acid concentration can be further guaranteed.
In a preferred scheme, the efficient and energy-saving sulfuric acid evaporation concentration system is characterized in that a first baffle plate is arranged in the upper tower. According to the scheme, the first baffle plate is arranged in the upper tower, so that the flow channel of the raw material acid can be prolonged, the heat exchange between the raw material acid and the secondary steam in the falling film heat exchange absorption tube is more sufficient, and the waste heat recovery rate is higher.
In a preferred scheme, the efficient and energy-saving sulfuric acid evaporation concentration system is characterized in that a baffle plate II is arranged in the lower tower. According to the scheme, the baffle plate II is arranged in the lower tower, so that the flow channel of high-temperature concentrated sulfuric acid can be prolonged, the heat exchange between the concentrated sulfuric acid and the raw material acid in the falling film heat exchange absorption tube is more sufficient, and the waste heat recovery rate is higher.
Preferably, the foregoing efficient and energy-saving sulfuric acid evaporation concentration system, the vacuum system is a vapor injection pump, the vapor injection pump is connected with the overhead vapor phase condenser, and an injection vapor inlet is provided on the vapor injection pump. The vacuum system of this scheme is the steam jet pump of preference, and evacuation ability is stronger, and the positive empty degree in falling film heat transfer absorption tower and the concentrated evaporimeter is lower, and evaporation efficiency is higher.
In a preferred scheme, the efficient and energy-saving sulfuric acid evaporation concentration system is characterized in that a steam condenser is connected to a steam spraying end of the vacuum system, and the steam condenser is connected with the wastewater tank after being connected with the tower top gas phase condenser in parallel. According to the scheme, the steam condenser is connected to the vacuum system, and the principle that the volume of the sprayed steam is suddenly reduced after condensation is utilized, so that the vacuumizing capacity is further improved.
The beneficial effects of the utility model are that
1. The utility model integrates and connects the falling film heat exchange absorption tower and the concentrating evaporator, and sets the falling film heat exchange absorption tower as an upper tower and a lower tower, and the falling film heat exchange absorption pipe is arranged in the upper tower and the lower tower in a penetrating way, and the falling film device is arranged at the top end of the falling film heat exchange absorption pipe, the high-temperature secondary steam directly enters the falling film heat exchange absorption pipe after coming out of the concentrating evaporator and contacts with the raw material acid liquid film in the falling film heat exchange absorption pipe, and the low-temperature raw material acid is utilized to absorb acid mist in the secondary steam while the contact heat exchange is completed, so that the purity of waste gas is improved, and in the upper tower section, the secondary steam can perform the wall-separating heat exchange with the raw material acid outside the falling film heat exchange absorption pipe, further absorbs the preheating in the secondary steam, improves the waste heat recovery rate and saves the energy consumption; the high-temperature concentrated sulfuric acid discharged from the concentrating evaporator passes through the lower tower and then exchanges heat with the raw material acid in the falling film heat exchange absorption tube in the lower tower, so that the preheating in the concentrated sulfuric acid is further absorbed, and the energy consumption is saved; in addition, the falling film heat exchange absorption tower of the utility model completes the procedures of waste heat recovery, acid mist absorption and primary evaporation, has high heat recovery rate, greatly simplifies the system and reduces the cost input of equipment.
2. The utility model realizes multistage continuous evaporation concentration in one concentration evaporator through the structure of the optimized concentration evaporator, greatly improves the concentration of sulfuric acid, can produce concentrated sulfuric acid with the concentration of more than 98 percent, and simultaneously further simplifies the system and reduces the cost input of equipment. The height of the overflow plate is set to be a certain gradient, the overflow plate is gradually lowered, on one hand, backflow can be prevented, on the other hand, the flow channel of sulfuric acid is prolonged, the heat exchange efficiency is improved, in addition, the maximum average temperature difference between acid liquid and a medium at the service side is ensured, and the concentration of produced sulfuric acid is higher.
3. According to the utility model, the overflow tank and the inverted U-shaped overflow pipe are further arranged, so that the liquid level in the concentration evaporator is always at a fixed height, and the sulfuric acid concentration can be further ensured.
4. According to the utility model, the first baffle plate is arranged in the upper tower, so that the flow passage of the raw material acid can be prolonged, the heat exchange between the raw material acid and the secondary steam in the falling film heat exchange absorption tube is more complete, and the waste heat recovery rate is higher. By arranging the baffle plate II in the lower tower, the flow passage of the high-temperature concentrated sulfuric acid can be prolonged, so that the heat exchange between the concentrated sulfuric acid and the raw material acid in the falling film heat exchange absorption tube is more sufficient, and the waste heat recovery rate is higher.
5. The vacuum system is preferably a steam jet pump, has stronger evacuation capability, lower positive air-tightness in the falling film heat exchange absorption tower and the concentration evaporator, higher evaporation efficiency, lower working temperature and more energy saving. The steam condenser is connected to the vacuum system, so that the vacuumizing capacity is further improved by utilizing the principle of sudden volume reduction after the sprayed steam is condensed, and the working temperature of the system is lower and the energy is saved.
Drawings
FIG. 1 is a schematic diagram of the system of the present utility model;
FIG. 2 is a schematic diagram of a falling film heat exchange absorber of the system of the present utility model;
FIG. 3 is a schematic diagram of the configuration of the concentrating evaporator of the system of the present utility model;
reference numerals illustrate: the device comprises a 1-falling film heat exchange absorption tower, a 101-upper tower, a 102-lower tower, a 103 tube plate I, a 104-raw material acid inlet, a 105-secondary steam outlet, a 106-falling film heat exchange absorption tube, a 107-falling film device, a 108-tube plate II, a 109-concentrated acid inlet, a 110-concentrated acid outlet, a 111-sulfuric acid outlet, a 112-baffle I, a 113-baffle II, a 2-concentrated evaporator, a 201-evaporator shell, a 202-steam inlet, a 203-steam condensate outlet, a 204-evaporator secondary steam outlet, a 205-evaporator concentrated acid outlet, a 206-tube plate III, a 207-tube plate IV, a 208-heat exchange tube, a 209-baffle, a 210-overflow plate, a 211-pressure balance port, a 3-raw material acid storage tank, a 4-concentrated acid storage tank, a 5-overhead gas phase condenser, a 6-vacuum system, a 7-waste water tank, an 8-overflow tank, a 9-steam condenser and a 10-jet steam inlet.
Detailed Description
The utility model is further illustrated by the following examples, which are not intended to be limiting.
Embodiments of the utility model
The "connections" described in this embodiment are all pipe connections.
An efficient energy-saving sulfuric acid evaporation concentration system, as shown in figures 1-3, comprises a falling film heat exchange absorption tower 1, a concentration evaporator 2, a raw material acid storage tank 3, a concentrated acid storage tank 4, an overhead gas phase condenser 5, a vacuum system 6 and a wastewater tank 7; the falling film heat exchange absorption tower 1 consists of an upper tower 101 and a lower tower 102, wherein the upper tower 101 and the lower tower 102 are separated by a first tube plate 103, a raw material acid inlet 104 is arranged on the side surface of the lower end of the upper tower 101, and the raw material acid inlet 104 is connected with the raw material acid storage tank 3; the top of the upper tower 101 is provided with a secondary steam outlet 105, and the secondary steam outlet 105 is connected with the tower top gas-phase condenser 5; a plurality of falling film heat exchange absorption pipes 106 are longitudinally arranged in the upper tower 101, a falling film device 107 is arranged at the top of each falling film heat exchange absorption pipe 106, and the lower ends of the falling film heat exchange absorption pipes 106 penetrate through the first tube plate 103 and then extend into the lower tower 102 and are connected with the second tube plate 108 arranged at the bottom of the lower tower 102; the bottom end of the lower tower 102 is a sulfuric acid outlet 111 and is connected with an evaporator secondary steam outlet 204 arranged on the concentrating evaporator 2, a concentrated acid inlet 109 and a concentrated acid outlet 110 are arranged on the side surface of the lower tower 102 between the first tube plate 103 and the second tube plate 108, the concentrated acid outlet 110 is connected with the concentrated acid storage tank 4, and the concentrated acid inlet 109 is connected with an evaporator concentrated acid outlet 205 arranged on the concentrating evaporator 2.
The working principle of the embodiment is as follows: when the raw dilute acid at the normal temperature of 25 ℃ is fed into a raw acid storage tank 3 for storage, the raw dilute acid is fed into a raw acid inlet 104 through a feed pump and a feed pipe and flows into a shell side of an upper tower 101, flows upwards, when the liquid level is higher than that of a falling film device 107, the raw dilute acid flows downwards along the inner wall of a falling film heat exchange absorption pipe 106 in a film forming manner, flows into a concentrating evaporator 2 below, after high-temperature heat exchange is carried out in the concentrating evaporator 2, most of water and a small part of sulfuric acid in the raw dilute acid are evaporated to form secondary steam, the secondary steam is discharged through an evaporator secondary steam outlet 204 and flows upwards and reversely, contact heat exchange is carried out between the secondary steam and the raw dilute acid in a countercurrent process, the raw dilute acid is preheated, meanwhile, the acid mist in the secondary steam is absorbed by the raw dilute acid, the cooled and the secondary steam after the acid mist is discharged through a secondary steam outlet 105, and enters a tower top gas phase condenser 5 for condensation under the action of a vacuum system 6, and the condensed waste water enters a waste water tank 7 for direct evacuation.
When the secondary steam enters the upper tower 101 section, the secondary steam not only contacts and exchanges heat with the sulfuric acid liquid film in the falling film heat exchange absorption tube 106, but also performs dividing wall type heat exchange with the raw material dilute acid outside the falling film heat exchange absorption tube 106, so that the preheating temperature of the raw material dilute acid is increased.
The temperature of the concentrated sulfuric acid discharged from the concentrated evaporator 2 is about 160 ℃, the concentrated sulfuric acid is introduced into the shell side of the lower tower 102 to exchange heat with the raw material dilute acid in the falling film heat exchange absorption tube 106 of the lower tower 102, the raw material dilute acid in the falling film heat exchange absorption tube 106 of the section is preliminarily heated to the boiling point under the common heating action of high-temperature secondary steam and the high-temperature concentrated sulfuric acid, part of water is evaporated in the section, flows upwards along with the secondary steam and is discharged, and the rest of raw material dilute acid enters the concentrated evaporator 2 below.
1-3, the concentrating evaporator 2 is horizontal and comprises an evaporator shell 201, wherein the outer sides of two ends of the evaporator shell 201 are respectively provided with a steam inlet 202 and a steam condensate outlet 203, the inner sides of the evaporator shell 201 are respectively provided with a tube plate III 206 and a tube plate IV 207, and a plurality of heat exchange tubes 208 are arranged between the tube plate III 206 and the tube plate IV 207; an evaporator secondary steam outlet 204 and an evaporator concentrated acid outlet 205 are arranged on the evaporator shell 201 between the tube plate III 206 and the tube plate IV 207, the evaporator secondary steam outlet 204 is close to one end of the steam inlet 202, and the evaporator concentrated acid outlet 205 is close to one end of the steam condensate outlet 203; a plurality of groups of partition plates 209 are distributed in the evaporator shell 201 between the evaporator secondary steam outlet 204 and the evaporator concentrated acid outlet 205, the upper ends of the partition plates 209 are fluid channels, the heights of all the partition plates 209 are consistent, overflow plates 210 are arranged between adjacent partition plates 209, the height of the upper end face of each overflow plate 210 is lower than that of the upper end face of each partition plate 209, the upper end of each overflow plate 210 is a fluid channel, and the height of the upper end of each overflow plate 210 is gradually reduced along with the flowing direction of fluid.
The working principle of the embodiment is the same as the previous embodiment, and the difference is that: after entering the concentration evaporator 2, the raw dilute acid flows by bypassing the lower end of the partition plate 209 and the upper end of the overflow plate 210 in sequence, the whole flow passage is S-shaped, and the overflow height of the next stage is always lower than that of the previous stage.
In a further embodiment, as shown in fig. 1-3, the concentrating evaporator 2 is further connected with an overflow tank 8, the bottom of the overflow tank 8 is connected with the concentrated acid outlet 205 of the evaporator through an inverted U-shaped overflow pipe 11, and the drainage position of the inverted U-shaped overflow pipe 11 is consistent with the height of the upper end face of the last overflow plate 210; the top of the overflow tank 8 is connected with a pressure balance port 211 arranged on the evaporator shell 201; the overflow tank 8 is connected to a concentrated acid inlet 109 on the side.
The working principle of the embodiment is the same as the previous embodiment, and the difference is that: the liquid level at the last overflow pipe 11 in the concentrating evaporator 2 is always kept in place by the inverted U-shaped overflow pipe 11 and the pressure equalizing port 211.
In a further embodiment, as shown in fig. 1-3, a first baffle 112 is disposed in the upper tower 101. The working principle of the embodiment is the same as the previous embodiment, and the difference is that: the dilute acid of the feedstock in the shell side of the upper column 101 flows around the first baffle 112 along the S-shaped flow path as it flows.
In a further embodiment, as shown in fig. 1-3, a second baffle 113 is disposed in the lower tower 102. The working principle of the embodiment is the same as the previous embodiment, and the difference is that: the concentrated sulfuric acid in the shell side of the lower tower 102 flows along the S-shaped flow channel around the baffle plate II 113 during the flowing.
In a further embodiment, as shown in fig. 1-3, the vacuum system 6 is a steam injection pump, and the steam injection pump is connected to the overhead gas-phase condenser 5, and is provided with an injection steam inlet 10. The working principle of the steam jet pump of the embodiment is identical to that of the existing steam jet pump.
In a further embodiment, as shown in fig. 1-3, a steam condenser 9 is connected to the steam spraying end of the vacuum system 6, and the steam condenser 9 is connected in parallel with the overhead gas-phase condenser 5 and then connected with the wastewater tank 7. The working principle of the embodiment is that the volume of high-temperature steam sprayed by the steam jet pump is suddenly reduced after the high-temperature steam enters the steam condenser 9, so that a large negative pressure is generated, and the vacuumizing capacity is improved.
While the utility model has been described with reference to the preferred embodiments, it should be understood that the utility model is not limited to the embodiments described above, but is intended to cover modifications, equivalents, and alternatives falling within the spirit and scope of the utility model.
Claims (7)
1. An energy-efficient sulfuric acid evaporation concentration system, its characterized in that: comprises a falling film heat exchange absorption tower (1), a concentrating evaporator (2), a raw material acid storage tank (3), a concentrated acid storage tank (4), a tower top gas phase condenser (5), a vacuum system (6) and a wastewater tank (7);
the falling film heat exchange absorption tower (1) consists of an upper tower (101) and a lower tower (102), wherein the upper tower (101) and the lower tower (102) are separated by a first tube plate (103), a raw material acid inlet (104) is arranged on the side surface of the lower end of the upper tower (101), and the raw material acid inlet (104) is connected with the raw material acid storage tank (3); the top of the upper tower (101) is provided with a secondary steam outlet (105), and the secondary steam outlet (105) is connected with the tower top gas-phase condenser (5); a plurality of falling film heat exchange absorption pipes (106) are longitudinally arranged in the upper tower (101), a falling film device (107) is arranged at the top of each falling film heat exchange absorption pipe (106), and the lower end of each falling film heat exchange absorption pipe (106) penetrates through the first tube plate (103) and then stretches into the lower tower (102) and is connected with the second tube plate (108) arranged at the bottom of the lower tower (102); the bottom end of the lower tower (102) is a sulfuric acid outlet (111) and is connected with an evaporator secondary steam outlet (204) arranged on the concentrating evaporator (2), a concentrated acid inlet (109) and a concentrated acid outlet (110) are arranged on the side face of the lower tower (102) between the first tube plate (103) and the second tube plate (108), the concentrated acid outlet (110) is connected with the concentrated acid storage tank (4), and the concentrated acid inlet (109) is connected with an evaporator concentrated acid outlet (205) arranged on the concentrating evaporator (2).
2. The energy efficient sulfuric acid evaporation concentration system of claim 1, wherein: the concentrating evaporator (2) is horizontal and comprises an evaporator shell (201), wherein the outer sides of two ends of the evaporator shell (201) are respectively provided with a steam inlet (202) and a steam condensate outlet (203), the inner sides of the evaporator shell are respectively provided with a tube plate III (206) and a tube plate IV (207), and a plurality of heat exchange tubes (208) are arranged between the tube plate III (206) and the tube plate IV (207); an evaporator secondary steam outlet (204) and an evaporator concentrated acid outlet (205) are arranged on the evaporator shell (201) between the tube plate III (206) and the tube plate IV (207), the evaporator secondary steam outlet (204) is close to one end of the steam inlet (202), and the evaporator concentrated acid outlet (205) is close to one end of the steam condensate outlet (203); the evaporator comprises an evaporator shell (201) between an evaporator secondary steam outlet (204) and an evaporator concentrated acid outlet (205), wherein a plurality of groups of clapboards (209) are distributed in the evaporator shell, the upper ends of the clapboards (209) are fluid channels, the heights of all the clapboards (209) are consistent, overflow plates (210) are arranged between adjacent clapboards (209), the height of the upper end face of each overflow plate (210) is lower than that of the upper end face of each clapboards (209), the upper ends of the overflow plates (210) are fluid channels, and the heights of the upper ends of the overflow plates (210) gradually decrease along with the fluid flowing direction.
3. The energy efficient sulfuric acid evaporation concentration system of claim 2, wherein: the concentrating evaporator (2) is also connected with an overflow tank (8), the bottom of the overflow tank (8) is connected with the concentrated acid outlet (205) of the evaporator through an inverted U-shaped overflow pipe (11), and the drainage position of the inverted U-shaped overflow pipe (11) is consistent with the height of the upper end face of the last overflow plate (210); the top of the overflow tank (8) is connected with a pressure balance port (211) arranged on the evaporator shell (201); the side surface of the overflow tank (8) is connected with a concentrated acid inlet (109).
4. The energy efficient sulfuric acid evaporation concentration system of claim 1, wherein: a first baffle plate (112) is arranged in the upper tower (101).
5. The energy efficient sulfuric acid evaporation concentration system of claim 1, wherein: a baffle plate II (113) is arranged in the lower tower (102).
6. The energy efficient sulfuric acid evaporation concentration system of claim 1, wherein: the vacuum system (6) is a steam jet pump, the steam jet pump is connected with the tower top gas phase condenser (5), and a jet steam inlet (10) is formed in the steam jet pump.
7. The energy efficient sulfuric acid evaporation concentration system of claim 6, wherein: the steam spraying end of the vacuum system (6) is connected with a steam condenser (9), and the steam condenser (9) is connected with the wastewater tank (7) after being connected with the tower top gas phase condenser (5) in parallel.
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| CN202322216253.XU CN220633012U (en) | 2023-08-17 | 2023-08-17 | Efficient and energy-saving sulfuric acid evaporation concentration system |
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| CN202322216253.XU CN220633012U (en) | 2023-08-17 | 2023-08-17 | Efficient and energy-saving sulfuric acid evaporation concentration system |
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