CN113339770A - Intensive energy-saving sulfur trioxide gas cooling system for sulfonation process and cooling method thereof - Google Patents
Intensive energy-saving sulfur trioxide gas cooling system for sulfonation process and cooling method thereof Download PDFInfo
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- CN113339770A CN113339770A CN202110465124.7A CN202110465124A CN113339770A CN 113339770 A CN113339770 A CN 113339770A CN 202110465124 A CN202110465124 A CN 202110465124A CN 113339770 A CN113339770 A CN 113339770A
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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Abstract
The invention relates to an intensive energy-saving sulfur trioxide gas cooling system for a sulfonation process, which comprises a sulfur trioxide conversion tower outlet and a sulfur trioxide heat recovery device, wherein the sulfur trioxide heat recovery device is formed by sequentially connecting a first-stage heat exchanger and a second-stage heat exchanger in series, the first-stage heat exchanger and the second-stage heat exchanger can be combined into one heat exchange device, sulfur trioxide is connected to a subsequent sulfonation section from the sulfur trioxide conversion tower outlet through the sulfur trioxide heat recovery device, deionized water is connected with a tube pass inlet of the sulfur trioxide heat recovery device through a water replenishing pump, a tube pass outlet of the first-stage heat exchanger is connected with a steam sub-cylinder, and a tube pass outlet of the second-stage heat exchanger is connected to a hot water tank. Meanwhile, the structure of the heat recovery device and the cooling method of the whole cooling system are further designed, so that the process flow is simplified, the investment of equipment and pipelines is reduced, and the power consumption generated by using air as a heat carrier is reduced on the premise of ensuring safety and stable operation.
Description
Technical Field
The invention relates to a heat recovery method and a device thereof in the production process of anionic surfactant sulfoacid (sulfuric acid). The invention belongs to the field of chemical production such as chemical industry, light industry, pharmacy, energy conservation and environmental protection, and can be applied to the reaction heat recovery in the sulfur trioxide gas generation process of a sulfur burning method.
Background
The heat transfer process refers to the process of heat transfer between materials, and is widely applied to the production fields of chemical industry, light industry, pharmacy, energy conservation, environmental protection and the like. The heat exchange of gas has the characteristics of high flow speed, large pressure change, large volume flow change and the like compared with the heat exchange of liquid.
In the gas-phase sulfonation production of sulfur trioxide, sulfur and air are subjected to combustion reaction in a sulfur furnace to generate sulfur dioxide gas, the temperature of the sulfur dioxide gas generated by the reaction is up to 680-700 ℃, the high-temperature sulfur dioxide gas needs to be cooled to about 440-450 ℃ and enters a conversion tower for oxidation reaction, the reaction process is a heat release process, the reaction heat needs to be removed by the gas participating in the reaction, and the reaction is developed towards the direction of generating sulfur trioxide under the action of a multi-stage fixed bed catalyst (usually divided into three-stage or four-stage catalysts). In the former stage, where the reaction temperature increases much between catalyst beds, it is usually necessary to add an interstage cooler between the beds of the reforming column to remove the heat of reaction. The reaction gas can be continuously converted into sulfur trioxide under the action of the catalyst, and the temperature of the generated sulfur trioxide gas when leaving the conversion tower is 400-450 ℃. And cooling the converted sulfur trioxide gas to 50-60 ℃ for the subsequent sulfonation reaction. In the sulfur trioxide sulfonation device 30-40 years ago in the early stage, a coil pipe spraying water cooling mode is adopted for cooling sulfur trioxide gas, equipment cost is saved for the cooler of the type, waste of reaction heat is caused, and consumption of cooling circulating water is increased. This approach has now been abandoned. The method generally adopted in the industry at present is to cool sulfur trioxide gas to below 60 ℃ in a multi-stage heat exchange mode by using cold air as a cold carrier. The heated air enters the waste heat recovery equipment through the air pipe, and low-pressure steam and hot water are prepared in an indirect heat exchange mode for other workshop sections in the workshop. The process is widely used in the industry at present, and has the advantages of large operation flexibility, mature equipment and the problems of more process links, large heat transfer resistance of gas-gas heat exchange, more equipment pipelines and large size, and increases the equipment investment.
Since sulfur trioxide gas is a strongly acidic gas, it is converted into strongly corrosive sulfuric acid upon contact with water, which is very likely to cause corrosion of equipment and endanger the safety of operators. Thus, the most important reason for avoiding the use of water as cooling medium for the sulfur trioxide gas cooling process operation is firstly in terms of safety and secondly the situation that the equipment may be over-pressurized due to the relatively rapid rise in the saturated vapor pressure of water at high temperatures. The above reasons limit the selectivity of the process route.
Disclosure of Invention
In order to solve the problems, the invention provides a method which has the advantages of safe operation, simple process, less usage amount of equipment pipelines, high heat recovery rate and high operation stability, and simultaneously reduces the power consumption generated by using air as a heat carrier.
In order to achieve the purpose, the intensive energy-saving sulfur trioxide gas cooling system for the sulfonation process comprises a sulfur trioxide conversion tower outlet and a sulfur trioxide heat recovery device, wherein the sulfur trioxide heat recovery device is formed by sequentially connecting a first-stage heat exchanger and a second-stage heat exchanger in series, the sulfur trioxide conversion tower outlet is connected to a subsequent sulfonation section through the sulfur trioxide heat recovery device, a deionized water main pipe is connected with a pipe pass inlet of the sulfur trioxide heat recovery device through a water replenishing pump, a pipe pass outlet of the first-stage heat exchanger is connected with a steam cylinder, and a pipe pass outlet of the second-stage heat exchanger is connected to a hot water tank.
The further scheme is that an outlet of the sulfur trioxide conversion tower is connected with an inlet of a shell pass of a first-stage heat exchanger, an outlet of the shell pass of the first-stage heat exchanger is connected with an inlet of a shell pass of a second-stage heat exchanger, an outlet of the shell pass of the second-stage heat exchanger is connected with a subsequent sulfonation working section, an outlet of the tube pass of the first-stage heat exchanger is connected with a steam distributing cylinder, an outlet of the tube pass of the second-stage heat exchanger is connected with a hot water tank, and a water outlet of the hot water. The structure is characterized in that a secondary heat exchanger is adopted, and heat is exchanged in two sections, so that heating media forming steam and hot water are output.
The sulfur trioxide heat recovery device is a heat recovery device which is an inclined structure with the included angle of the central line and the horizontal plane of 1-5 degrees and comprises a first-stage pipe box, a first-stage pipe pass outlet, an outer pipe plate, a first-stage liquid accumulation cavity, an inner pipe plate, a second-stage liquid accumulation cavity, a shell pass inlet, a barrel, a first-stage heat exchange pipe, a shell pass outlet, a second-stage pipe box, a split-pass partition plate, a second-stage pipe pass inlet, a second-stage liquid accumulation cavity exhaust port, a shell pass exhaust port, a second-stage heat exchange pipe, a baffle plate, a saddle-type support, a first-stage liquid accumulation cavity exhaust port and a first-stage pipe pass inlet, wherein the first-stage pipe box and the second-stage pipe box are symmetrically arranged at two ends of the barrel, the outer pipe plate, the first-stage liquid accumulation cavity and the inner pipe plate are sequentially arranged between the first-stage pipe box and the barrel, and the inner pipe plate are arranged between the barrel and the second-stage pipe box at one time, A second-stage liquid accumulation cavity and an outer tube plate, wherein a first-stage tube pass inlet and a first-stage tube pass outlet are arranged on the first-stage tube box, a pass partition plate is arranged in the middle of the first-stage tube box, a second-stage tube pass inlet and a second-stage tube pass outlet are arranged on the second-stage tube box, a pass partition plate is arranged in the middle of the second-stage tube box, the horizontal position of the first-stage tube box is higher than that of the second-stage tube box, a shell pass inlet is arranged at the position, close to the first-stage tube box, on the barrel, a shell pass outlet is arranged at the position, close to the second-stage tube box, on the barrel, a shell pass exhaust port is arranged at the bottom, close to the second-stage tube box, a baffle plate, a first-stage heat exchange tube and a second-stage heat exchange tube are arranged in the barrel, the length of first order heat exchange tube be good at the length of second level heat exchange tube, first order hydrops chamber bottom is equipped with first order hydrops chamber drain outlet, the bottom in second order hydrops chamber is equipped with second order hydrops chamber drain outlet. Through the specially designed heat recovery device, sulfur trioxide gas is placed to be in direct contact with a heating medium, and the reliability of heat exchange is guaranteed, so that the online time and the service life of equipment are effectively prolonged.
In a further scheme, the sulfur trioxide heat recovery device is composed of two separated heat recoverers. A whole set of sulfur trioxide heat recovery device is formed by two separated heat recoverers, the safety and the reliability of heat exchange can be effectively guaranteed, a bypass system can be formed by pipeline switching when necessary, and maintenance is convenient.
The heat exchange tube adopts one of a seamless steel tube, a grooved tube and a finned tube, the heat exchange tube and the outer tube plate are connected in a mode of expansion joint and welding, and the material is one of carbon steel, low alloy steel, stainless steel, titanium material and silicon carbide; the hot water pump and the water replenishing pump are selected from one or a combination of a centrifugal pump, a rotor pump and a reciprocating pump; the front part of the steam cylinder is connected with a high-pressure steam main pipe through a steam temperature and pressure reducing device; steam temperature and pressure reduction device include governing valve and front and back trip valve, set up the bypass that is equipped with the trip valve simultaneously, one of self-operated control valve, electrical control valve and pneumatic control valve is chooseed for use to the governing valve, one of gate valve and stop valve is chooseed for use to the trip valve to set up the moisturizing mouth according to the pressure differential that comes house steward steam and heat exchanger to produce steam. Through further structure refinement to the heat recovery device, guarantee the efficiency of heat recovery to the needs of various production environment are adapted.
A sulfur trioxide gas cooling method using the cooling system, comprising the steps of:
a. high-temperature sulfur trioxide gas with the temperature of 370-520 ℃ enters the shell pass of the first-stage heat exchanger from a sulfur trioxide conversion tower, and the air input is 2500-4500 Nm3H, oxidizing the mixture by primary heat exchangeReducing the temperature of the sulfur gas to 100-250 ℃;
b. enabling sulfur trioxide gas with the temperature of 100-250 ℃ to enter a shell pass of a second-stage heat exchanger from a shell pass outlet of the first-stage heat exchanger, and reducing the temperature of the sulfur trioxide gas to 40-90 ℃ through second-stage heat exchange;
c. deionized water with the temperature of 15-95 ℃ enters a tube pass of a first-stage heat exchanger, the deionized water is heated and gasified through first-stage heat exchange to generate steam, and the steam pressure is 0.2-1.2 MPa;
d. steam with the pressure of 0.2-1.2 MPa enters a steam branch cylinder from a tube pass outlet of a first-stage heat exchanger, the pressure of the steam enters a high-pressure steam from a steam main pipe in the steam branch cylinder, the steam pressure of the steam main pipe is 0.4-1.5 MPa, and the steam is connected to each steam consuming point in a production environment after being regulated;
e. deionized water with the temperature of 15-35 ℃ enters a tube pass of a second-stage heat exchanger, the deionized water is heated through second-stage heat exchange to generate hot water, and the temperature of the outlet hot water is 32-95 ℃;
f. and deionized water with the temperature of 32-95 ℃ enters a hot water tank from an outlet of the tube pass of the second-stage heat exchanger, and hot water in the hot water tank is connected to a hot water main pipe in the production environment through a hot water pump.
The further proposal is that the hot water produced by the second-stage heat exchanger is used for supplementing water for the first-stage heat exchanger.
The further scheme is that the water quality of the deionized water meets the requirements of GB/T1576-2018 'water quality of industrial boilers' and meets the requirements that the hardness is less than or equal to 2.0 mu mol/L, the dissolved oxygen is less than or equal to 15 mu g/L, the iron is less than or equal to 50 mu g/L, the copper is less than or equal to 10 mu g/L, and the silicon dioxide is less than or equal to 20 mu g/L.
Compared with the prior art, the intensive energy-saving sulfur trioxide gas cooling system and the cooling method thereof for the sulfonation process have the following characteristics:
1. the heat exchange equipment which is stable and reliable is used, particularly a double-tube plate heat exchanger and the like is adopted, so that the possibility of contact between sulfur trioxide gas and water (including moisture contained in air) is reduced, the fault rate of a sulfur trioxide cooling section is reduced, and the operation safety is improved;
2. the water is used as a cooling medium to replace air, and the specific heat capacity of the water is far greater than that of the air, so that a water pump with small volume flow and low power can be selected to replace a high-power air fan, and the energy saving rate is 30-75%;
3. the direct heat exchange mode of sulfur trioxide-water replaces an indirect heat exchange mode of sulfur trioxide-air-water, so that the heat efficiency is improved by 20-45%, meanwhile, a waste heat boiler, a hot water heat exchanger and auxiliary equipment, pipelines and instruments thereof are reduced, and the investment of sulfur trioxide workshop section equipment is reduced by 15-30%;
4. the grade of steam generated by recovering heat is improved due to the improvement of the heat efficiency, and the highest pressure of saturated steam generated stably and continuously is increased from 0.6MPa to 1.0-1.2 MPa.
Drawings
FIG. 1 is a schematic system flow chart of example 1 of the present invention.
FIG. 2 is a simplified system flow diagram according to example 2 of the present invention.
FIG. 3 is a schematic view of a sulfur trioxide heat recovery device of the present invention.
Description of reference numerals:
1-sulfur trioxide conversion tower outlet; 2-sulfur trioxide heat recovery unit; 3-steam temperature and pressure reduction device; 4-steam cylinder separation; 5, a hot water tank; 6-hot water pump; 7-a first-stage water replenishing pump; 8-a second-stage water replenishing pump; 21-first stage heat exchanger; 22-second stage heat exchanger; 201-first level channel box; 202-first stage tube pass outlet; 203-outer tube plate; 204-hydrops chamber; 205 — inner tube sheet; 206-shell side inlet; 207-cylinder; 208-first stage heat exchange tube; 209-shell side outlet; 210 — second stage tube pass outlet; 211-second level channel box; 212-a pass divider; 213 — second stage tube pass inlet; 214-second-stage dropsy cavity drain port; 215-shell side drain; 216-second stage heat exchange tube; 217-baffle plate; 218-saddle support; 219-first-stage dropsy cavity drain port; 220 — first stage tube pass inlet.
Detailed Description
To further illustrate the technical means and effects of the present invention adopted to achieve the predetermined objects, the following detailed description of the embodiments, structures, features and effects according to the present invention will be made with reference to the accompanying drawings and preferred embodiments.
Example 1.
The intensive energy-saving sulfur trioxide gas cooling system for the sulfonation process described in this embodiment comprises a sulfur trioxide conversion tower outlet 1 and a sulfur trioxide heat recovery device 2, wherein the sulfur trioxide heat recovery device 2 is a heat recovery device formed by sequentially connecting a first-stage heat exchanger 21 and a second-stage heat exchanger 22 in series, the heat recovery device is an inclined structure with an included angle of 1-5 degrees between a central line and a horizontal plane, and comprises a first-stage tube box 201, a first-stage tube pass outlet 202, an outer-side tube plate 203, a first-stage liquid accumulation cavity, an inner-side tube plate 205, a second-stage liquid accumulation cavity, a shell pass inlet 206, a cylinder 207, a first-stage heat exchange tube 208, a shell pass outlet 209, a second-stage tube pass outlet 210, a second-stage tube box 211, a split-pass partition plate 212, a second-stage tube pass inlet 213, a second-stage liquid accumulation cavity exhaust port 214, a shell pass exhaust port 215, a second-stage heat exchange tube 216, a baffle plate 217, a saddle-type support 218, a first-stage heat exchange tube outlet 210, a second-type support, a second-stage heat exchange tube-type heat recovery device, a second heat recovery device, and a third-type heat recovery device, A first-stage liquid-accumulating-cavity drainage port 219 and a first-stage tube pass inlet 220, a first-stage tube box 201 and a second-stage tube box 211 are symmetrically arranged at two ends of a cylinder 207, an outer tube plate 203, a first-stage liquid-accumulating cavity and an inner tube plate 205 are sequentially arranged between the first-stage tube box 201 and the cylinder 207, the inner tube plate 205, the second-stage liquid-accumulating cavity and the outer tube plate 203 are arranged between the cylinder 207 and the second-stage tube box 211 at one time, a first-stage tube pass inlet 220 and a first-stage tube pass outlet 202 are arranged on the first-stage tube box 201, a pass partition plate 212 is arranged in the middle of the first-stage tube box 201, a second-stage tube pass inlet 213 and a second-stage tube pass outlet 210 are arranged on the second-stage tube box 211, a pass partition plate 212 is arranged in the middle of the second-stage tube box 211, the first-stage tube box 201 is higher in horizontal position than the second-stage tube box 211, a shell pass inlet 206 is arranged in a position close to the first-stage tube box 201 on the cylinder 207, a shell-pass outlet 209 is arranged in a position close to the second-stage tube box 211 on the cylinder 207, a shell pass exhaust port 215 is formed in the bottom, close to the second-stage tube box 211, of the cylinder body 207, a baffle plate 217, a first-stage heat exchange tube 208 and a second-stage heat exchange tube 216 are arranged in the cylinder body 207, the length of the first-stage heat exchange tube 208 is longer than that of the second-stage heat exchange tube 216, a first-stage accumulated liquid cavity exhaust port 219 is formed in the bottom of the first-stage accumulated liquid cavity, and a second-stage accumulated liquid cavity exhaust port 214 is formed in the bottom of the second-stage accumulated liquid cavity. The outlet 1 of the sulfur trioxide conversion tower is connected with a shell pass inlet of a heat recovery device, sulfur trioxide gas enters a cylinder 207 through the shell pass inlet 206, exchanges heat with a first heat exchange tube 208, enters the rear half part of the cylinder 207 through a part of baffle plates 217, exchanges heat with a second-stage heat exchange tube 216, and finally is connected with a subsequent sulfonation working section through a shell pass outlet 209 of the heat recovery device, a first-stage tube pass outlet 202 is connected with a steam cylinder 4, a second-stage tube pass outlet 210 is connected with a hot water tank 5, and a water outlet of the hot water tank 5 is connected with a hot water pump 6.
The heat exchange tube is one of a seamless steel tube, a grooved tube and a finned tube, is connected with the outer tube plate 203 in a manner of expansion joint and welding, and is made of one of carbon steel, low alloy steel, stainless steel, titanium and silicon carbide; the hot water pump 6 and the water replenishing pump are selected from one or a combination of a centrifugal pump, a rotor pump and a reciprocating pump; the front part of the steam cylinder 4 is connected with a high-pressure steam main pipe through a steam temperature and pressure reducing device 3; steam temperature and pressure reduction device 3 include governing valve and front and back trip valve, set up the bypass that is equipped with the trip valve simultaneously, the governing valve is selected for use one of self-operated regulating valve, electrical control valve and pneumatic control valve, one of gate valve and stop valve is selected for use to the trip valve to set up the moisturizing mouth according to the pressure differential that comes from house steward steam and heat exchanger production steam.
The sulfur trioxide gas cooling process described in this example includes the following steps:
(1) the high-temperature sulfur trioxide gas with the temperature of 370-425 ℃ enters a shell pass inlet of a sulfur trioxide heat recovery device from a sulfur trioxide conversion tower, and the air input is 2500-3340 Nm3The temperature of sulfur trioxide gas is reduced to 100-180 ℃ through first-stage heat exchange;
(2) the sulfur trioxide gas with the temperature of 100-180 ℃ enters second-stage heat exchange from the first-stage heat exchange in the shell pass of the sulfur trioxide heat recovery device, and the temperature of the sulfur trioxide gas is reduced to 40-55 ℃ through the second-stage heat exchange;
(3) deionized water with the temperature of 15-50 ℃ directly enters a first-stage tube pass inlet from a second-stage tube pass outlet of the sulfur trioxide heat recovery device, the deionized water is heated and gasified through first-stage heat exchange to generate steam, and the steam pressure is 0.2-0.7 MPa;
(4) the steam with the pressure of 0.2 MPa-0.7 MPa enters a steam branch cylinder from a first-stage tube pass outlet of the sulfur trioxide heat recovery device, the pressure of the steam enters the steam branch cylinder and is regulated with high-pressure steam from a steam main pipe, the steam pressure of the main pipe is 0.4 MPa-0.8 MPa, and the steam is connected to each steam consuming point in a workshop after being regulated;
(5) and deionized water with the temperature of 15-30 ℃ enters a second-stage tube pass inlet of the sulfur trioxide heat recovery device, the deionized water is heated through second-stage heat exchange to generate hot water, and the temperature of the outlet hot water is 32-50 ℃.
Example 2.
The embodiment describes an intensive energy-saving sulfur trioxide gas cooling system for sulfonation processes, wherein the sulfur trioxide heat recovery device is composed of two separate heat recoverers. The structure of the heat recovery device was the same as that of example 1. The shell pass inlet of the first-stage heat recoverer is connected with the outlet of the sulfur trioxide conversion tower, and the shell pass outlet of the first-stage heat recoverer is connected with the shell pass outlet of the second-stage heat recoverer. Two tube pass inlets of the two heat recoverers can be connected with a water replenishing pump, at least one of two tube pass outlets of the first-stage heat recoverer is connected with the steam cylinder, and a first-stage tube pass outlet of the second-stage heat recoverer is connected with a second-stage tube pass inlet of the first-stage heat recovery period.
The sulfur trioxide gas cooling process comprises the following steps:
(1) high-temperature sulfur trioxide gas with the temperature of 430-520 ℃ enters the shell side of the first-stage heat recoverer from a sulfur trioxide conversion tower, and the air input is 3500-4500 Nm3The temperature of sulfur trioxide gas is reduced to 170-250 ℃ through first-stage heat exchange;
(2) enabling sulfur trioxide gas with the temperature of 170-250 ℃ to enter the shell pass of a second-stage heat recoverer from the shell pass outlet of the first-stage heat recoverer, and reducing the temperature of the sulfur trioxide gas to 42-90 ℃ through second-stage heat exchange;
(3) deionized water with the temperature of 32-95 ℃ enters a tube side inlet of a first-stage heat recoverer, the deionized water is heated and gasified through first-stage heat exchange to generate steam, and the steam pressure is 0.6-1.2 MPa;
(4) steam with the pressure of 0.6-1.2 MPa enters a steam branch cylinder from a first-stage heat recoverer, the pressure of the steam enters a high-pressure steam from a steam main pipe in the steam branch cylinder to be regulated, the steam pressure of the main pipe is 0.6-1.5 MPa, and the steam is connected to each steam using point in a workshop after being regulated;
(5) deionized water with the temperature of 32-35 ℃ enters a tube pass inlet of a second-stage heat recoverer, the deionized water is heated through second-stage heat exchange to generate hot water, and the temperature of the outlet hot water is 40-95 ℃;
(6) and deionized water with the temperature of 40-95 ℃ enters a hot water tank from a tube side outlet of the second-stage heat recoverer or enters a tube side inlet of the first-stage heat recoverer, and hot water in the hot water tank is connected to a hot water main pipe in a workshop through a hot water pump.
Although the present invention has been described with reference to the preferred embodiments, it should be understood that various changes, substitutions and alterations can be made herein without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (8)
1. The utility model provides an intensive energy-saving sulfur trioxide gas cooling system for sulfonation process, includes sulfur trioxide conversion tower export and sulfur trioxide heat recovery unit, characterized by sulfur trioxide heat recovery unit form by first order heat exchanger and second level heat exchanger establish ties in proper order, sulfur trioxide conversion tower export be connected to follow-up sulfonation workshop section behind through sulfur trioxide heat recovery unit, the tube side import that the deionized water house steward passes through moisturizing pump connection sulfur trioxide heat recovery unit, the tube side exit linkage steam of first order heat exchanger divide the cylinder, the tube side exit linkage of second level heat exchanger is to the hot-water cylinder.
2. The intensive energy-saving sulfur trioxide gas cooling system for the sulfonation process of claim 1, wherein an outlet of the sulfur trioxide conversion tower is connected with an inlet of a shell side of a first-stage heat exchanger, an outlet of the shell side of the first-stage heat exchanger is connected with an inlet of a shell side of a second-stage heat exchanger, an outlet of the shell side of the second-stage heat exchanger is connected with a subsequent sulfonation section, an outlet of the tube side of the first-stage heat exchanger is connected with a steam cylinder, an outlet of the tube side of the second-stage heat exchanger is connected with a hot water tank, and a water outlet of the hot water tank is connected with a hot water pump.
3. The intensive energy-saving sulfur trioxide gas cooling system for sulfonation according to claim 3, wherein the sulfur trioxide heat recovery device is a heat recovery device, the heat recovery device is an inclined structure having a center line inclined at an angle of 1 to 5 ° from the horizontal plane, and comprises a first-stage tube box, a first-stage tube pass outlet, an outer-side tube plate, a first-stage liquid accumulation chamber, an inner-side tube plate, a second-stage liquid accumulation chamber, a shell pass inlet, a cylinder, a first-stage heat exchange tube, a shell pass outlet, a second-stage tube box, a split partition, a second-stage tube pass inlet, a second-stage liquid accumulation chamber drain, a shell pass drain, a second-stage heat exchange tube, a baffle plate, a saddle-type support, a first-stage liquid accumulation chamber drain and a first-stage tube pass inlet, the first-stage tube box and the second-stage tube box are symmetrically arranged at two ends of the cylinder, and the outer-side tube plate, the second-stage tube box, the first-stage tube box and the cylinder are sequentially arranged between the first-stage tube box and the cylinder, The heat exchanger comprises a first-stage liquid accumulation cavity and an inner tube plate, wherein the inner tube plate, a second-stage liquid accumulation cavity and an outer tube plate are arranged between a barrel and a second-stage tube box at one time, a first-stage tube pass inlet and a first-stage tube pass outlet are arranged on the first-stage tube box, a pass partition plate is arranged in the middle of the first-stage tube box, a second-stage tube pass inlet and a second-stage tube pass outlet are arranged on the second-stage tube box, a pass partition plate is arranged in the middle of the second-stage tube box, the horizontal position of the first-stage tube box is higher than that of the second-stage tube box, a shell pass inlet is arranged at the position, close to the first-stage tube box, of the barrel, a shell pass outlet is arranged at the position, close to the second-stage tube box, a shell pass purge outlet is arranged at the bottom, close to the second-stage tube box, a baffle plate, a first-, the bottom of the second-stage dropsy cavity is provided with a second-stage dropsy cavity drain outlet.
4. The intensive energy-saving sulfur trioxide gas cooling system for sulfonation processes of claim 3, characterized in that said sulfur trioxide heat recovery means is comprised of two separate heat recoverers.
5. The intensive energy-saving sulfur trioxide gas cooling system for sulfonation processes of claim 4, wherein the heat exchange tube is one of a seamless steel tube, a grooved tube and a finned tube, the heat exchange tube is connected with the outer tube plate in an expansion joint and welding manner, and is made of one of carbon steel, low alloy steel, stainless steel, titanium and silicon carbide; the hot water pump and the water replenishing pump are selected from one or a combination of a centrifugal pump, a rotor pump and a reciprocating pump; the front part of the steam cylinder is connected with a high-pressure steam main pipe through a steam temperature and pressure reducing device; steam temperature and pressure reduction device include governing valve and front and back trip valve, set up the bypass that is equipped with the trip valve simultaneously, one of self-operated control valve, electrical control valve and pneumatic control valve is chooseed for use to the governing valve, one of gate valve and stop valve is chooseed for use to the trip valve to set up the moisturizing mouth according to the pressure differential that comes house steward steam and heat exchanger to produce steam.
6. A method for cooling sulfur trioxide gas using the cooling system according to claims 1 to 5, characterized by comprising the steps of: a. high-temperature sulfur trioxide gas with the temperature of 370-520 ℃ enters the shell pass of the first-stage heat exchanger from a sulfur trioxide conversion tower, and the air input is 2500-4500 Nm3The temperature of sulfur trioxide gas is reduced to 100-250 ℃ through first-stage heat exchange; b. sulfur trioxide gas with temperature of 100-250 DEG CEntering a shell pass of a second-stage heat exchanger from a shell pass outlet of the first-stage heat exchanger, and reducing the temperature of sulfur trioxide gas to 40-90 ℃ through second-stage heat exchange; c. Deionized water with the temperature of 15-95 ℃ enters a tube pass of a first-stage heat exchanger, the deionized water is heated and gasified through first-stage heat exchange to generate steam, and the steam pressure is 0.2-1.2 MPa; d. Steam with the pressure of 0.2-1.2 MPa enters a steam branch cylinder from a tube pass outlet of a first-stage heat exchanger, the pressure of the steam enters a high-pressure steam from a steam main pipe in the steam branch cylinder, the steam pressure of the steam main pipe is 0.4-1.5 MPa, and the steam is connected to each steam consuming point in a production environment after being regulated; e. Deionized water with the temperature of 15-35 ℃ enters a tube pass of a second-stage heat exchanger, the deionized water is heated through second-stage heat exchange to generate hot water, and the temperature of the outlet hot water is 32-95 ℃; f. And deionized water with the temperature of 32-95 ℃ enters a hot water tank from an outlet of the tube pass of the second-stage heat exchanger, and hot water in the hot water tank is connected to a hot water main pipe in the production environment through a hot water pump.
7. The sulfur trioxide gas cooling process of claim 6 wherein the hot water produced by the secondary heat exchanger is used to replenish the water in the primary heat exchanger.
8. The method for cooling sulfur trioxide gas according to claim 6, characterized in that the quality of the deionized water meets the requirements of GB/T1576-2018 "quality of Water for Industrial boilers" and meets the requirements of hardness not more than 2.0 μmol/L, dissolved oxygen not more than 15 μ g/L, iron not more than 50 μ g/L, copper not more than 10 μ g/L and silicon dioxide not more than 20 μ g/L.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114682185A (en) * | 2022-03-23 | 2022-07-01 | 中国日用化学研究院有限公司 | Continuous sulfonation device and process for flexible material |
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| CN209263721U (en) * | 2018-10-26 | 2019-08-16 | 中石化广州工程有限公司 | A kind of shell-and-tube exchanger |
| CN212799638U (en) * | 2020-04-28 | 2021-03-26 | 东明俱进化工有限公司 | Improved generation sulfur trioxide gas production system |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN209263721U (en) * | 2018-10-26 | 2019-08-16 | 中石化广州工程有限公司 | A kind of shell-and-tube exchanger |
| CN212799638U (en) * | 2020-04-28 | 2021-03-26 | 东明俱进化工有限公司 | Improved generation sulfur trioxide gas production system |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114682185A (en) * | 2022-03-23 | 2022-07-01 | 中国日用化学研究院有限公司 | Continuous sulfonation device and process for flexible material |
| CN114682185B (en) * | 2022-03-23 | 2024-04-09 | 中国日用化学研究院有限公司 | Continuous sulfonation device and process for flexible material |
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Application publication date: 20210903 |