WO2019192173A1 - Acid generation energy recovery device and method for so3-containing gas - Google Patents

Acid generation energy recovery device and method for so3-containing gas Download PDF

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Publication number
WO2019192173A1
WO2019192173A1 PCT/CN2018/112925 CN2018112925W WO2019192173A1 WO 2019192173 A1 WO2019192173 A1 WO 2019192173A1 CN 2018112925 W CN2018112925 W CN 2018112925W WO 2019192173 A1 WO2019192173 A1 WO 2019192173A1
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Prior art keywords
evaporator
deaerator
low pressure
sent
process gas
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PCT/CN2018/112925
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French (fr)
Chinese (zh)
Inventor
俞向东
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南京海陆化工科技有限公司
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Publication of WO2019192173A1 publication Critical patent/WO2019192173A1/en

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/69—Sulfur trioxide; Sulfuric acid
    • C01B17/90—Separation; Purification
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/69—Sulfur trioxide; Sulfuric acid
    • C01B17/74—Preparation
    • C01B17/76—Preparation by contact processes
    • C01B17/80—Apparatus
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B1/00—Methods of steam generation characterised by form of heating method
    • F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
    • F22B1/16—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being hot liquid or hot vapour, e.g. waste liquid, waste vapour
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

Definitions

  • the present invention relates to the field of chemical industry, particularly, to a S0 3 gas energy recovery system and method of containing the acid.
  • the device After the acid temperature is lowered, the mixture is added to the mixer to add water to reduce the acid concentration, and then sent to the high-temperature absorption tower for circulating absorption of SO 3 ; the device produces acid from the outlet of the evaporator.
  • the tube is connected to the outside, and is supplied by the water heater and the desalted water heater after cooling.
  • the proportion of sulfuric acid in the circulating acid is higher due to the low temperature heat recovery system of the acid smelting and smelting gas, and the external acid temperature is usually From 130 ° C to 160 ° C, some of the heat is still not effectively recovered.
  • This part of the sent sulfuric acid can be added to other process media with lower temperature, can not produce low pressure steam, low energy recovery quality, limited use range.
  • the direct steam production rate of low-pressure steam is generally about 0.25 to 0.40 t per ton of sulfuric acid produced by low-pressure steam, and some of the heat is still not fully utilized.
  • the present invention provides an S0 3 gas sulphuric acid energy recovery device and method for the deficiencies of the prior art.
  • the technical scheme of the first SO 3 gas-containing acid recovery device provided by the present invention is as follows:
  • An S3 3 gas sulphuric acid energy recovery device comprising a reaction tower, an evaporator and an evaporation deaerator, wherein the bottom of the reaction tower is connected to the evaporator by a circulation pump, and an output end of the evaporator It is connected to the upper part of the reaction tower through a mixer, and the other output end of the evaporator is sequentially connected with the evaporator feed water heater, the evaporating deaerator and the desalinated preheater, and the output pipeline of the process gas containing SO 3 is The bottom of the reaction column is connected.
  • the output end of the desalted water is connected to the evaporating deaerator through a desalinating preheater, and an output end of the bottom of the evaporating deaerator is sequentially passed through the low pressure feed pump and the evaporator feed water heater and The input of the evaporator is connected and the other output is connected to the mixer via a low pressure feed pump.
  • the output of the top of the evaporating deaerator is connected to an output pipe of a process gas containing SO 3 .
  • a method for energy recovery using the above apparatus characterized in that the method comprises the following steps:
  • the process gas containing SO 3 is mixed with the low-pressure steam produced by the evaporating deaerator at a mass ratio of 60 ⁇ 40:1 before entering the reaction tower, and some or all of the SO 3 and low pressure in the process gas containing SO 3
  • the steam reacts to generate H 2 SO 4 , and the process gas enters the reaction tower after the temperature rises, and continues to react with the circulating acid under the upper spray, and the high-temperature sulfuric acid formed by the reaction is combined at the bottom of the tower and then pressurized by the circulation pump.
  • the evaporator generates low-pressure steam, and the tail gas is sent to the next process after the reaction of the process gas;
  • the ambient temperature demineralized water sent by the outside is first heated in the desalinated preheater, then sent to the evaporating deaerator for heating, and the low pressure steam is generated simultaneously with the thermal deaeration, and the low pressure steam is sent to the inlet of the reaction tower and the process gas.
  • the deaerated water in the evaporating deaerator is pressurized by the low pressure feed water pump, 25 ⁇ 15% (mass percentage) of the low pressure feed water to the mixer to reduce the circulating acid concentration, and the remaining low pressure feed water is sent to the evaporator feed water heater. After heating, it is sent to the evaporator to generate low pressure steam.
  • the pressure of the low-pressure steam generated by the evaporating deaerator (6) in step (1) is 0.2 ⁇ 0.1 MPa
  • the temperature of the high-temperature sulfuric acid at the outlet of the circulation pump (2) is 190 ⁇ 30° C.
  • the evaporator (3) The generated low pressure steam pressure is 0.8 ⁇ 0.4 MPa.
  • An S3 3 gas sulphuric acid energy recovery device comprising a reaction tower, an evaporator, an evaporator feed water heater and an evaporative deaerator, wherein the bottom of the reaction tower is connected to the evaporator through a circulation pump, and the evaporator One output is connected to the upper portion of the reaction tower through a mixer, and the other output end of the evaporator is connected to the evaporator feed water heater and the evaporating deaerator, respectively, and the output of the evaporator feed water heater and the evaporating deaerator are Connected to the desalted preheater, the output line of the SO 3 containing process gas is connected to the bottom of the reaction column.
  • the output end of the desalinated water is connected to the evaporating deaerator through a desalinating preheater, and an output end of the bottom of the evaporating deaerator is sequentially passed through a low pressure feed pump and an evaporator feed water heater.
  • the input of the evaporator is connected and the other output is connected to the mixer via a low pressure feed pump.
  • the output of the top of the evaporating deaerator is connected to an output pipe of a process gas containing SO 3 .
  • a method for energy recovery using the apparatus described above comprising the steps of:
  • the process gas containing SO 3 is mixed with the low-pressure steam produced by the evaporating deaerator at a mass ratio of 60 ⁇ 40:1 before entering the reaction tower, and some or all of the SO 3 and low pressure in the process gas containing SO 3
  • the steam reacts to generate H 2 SO 4 , and the process gas enters the reaction tower after the temperature rises, and continues to react with the circulating acid under the upper spray, and the high-temperature sulfuric acid formed by the reaction is combined at the bottom of the tower and then pressurized by the circulation pump.
  • the evaporator generates low-pressure steam, and the tail gas is sent to the next process after the reaction of the process gas;
  • the part 60 ⁇ 40% (mass%) enters the evaporative deaerator to remove oxygen and generate low-pressure steam, and the other part enters the evaporator feed water heater to heat the low-pressure feed water, from the evaporative deaerator and the evaporator
  • the sulfuric acid coming out of the feed water heater enters the desalinated preheater, preheating the normal temperature to remove the brine, and after the temperature is lowered, the sulfuric acid is sent to the downstream process for treatment;
  • the ambient temperature demineralized water sent by the outside is first heated in the desalinated preheater, then sent to the evaporating deaerator for heating, and the low pressure steam is generated simultaneously by the thermal deaeration, and the low pressure steam is sent to the reaction tower inlet line and the process gas.
  • the SO 3 reaction after the deaerated water in the evaporating deaerator is pressurized by the low pressure feed water pump, 25 ⁇ 15% (mass percent) of the low pressure feed water is fed to the mixer to reduce the circulating acid concentration, and the remaining part is sent to the evaporator feed water heater. After heating, it is sent to the evaporator to generate low pressure steam.
  • the pressure of the low-pressure steam generated by the evaporating deaerator in step (1) is 0.15 ⁇ 0.05 MPa
  • the temperature of the high-temperature sulfuric acid at the outlet of the circulating pump is 190 ⁇ 30° C.
  • the pressure of the evaporator generating low-pressure steam is 0.8 ⁇ 0.4 MPa.
  • a third aspect of the present invention provides an acid-containing S0 3 gas energy recovery system is as follows:
  • An S3 3 gas sulphuric acid energy recovery device comprising a reaction tower, an evaporator, an evaporator feed water heater mixer connected to an upper portion of the reaction tower, and the other output end of the evaporator is sequentially connected with an evaporating deaerator and evaporating
  • the feed water heater is connected to the desalinated preheater, and the output line of the process gas containing SO 3 is connected to the bottom of the reaction tower.
  • the output of the desalted water is connected to the evaporating deaerator through a desalinating preheater, and an output end of the bottom of the evaporating deaerator is sequentially passed through the low pressure feed pump and the evaporator feed water heater and the evaporator. Connected, the other output is connected to the mixer via a low pressure feed pump.
  • the output of the top of the evaporating deaerator is connected to an output pipe of a process gas containing SO 3 .
  • a method for realizing energy recovery of sulphuric acid containing S0 3 gas by using the above device comprising the steps of:
  • the process gas containing SO 3 is mixed with the low-pressure steam produced by the evaporating deaerator at a mass ratio of 60 ⁇ 40:1 before entering the reaction tower, and some or all of the SO 3 and low pressure in the process gas containing SO 3
  • the steam reacts to generate H 2 SO 4 , and the process gas enters the reaction tower after the temperature rises, and continues to react with the circulating acid under the upper spray, and the high-temperature sulfuric acid formed by the reaction is combined at the bottom of the tower and then pressurized by the circulation pump.
  • the evaporator generates low-pressure steam, and the tail gas is sent to the next process after the reaction;
  • the ambient temperature demineralized water sent by the outside is first heated in the desalinated preheater, then sent to the evaporating deaerator for heating, and the low pressure steam is generated simultaneously with the thermal deaeration, and the low pressure steam is sent to the inlet of the reaction tower and the process gas.
  • the deaerated water in the evaporating deaerator is pressurized by the low pressure feed water pump, 25 ⁇ 15% (mass percentage) of the low pressure feed water to the mixer to reduce the circulating acid concentration, and the remaining low pressure feed water is sent to the evaporator feed water heater. After heating, it is sent to the evaporator to generate low pressure steam.
  • the pressure of the low-pressure steam generated by the evaporating deaerator in step (1) is 0.15 ⁇ 0.05 MPa
  • the temperature of the high-temperature sulfuric acid at the outlet of the ring pump is 190 ⁇ 30° C.
  • the pressure of the low-pressure steam generated by the evaporator is 0.8 ⁇ 0.4. MPa.
  • the pressures described in the technical solutions of the present invention are all gauge pressures.
  • FIG 2 is a schematic diagram of another S0 3 gas energy recovery system containing an acid.
  • FIG. 3 is a schematic S0 3 gas energy recovery system of the third containing acid.
  • 1 is the reaction tower
  • 2 is the circulation pump
  • 3 is the evaporator
  • 4 is the mixer
  • 5 is the evaporator feed water heater
  • 6 is the evaporation deaerator
  • 7 is the desalinated preheater
  • 8 is the low pressure feed pump .
  • the apparatus comprising a reaction column (1), an evaporator (3) and evaporated deaerator (6), the bottom of the reaction column (1) by a circulation pump (2) is connected to the evaporator (3), and an output end of the evaporator (3) is connected to an upper portion of the reaction column (1) through a mixer (4), the evaporator (3)
  • the other output is connected in series through the evaporator feed water heater (5), the evaporative deaerator (6) and the desalinated preheater (7), the output line of the process gas containing SO 3 and the bottom of the reaction tower (1). Connected.
  • the output of the desalted water is connected to the evaporating deaerator (6) through a desalted water preheater (7), and an output end of the evaporating deaerator (6) is sequentially passed through the low pressure feed pump (8) with the evaporator.
  • the feedwater heater (5) is connected to the input of the evaporator (3) and the other output is connected to the mixer (4) via a low pressure feed pump (8).
  • the output of the evaporator top deaerator (6) and the output duct of the process gas containing SO 3 is connected.
  • the process gas containing SO 3 is mixed with 0.1 MPa (g) of low pressure steam produced by the evaporating deaerator (6) in a mass ratio of 30:1 before entering the reaction column (1), and some SO 3 and low pressure in the process gas.
  • the temperature of the sulfuric acid formed by the steam reaction increases, and the temperature of the process gas rises to 40 ° C.
  • the process gas continues to react with the circulating acid under the upper spray, and the reaction forms a high temperature sulfuric acid of 200 ° C after confluence at the bottom of the column.
  • 80% (mass percentage) of high-temperature sulfuric acid exits the evaporator (3) and then enters the mixer (4).
  • the low-pressure feed water is used to reduce the acid concentration and then enter the reaction column (1) to absorb the SO 3 in the process gas, and the remaining part of the high temperature.
  • Sulfuric acid is taken from the outlet acid pipeline of the evaporator (3) outlet, first enters the evaporator feed water heater (5) and is heated to the low-pressure feed water, and then enters the evaporating deaerator (6) to remove oxygen and generate low-pressure steam 0.1MPa. Finally, the demineralized water preheater is introduced, the salt water is preheated at normal temperature, and the temperature of the external sulfuric acid is lowered to 105 ° C to be sent to the downstream process.
  • the ambient temperature demineralized water sent by the outside is first heated to 100 ° C in the desalted water preheater (7), then sent to the evaporating deaerator (6), heated to 120 ° C, and the thermal deaeration simultaneously produces 0.1 MP (g) low pressure.
  • Steam, low pressure steam is sent to the reaction tower (1) inlet and reacted with SO 3 in the process gas, and the deaerated water in the evaporating deaerator (6) is pressurized by the low pressure feed pump (8), 10% (mass percentage)
  • the low pressure feed water supply mixer (4) reduces the circulating acid concentration, and the remaining evaporator feed water heater (5) is heated to 160 ° C and sent to the evaporator to produce 0.6 MPa of low pressure steam.
  • the temperature of the sulfuric acid is significantly reduced, and the low-pressure steam of 0.595 tons per ton of sulfuric acid by-product can be realized.
  • the SO 3 -containing process gas is mixed with 0.15 MPa (g) of low-pressure steam produced by the evaporating deaerator (6) at a mass ratio of 50:1 before entering the reaction column (1).
  • Part of the process gas contains SO 3 and low pressure.
  • the temperature of the sulfuric acid process gas is increased by steam reaction, and the temperature of the process gas is raised to 55 ° C.
  • the process gas continues to react with the circulating acid under the upper spray, and the reaction produces a high temperature sulfuric acid of 210 ° C after confluence at the bottom of the column.
  • 85% (mass percent) of high-temperature sulfuric acid exits the evaporator (3) and mostly enters the mixer (4), lowers the acid concentration with low-pressure feed water, and then enters the reaction tower (1) to absorb the SO 3 in the process gas, and the remaining
  • the high-temperature sulfuric acid is taken out from the outlet acid circuit of the evaporator outlet, first enters the evaporator feed water heater (5) and is heated to the low-pressure feed water, and then enters the evaporating deaerator (6) to remove oxygen and generate low-pressure steam 0.15MPa, and finally enters
  • the desalinated preheater is preheated to remove salt water at normal temperature, and the temperature of the external sulfuric acid is lowered to 115 ° C for downstream processing.
  • the ambient temperature demineralized water sent by the outside is first heated to 110 ° C in the desalted water preheater (7), then sent to the evaporating deaerator (6), heated to 127 ° C, and the heat deoxidation simultaneously generates 0.15 MP low pressure steam, low pressure.
  • the steam is sent to the reaction tower (1) and reacted with SO 3 in the process gas.
  • 20% (mass percent) of the low pressure feed water is sent.
  • the mixer (4) reduces the circulating acid concentration, and the remainder is sent to the evaporator feed water heater (5), heated to 170 ° C, and sent to the evaporator to produce 0.8 MPa of low pressure steam.
  • the temperature of the sulfuric acid is significantly reduced, and the low-pressure steam of 0.584 tons per ton of sulfuric acid by-product can be realized.
  • the process gas containing SO 3 is mixed with 0.2 MPa (g) of low pressure steam generated by the evaporating deaerator (6) at a mass ratio of 90:1 before entering the reaction column (1), and some SO 3 and low pressure in the process gas.
  • the steam reaction generates H 2 SO process gas temperature rise, the process gas temperature rise is 70 ° C, after entering the reaction tower (1), the process gas continues to react with the circulating acid under the upper spray, and the reaction generates 220 ° C high temperature sulfuric acid at the bottom of the tower. After the combination, it is pressurized by the circulating pump (2) and sent to the evaporator (3) to generate 1.2 MPa (g) of low-pressure steam. After the reaction, the tail gas is sent to the next process.
  • the normal temperature demineralized water sent from the outside is first heated to 120 ° C in the desalinated preheater (7), then sent to the evaporating deaerator (6), heated to 133 ° C, and the thermal deaeration simultaneously produces 0.2 MP (g) low pressure.
  • Low pressure steam is sent to the reaction tower (1) inlet and reacted with SO 3 in the process gas, and the deaerated water in the evaporating deaerator (6) is pressurized by the low pressure feed pump (8), 40% (mass percentage)
  • the low pressure feed water mixer (4) reduces the circulating acid concentration, and the remainder is sent to the evaporator feed water heater (5), heated to 185 ° C, and sent to the evaporator to produce 1.2 MPa of low pressure steam.
  • the temperature of the sulfuric acid is significantly reduced, and the low-pressure steam of 0.578 tons per ton of sulfuric acid by-product can be realized.
  • the apparatus comprising a reaction column (1), an evaporator (3), an evaporator feedwater heater (5) and evaporated deaerator (6), the The bottom of the reaction column (1) is connected to the evaporator (3) through a circulation pump (2), and an output end of the evaporator (3) is connected to the upper portion of the reaction column (1) through a mixer (4), and the evaporator ( The other output of 3) is connected to the evaporator feed water heater (5) and the evaporative deaerator (6), respectively, and the output of the evaporator feed water heater (5) and the evaporating deaerator (6) are The desalted water preheater (7) is connected, and the output pipe of the SO 3 containing process gas is connected to the bottom of the reaction column (1).
  • the external desalted water end is connected to the evaporating deaerator (6) through a desalted water preheater (7), and an output end of the bottom of the evaporating deaerator (6) is sequentially supplied with water through the low pressure feed pump (8)
  • the heater (5) is connected to the input of the evaporator (3) and the other output is connected to the mixer (4) via a low pressure feed pump (8).
  • the output of the evaporator top deaerator (6) and the output duct of the process gas containing SO 3 is connected.
  • the process gas containing SO 3 is mixed with 0.1 MPa (g) of low pressure steam produced by the evaporating deaerator (6) at a mass ratio of 30:1 before entering the reaction column (1), and some SO 3 and low pressure in the process gas.
  • the temperature of the sulfuric acid formed by the steam reaction increases, and the temperature of the process gas rises to 40 ° C.
  • the process gas continues to react with the circulating acid under the upper spray, and the reaction forms a high temperature sulfuric acid of 200 ° C after confluence at the bottom of the column.
  • the normal temperature demineralized water sent from the outside is first heated to 95 ° C in the desalted water preheater (7), then sent to the evaporating deaerator (6), heated to 120 ° C, and the heat deoxidation simultaneously generates 0.1 MP low pressure steam, low pressure
  • the steam is sent to the reaction tower (1) and reacted with SO 3 in the process gas.
  • 10% (mass percent) of the low pressure feed water is sent.
  • the mixer (4) reduces the circulating acid concentration, and the remainder is sent to the evaporator feed water heater (5), heated to 158 ° C, and sent to the evaporator to produce 0.6 MPa of low pressure steam.
  • the temperature of the sulfuric acid is significantly reduced, and the low-pressure steam of 0.632 tons per ton of sulfuric acid by-product can be realized.
  • the process gas containing SO 3 is mixed with 0.15 MPa of low pressure steam produced by the evaporating deaerator (6) at a mass ratio of 50:1 before entering the reaction column (1), and some SO 3 in the process gas is reacted with low pressure steam to form
  • the temperature of the sulfuric acid process gas rises, and the temperature of the process gas rises to 55 ° C.
  • the process gas continues to react with the circulating acid under the upper spray, and the reaction produces a high temperature sulfuric acid of 210 ° C, which is merged at the bottom of the column and then passed through a circulation pump.
  • the ambient temperature demineralized water sent by the outside is first heated to 98 ° C in the desalted water preheater (7), then sent to the evaporating deaerator (6), heated to 127 ° C, and the heat deoxidation simultaneously generates 0.15 MP low pressure steam, low pressure
  • the steam is sent to the reaction tower (1) and reacted with SO 3 in the process gas.
  • 20% (mass percent) of the low pressure feed water is sent.
  • the mixer (4) reduces the circulating acid concentration, and the remainder is sent to the evaporator feed water heater (5), heated to 163 ° C, and sent to the evaporator to produce 0.8 MPa of low pressure steam.
  • the temperature of the sulfuric acid is significantly reduced, and the low-pressure steam of 0.625 tons per ton of sulfuric acid by-product can be realized.
  • the process gas containing SO 3 is mixed with 0.2 MPa (g) of low pressure steam produced by the evaporating deaerator (6) at a mass ratio of 90:1 before entering the reaction column (1), and some SO 3 and low pressure in the process gas.
  • the temperature of the sulfuric acid process gas is increased by steam reaction, and the temperature of the process gas is increased to 70 ° C.
  • the process gas continues to react with the circulating acid under the upper spray, and the reaction forms a high temperature sulfuric acid of 220 ° C after confluence at the bottom of the tower.
  • the tail gas is sent to the next process.
  • 95% (mass percent) of high-temperature sulfuric acid exits the evaporator (3) and then enters the mixer (4).
  • the low-pressure feed water is used to reduce the acid concentration and then enter the reaction column (1) to absorb the SO 3 in the process gas, and the remaining high-temperature sulfuric acid. It is taken out from the outlet acid circuit of the evaporator outlet and divided into two parts. 40% (mass percent) enters the evaporator feed water heater (5) and is heated to the low pressure feed water, and 60% (mass percent) enters the evaporative deaerator.
  • the normal temperature demineralized water sent from the outside is first heated to 107 ° C in the desalinated preheater (7), then sent to the evaporating deaerator (6), heated to 133 ° C, and deactivated by heat to generate 0.2 MP (g) low pressure.
  • Low pressure steam is sent to the reaction tower (1) inlet and reacted with SO 3 in the process gas, and the deaerated water in the evaporating deaerator (6) is pressurized by the low pressure feed pump (8), 40% (mass percentage)
  • the low pressure feed water mixer (4) reduces the circulating acid concentration, and the remainder is sent to the evaporator feed water heater (5), heated to 176 ° C, and sent to the evaporator to produce 1.2 MPa of low pressure steam.
  • the temperature of the sulfuric acid is significantly reduced, and the low-pressure steam of 0.608 tons per ton of sulfuric acid by-product can be realized.
  • S0 3 containing acid gas energy recovery system comprising a reaction column (1), an evaporator (3), an evaporator feedwater heater (5) and evaporated deaerator (6), the The bottom of the reaction column (1) is connected to the evaporator (3) through a circulation pump (2), and an output end of the evaporator (3) is connected to the upper portion of the reaction column (1) through a mixer (4), and the evaporator ( The other output of 3) is connected to the evaporating deaerator (6), the evaporator feed water heater (5) and the desalinated preheater (7) in sequence, and the output pipe and reaction tower of the process gas containing SO 3 ( 1) The bottom is connected.
  • the input end of the desalted water is connected to the evaporating deaerator (6) through a desalted preheater (7), and an output end of the bottom of the evaporating deaerator (6) is sequentially passed through the low pressure feed pump (8) with the evaporator
  • the feedwater heater (5) is connected to the input of the evaporator (3) and the other output is connected to the mixer (4) via a low pressure feed pump (8).
  • the output of the evaporator top deaerator (6) and the output duct of the process gas containing SO 3 is connected.
  • the process gas containing SO 3 is mixed with 0.1 MPa (g) of low pressure steam produced by the evaporating deaerator (6) at a mass ratio of 30:1 before entering the reaction column (1), and part of the SO 3 and low pressure steam in the process gas.
  • the temperature of the sulfuric acid produced by the reaction is increased, and the temperature of the process gas is raised to 40 ° C.
  • the process gas continues to react with the circulating acid under the upper spray, and the reaction produces a high temperature sulfuric acid at 200 ° C.
  • the circulating pump (2) is pressurized and sent to the evaporator (3) to generate 0.6 MPa (g) of low pressure steam. After the reaction, the tail gas is sent to the next process.
  • the normal temperature demineralized water sent from the outside is first heated to 98 ° C in the desalted water preheater (7), then sent to the evaporating deaerator (6), heated to 120 ° C, and the thermal deaeration simultaneously produces 0.1 MP (g) low pressure.
  • Low pressure steam is sent to the reaction tower (1) inlet and reacted with SO 3 in the process gas, and the deaerated water in the evaporating deaerator (6) is pressurized by the low pressure feed pump (8), 10% (mass percentage)
  • the low pressure feed water mixer (4) reduces the circulating acid concentration, and the remainder is sent to the evaporator feed water heater (5), heated to 150 ° C, and sent to the evaporator to produce 0.6 MPa of low pressure steam.
  • the temperature of the sulfuric acid is significantly reduced, and the low-pressure steam of 0.615 tons per ton of sulfuric acid by-product can be realized.
  • the process gas containing SO 3 is mixed with 0.15 MPa (g) of low pressure steam produced by the evaporating deaerator (6) at a mass ratio of 50:1 before entering the reaction column (1), and part of the SO 3 and low pressure steam in the process gas.
  • the reaction generates H 2 SO process gas temperature rise, the process gas temperature rise is 55 ° C, after entering the reaction tower (1), the process gas continues to react with the circulating acid under the upper spray, and the reaction produces 210 ° C high temperature sulfuric acid at the bottom of the tower.
  • the tail gas is sent to the next process.
  • the normal temperature demineralized water sent from the outside is first heated to 105 ° C in the desalted water preheater (7), then sent to the evaporating deaerator (6), heated to 127 ° C, and the thermal deaeration simultaneously produces 0.15 MP (g) low pressure.
  • Low pressure steam is sent to the reaction tower (1) inlet and reacted with SO 3 in the process gas, and the deaerated water in the evaporating deaerator (6) is pressurized by the low pressure feed pump (8), 20% (mass percentage)
  • the low pressure feed water mixer (4) reduces the circulating acid concentration, and the remainder is sent to the evaporator feed water heater (5), heated to 160 ° C, and sent to the evaporator to produce 0.8 MPa of low pressure steam.
  • the temperature of the sulfuric acid is significantly reduced, and the low-pressure steam of 0.603 tons per ton of sulfuric acid by-product can be realized.
  • the process gas containing SO 3 is mixed with 0.2 MPa (g) of low pressure steam produced by the evaporating deaerator (6) at a mass ratio of 90:1 before entering the reaction column (1), and some SO 3 and low pressure in the process gas.
  • the temperature of the sulfuric acid process gas is increased by steam reaction, and the temperature of the process gas is increased to 70 ° C.
  • the process gas continues to react with the circulating acid under the upper spray, and the reaction forms a high temperature sulfuric acid of 220 ° C after confluence at the bottom of the tower.
  • the tail gas is sent to the next process.
  • 95% (mass percent) of high-temperature sulfuric acid exits the evaporator (3) and then enters the mixer (4).
  • the low-pressure feed water is used to reduce the acid concentration and then enter the reaction column (1) to absorb the SO 3 in the process gas, and the remaining high-temperature sulfuric acid.
  • From the outlet of the evaporator outlet acid pipeline first enter the evaporation deaerator (6) thermal deaeration and generate low pressure steam 0.2MPa, then enter the evaporator feed water heater (5) heated to send low pressure feed water, and finally into the desalinated water
  • the preheater is preheated to remove salt water at normal temperature, and the temperature of the external sulfuric acid is lowered to 121 ° C for downstream processing.
  • the ambient temperature demineralized water sent by the outside is first heated to 115 ° C in the desalted water preheater (7), then sent to the evaporating deaerator (6), heated to 133 ° C, and the thermal deaeration simultaneously produces 0.2 MP (g) low pressure.
  • Low pressure steam is sent to the reaction tower (1) inlet and reacted with SO 3 in the process gas, and the deaerated water in the evaporating deaerator (6) is pressurized by the low pressure feed pump (8), 35% (mass percentage)
  • the low pressure feed water mixer (4) reduces the circulating acid concentration, and the remainder is sent to the evaporator feed water heater (5), heated to 171 ° C, and sent to the evaporator to produce 1.2 MPa of low pressure steam.
  • the temperature of the sulfuric acid is significantly reduced, and the low-pressure steam of 0.596 tons per ton of sulfuric acid by-product can be realized.

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Abstract

An acid generation energy recovery device and method for SO3-containing gas. The device comprises a reaction tower (1), an evaporator (3) and an evaporation deaerator (6); a bottom portion of the reaction tower (1) is connected to the evaporator (3) by means of a circulation pump (2), and an output end of the evaporator (3) is connected to an upper portion of the reaction column tower (1) by means of a mixer (4), while another output end of the evaporator (3) is sequentially connected to an evaporator water feeding heater (5), the evaporation deaerator (6) and a desalted water preheater (7); an output pipe for SO3-containing process gas is connected to the bottom portion of the reaction tower (1). The device directly produces low-pressure steam by using heat from externally provided sulfuric acid, which is then sent to a process gas pipe before the reaction tower so as to replace part of the water added to the mixer, thereby reducing the working load of the mixer, reducing the circulating acid flow, and reducing the power consumption of the circulating pump. More importantly, the heat of low-temperature steam is converted to the heat of high-temperature concentrated acid without additional energy consumption, and same passes through the evaporator to generate more low-pressure steam of a higher pressure.

Description

一种含S0 3气体制酸能量回收装置及方法 One containing S0       3 gas acid production energy recovery device and method      技术领域Technical field
本发明涉及化工领域，具体涉及一种含S0 3气体制酸能量回收装置及方法。 The present invention relates to the field of chemical industry, particularly, to a S0 3 gas energy recovery system and method of containing the acid.
背景技术Background technique
目前硫酸生产行业，特别是在矿或冶炼烟气制酸行业，很多装置SO 3被H 2O吸收生产硫酸反应的能量通常由循环水带到大气中，全部或大部分浪费了。这种工艺流程不但没有产生效益，而且需要消耗大量循环水。有部分装置在干吸工段已设置了低温热回收装置，其主要工艺流程是：含SO 3的工艺气体进入高温吸收塔，被塔内喷淋酸吸收，释放出热量，酸温升高，高温浓酸被高温循环泵抽送加压送入蒸发器产生低压蒸汽，酸温降低后进入混合器加水降低酸浓，而后再送入高温吸收塔循环吸收SO 3；装置产酸从蒸发器出口的循环酸管上接出，经给水加热器和脱盐水加热器降温后外供，由于矿回冶炼烟气制酸干吸低温热回收系统外供硫酸在循环酸中的比例较高，外供酸温通常为130℃～160℃，仍有部分热量未能有效回收，这部分外送硫酸可加入其它温度较低的工艺介质，不能产生低压蒸汽，能量回收品质低，使用范围受限。在这类低温热回收装置中，低压蒸汽的直接产汽率一般为每生产1吨硫酸产低压蒸汽0.25～0.40t左右，仍有部分热量并未充分利用。 At present, in the sulfuric acid production industry, especially in the mine or smelting flue gas acid production industry, many devices that absorb SO 2 by H 2 O to produce sulfuric acid are usually brought to the atmosphere by circulating water, and all or most of it is wasted. This process not only does not produce benefits, but also consumes a lot of circulating water. Some devices have set up a low-temperature heat recovery device in the dry suction section. The main process flow is: the process gas containing SO 3 enters the high-temperature absorption tower, is absorbed by the spray acid in the tower, releases heat, and the acid temperature rises, high temperature. The concentrated acid is pumped by the high-temperature circulating pump and sent to the evaporator to generate low-pressure steam. After the acid temperature is lowered, the mixture is added to the mixer to add water to reduce the acid concentration, and then sent to the high-temperature absorption tower for circulating absorption of SO 3 ; the device produces acid from the outlet of the evaporator. The tube is connected to the outside, and is supplied by the water heater and the desalted water heater after cooling. The proportion of sulfuric acid in the circulating acid is higher due to the low temperature heat recovery system of the acid smelting and smelting gas, and the external acid temperature is usually From 130 ° C to 160 ° C, some of the heat is still not effectively recovered. This part of the sent sulfuric acid can be added to other process media with lower temperature, can not produce low pressure steam, low energy recovery quality, limited use range. In such a low-temperature heat recovery device, the direct steam production rate of low-pressure steam is generally about 0.25 to 0.40 t per ton of sulfuric acid produced by low-pressure steam, and some of the heat is still not fully utilized.
发明内容Summary of the invention
本发明是针对现有技术存在的不足提供S0 3气体制酸能量回收装置及方法。 The present invention provides an S0 3 gas sulphuric acid energy recovery device and method for the deficiencies of the prior art.
本发明的目的可以通过以下技术方案实现The object of the present invention can be achieved by the following technical solutions
本发明提供的第一种含S0 3气体制酸能量回收装置的技术方案如下： The technical scheme of the first SO 3 gas-containing acid recovery device provided by the present invention is as follows:
一种含S0 3气体制酸能量回收装置，该装置包括反应塔、蒸发器和蒸发除氧器，所述的反应塔的底部通过循环泵与蒸发器相连，所述的蒸发器的一个输出端通过混合器与反应塔的上部相连，所述的蒸发器的另一个输出端依次与蒸发器给水加热器、蒸发除氧器和脱盐水预热器相连，含SO 3的工艺气体的输出管道与反应塔的底部相连。 An S3 3 gas sulphuric acid energy recovery device, the device comprising a reaction tower, an evaporator and an evaporation deaerator, wherein the bottom of the reaction tower is connected to the evaporator by a circulation pump, and an output end of the evaporator It is connected to the upper part of the reaction tower through a mixer, and the other output end of the evaporator is sequentially connected with the evaporator feed water heater, the evaporating deaerator and the desalinated preheater, and the output pipeline of the process gas containing SO 3 is The bottom of the reaction column is connected.
在一些具体的技术方案中：脱盐水的输出端通过脱盐水预热器与蒸发除氧器相连，所述的蒸发除氧器底部的一个输出端通过低压给水泵依次与蒸发器给水加热器和蒸发器的 输入端相连，另一个输出端通过低压给水泵与混合器相连。In some specific technical solutions, the output end of the desalted water is connected to the evaporating deaerator through a desalinating preheater, and an output end of the bottom of the evaporating deaerator is sequentially passed through the low pressure feed pump and the evaporator feed water heater and The input of the evaporator is connected and the other output is connected to the mixer via a low pressure feed pump.
在一些具体的技术方案中：所述的蒸发除氧器顶部的输出端与含SO 3的工艺气体的输出管道相连。 In some specific technical solutions, the output of the top of the evaporating deaerator is connected to an output pipe of a process gas containing SO 3 .
一种利用上述的装置实现能量回收的方法，其特征在于：该方法包括以下步骤：A method for energy recovery using the above apparatus, characterized in that the method comprises the following steps:
(1)含SO 3的工艺气体在进入反应塔前，先与蒸发除氧器产生的低压蒸汽按60±40:1的质量比混合，含SO 3的工艺气体中部分或全部SO 3与低压蒸汽反应生成H 2SO 4，所述的工艺气体温度升高后进入反应塔后与上部喷淋下的循环酸继续反应，反应生成的高温硫酸在塔底部汇合后经循环泵加压后送入蒸发器产生低压蒸汽，工艺气体反应后尾气送下一工序处理； (1) The process gas containing SO 3 is mixed with the low-pressure steam produced by the evaporating deaerator at a mass ratio of 60±40:1 before entering the reaction tower, and some or all of the SO 3 and low pressure in the process gas containing SO 3 The steam reacts to generate H 2 SO 4 , and the process gas enters the reaction tower after the temperature rises, and continues to react with the circulating acid under the upper spray, and the high-temperature sulfuric acid formed by the reaction is combined at the bottom of the tower and then pressurized by the circulation pump. The evaporator generates low-pressure steam, and the tail gas is sent to the next process after the reaction of the process gas;
(2)85±10％(质量百分数)的高温硫酸出蒸发器后一部分进入混合器，用低压给水降低酸浓后再进入反应塔循环吸收工艺气体中的SO 3，剩余的高温硫酸从蒸发器出口循环酸管路上接出，先进入蒸发器给水加热器加热送入低压给水，再进入蒸发除氧器热力除氧并产生低压蒸汽，最后进入脱盐水预热器，预热常温脱盐水，降温后硫酸送下游工序处理； (2) 85±10% (mass percentage) of high-temperature sulfuric acid out of the evaporator and a part of the evaporator enters the mixer, lowers the acid concentration with low-pressure feed water, and then enters the reaction tower to absorb SO 3 in the process gas, and the remaining high-temperature sulfuric acid from the evaporator The outlet circulating acid pipeline is connected, first enters the evaporator feed water heater to heat the low-pressure feed water, then enters the evaporative deaerator to remove oxygen and generates low-pressure steam, and finally enters the desalinated preheater, preheats the normal temperature to remove the brine, and cools down. After the sulfuric acid is sent to the downstream process;
(3)外界送入的常温脱盐水，先在脱盐水预热器中加热，之后再送入蒸发除氧器加热，在热力除氧同时产生低压蒸汽，低压蒸汽送反应塔进口与工艺气体中的SO 3反应，蒸发除氧器中的除氧水经低压给水泵加压后，25±15％(质量百分数)的低压给水送混合器降低循环酸浓度，剩余的低压给水送蒸发器给水加热器，加热后再送入蒸发器产生低压蒸汽。 (3) The ambient temperature demineralized water sent by the outside is first heated in the desalinated preheater, then sent to the evaporating deaerator for heating, and the low pressure steam is generated simultaneously with the thermal deaeration, and the low pressure steam is sent to the inlet of the reaction tower and the process gas. After the SO 3 reaction, the deaerated water in the evaporating deaerator is pressurized by the low pressure feed water pump, 25±15% (mass percentage) of the low pressure feed water to the mixer to reduce the circulating acid concentration, and the remaining low pressure feed water is sent to the evaporator feed water heater. After heating, it is sent to the evaporator to generate low pressure steam.
在一些具体的技术方案中：步骤(1)中蒸发除氧器(6)产生的低压蒸汽的压力为0.2±0.1MPa，循环泵(2)出口高温硫酸的温度为190±30℃，蒸发器(3)产生的低压蒸汽压力为0.8±0.4MPa。In some specific technical solutions: the pressure of the low-pressure steam generated by the evaporating deaerator (6) in step (1) is 0.2±0.1 MPa, and the temperature of the high-temperature sulfuric acid at the outlet of the circulation pump (2) is 190±30° C., the evaporator (3) The generated low pressure steam pressure is 0.8 ± 0.4 MPa.
本发明提供的第二种含S0 3气体制酸能量回收装置的技术方案如下： The technical scheme of the second SO 3 -containing acid-making energy recovery device provided by the invention is as follows:
一种含S0 3气体制酸能量回收装置，该装置包括反应塔、蒸发器、蒸发器给水加热器和蒸发除氧器，所述的反应塔的底部通过循环泵与蒸发器相连，蒸发器的一个输出端通过混合器与反应塔的上部相连，蒸发器的另一个输出端分别和蒸发器给水加热器和蒸发除氧器相连，所述蒸发器给水加热器和蒸发除氧器的输出端均与脱盐水预热器相连，含SO 3的工艺气体的输出管道与反应塔的底部相连。 An S3 3 gas sulphuric acid energy recovery device, the device comprising a reaction tower, an evaporator, an evaporator feed water heater and an evaporative deaerator, wherein the bottom of the reaction tower is connected to the evaporator through a circulation pump, and the evaporator One output is connected to the upper portion of the reaction tower through a mixer, and the other output end of the evaporator is connected to the evaporator feed water heater and the evaporating deaerator, respectively, and the output of the evaporator feed water heater and the evaporating deaerator are Connected to the desalted preheater, the output line of the SO 3 containing process gas is connected to the bottom of the reaction column.
在一些具体的技术方案中：脱盐水的输出端通过脱盐水预热器与蒸发除氧器相连，所述的蒸发除氧器底部的一个输出端依次通过低压给水泵、蒸发器给水加热器与蒸发器的输 入端相连，另一个输出端通过低压给水泵与混合器相连。In some specific technical solutions, the output end of the desalinated water is connected to the evaporating deaerator through a desalinating preheater, and an output end of the bottom of the evaporating deaerator is sequentially passed through a low pressure feed pump and an evaporator feed water heater. The input of the evaporator is connected and the other output is connected to the mixer via a low pressure feed pump.
在一些具体的技术方案中：所述的蒸发除氧器顶部的输出端与含SO 3的工艺气体的输出管道相连。 In some specific technical solutions, the output of the top of the evaporating deaerator is connected to an output pipe of a process gas containing SO 3 .
一种利用上述的装置实现能量回收的方法，该方法包括以下步骤：A method for energy recovery using the apparatus described above, the method comprising the steps of:
(1)含SO 3的工艺气体在进入反应塔前，先与蒸发除氧器产生的低压蒸汽按60±40:1的质量比混合，含SO 3的工艺气体中部分或全部SO 3与低压蒸汽反应生成H 2SO 4，所述的工艺气体温度升高后进入反应塔后与上部喷淋下的循环酸继续反应，反应生成的高温硫酸在塔底部汇合后经循环泵加压后送入蒸发器产生低压蒸汽，工艺气体反应后尾气送下一工序处理； (1) The process gas containing SO 3 is mixed with the low-pressure steam produced by the evaporating deaerator at a mass ratio of 60±40:1 before entering the reaction tower, and some or all of the SO 3 and low pressure in the process gas containing SO 3 The steam reacts to generate H 2 SO 4 , and the process gas enters the reaction tower after the temperature rises, and continues to react with the circulating acid under the upper spray, and the high-temperature sulfuric acid formed by the reaction is combined at the bottom of the tower and then pressurized by the circulation pump. The evaporator generates low-pressure steam, and the tail gas is sent to the next process after the reaction of the process gas;
(2)85±10％(质量百分数)的高温硫酸出蒸发器后进入混合器，用低压给水降低酸浓后再进入反应塔循环吸收工艺气体中的SO 3，剩余的高温硫酸再次分为两个部分，60±40％(质量百分数)进入蒸发除氧器热力除氧并产生低压蒸汽，剩余的另一部分部分进入蒸发器给水加热器加热送入低压给水，，从蒸发除氧器和蒸发器给水加热器出来的硫酸进入脱盐水预热器，预热常温脱盐水，降温后硫酸送下游工序处理； (2) 85±10% (mass percentage) of high-temperature sulfuric acid exits the evaporator and enters the mixer. The low-pressure feed water is used to reduce the acid concentration and then enter the reaction tower to absorb the SO 3 in the process gas. The remaining high-temperature sulfuric acid is divided into two again. The part, 60±40% (mass%) enters the evaporative deaerator to remove oxygen and generate low-pressure steam, and the other part enters the evaporator feed water heater to heat the low-pressure feed water, from the evaporative deaerator and the evaporator The sulfuric acid coming out of the feed water heater enters the desalinated preheater, preheating the normal temperature to remove the brine, and after the temperature is lowered, the sulfuric acid is sent to the downstream process for treatment;
(3)外界送入的常温脱盐水，先在脱盐水预热器中加热，之后再送入蒸发除氧器加热，在热力除氧同时产生低压蒸汽，低压蒸汽送反应塔进口管路与工艺气体中的SO 3反应，蒸发除氧器中的除氧水经低压给水泵加压后，25±15％(质量百分数)的低压给水送混合器降低循环酸浓度，剩余部分送蒸发器给水加热器，加热后再送入蒸发器产生低压蒸汽。 (3) The ambient temperature demineralized water sent by the outside is first heated in the desalinated preheater, then sent to the evaporating deaerator for heating, and the low pressure steam is generated simultaneously by the thermal deaeration, and the low pressure steam is sent to the reaction tower inlet line and the process gas. In the SO 3 reaction, after the deaerated water in the evaporating deaerator is pressurized by the low pressure feed water pump, 25±15% (mass percent) of the low pressure feed water is fed to the mixer to reduce the circulating acid concentration, and the remaining part is sent to the evaporator feed water heater. After heating, it is sent to the evaporator to generate low pressure steam.
在一些具体的技术方案中：步骤(1)中蒸发除氧器产生的低压蒸汽的压力为0.15±0.05MPa，循环泵出口高温硫酸的温度为190±30℃，蒸发器产生低压蒸汽的压力为0.8±0.4MPa。In some specific technical solutions, the pressure of the low-pressure steam generated by the evaporating deaerator in step (1) is 0.15±0.05 MPa, the temperature of the high-temperature sulfuric acid at the outlet of the circulating pump is 190±30° C., and the pressure of the evaporator generating low-pressure steam is 0.8 ± 0.4 MPa.
本发明提供的第三种含S0 3气体制酸能量回收装置的技术方案如下： A third aspect of the present invention provides an acid-containing S0 3 gas energy recovery system is as follows:
一种含S0 3气体制酸能量回收装置，该装置包括反应塔、蒸发器、蒸发器给水加热器混合器与反应塔的上部相连，蒸发器的另一个输出端依次与蒸发除氧器和蒸发器给水加热器和脱盐水预热器相连，含SO 3的工艺气体的输出管道与反应塔的底部相连。 An S3 3 gas sulphuric acid energy recovery device, the device comprising a reaction tower, an evaporator, an evaporator feed water heater mixer connected to an upper portion of the reaction tower, and the other output end of the evaporator is sequentially connected with an evaporating deaerator and evaporating The feed water heater is connected to the desalinated preheater, and the output line of the process gas containing SO 3 is connected to the bottom of the reaction tower.
在一些技术方案中：脱盐水的输出端通过脱盐水预热器与蒸发除氧器相连，所述的蒸发除氧器底部的一个输出端通过低压给水泵依次与蒸发器给水加热器和蒸发器相连，另一个输出端通过低压给水泵与混合器相连。In some technical solutions, the output of the desalted water is connected to the evaporating deaerator through a desalinating preheater, and an output end of the bottom of the evaporating deaerator is sequentially passed through the low pressure feed pump and the evaporator feed water heater and the evaporator. Connected, the other output is connected to the mixer via a low pressure feed pump.
在一些具体的技术方案中：所述的蒸发除氧器顶部的输出端与含SO 3的工艺气体的输 出管道相连。 In some specific technical solutions, the output of the top of the evaporating deaerator is connected to an output pipe of a process gas containing SO 3 .
一种利用上述的装置实现含S0 3气体制酸能量回收的方法，该方法包括以步骤： A method for realizing energy recovery of sulphuric acid containing S0 3 gas by using the above device, the method comprising the steps of:
(1)含SO 3的工艺气体在进入反应塔前，先与蒸发除氧器产生的低压蒸汽按60±40:1的质量比混合，含SO 3的工艺气体中部分或全部SO 3与低压蒸汽反应生成H 2SO 4，所述的工艺气体温度升高后进入反应塔后与上部喷淋下的循环酸继续反应，反应生成的高温硫酸在塔底部汇合后经循环泵加压后送入蒸发器产生低压蒸汽，反应后尾气送下一工序处理； (1) The process gas containing SO 3 is mixed with the low-pressure steam produced by the evaporating deaerator at a mass ratio of 60±40:1 before entering the reaction tower, and some or all of the SO 3 and low pressure in the process gas containing SO 3 The steam reacts to generate H 2 SO 4 , and the process gas enters the reaction tower after the temperature rises, and continues to react with the circulating acid under the upper spray, and the high-temperature sulfuric acid formed by the reaction is combined at the bottom of the tower and then pressurized by the circulation pump. The evaporator generates low-pressure steam, and the tail gas is sent to the next process after the reaction;
(2)85+10％(质量百分数)高温硫酸出蒸发器后一部分进入混合器，用低压给水降低酸浓后再进入反应塔循环吸收工艺气体中的SO 3，剩余的高温浓硫酸依次进入蒸发除氧器产生低蒸汽、再进入蒸发器给水加热器加热送入低压给水，在进入脱盐水预热器加热外界送入的脱盐水，降温后硫酸送下游工序处理； (2) 85+10% (mass percentage) high-temperature sulfuric acid exits the evaporator and then enters the mixer. The low-pressure feed water is used to reduce the acid concentration, and then enters the reaction tower to absorb the SO 3 in the process gas. The remaining high-temperature concentrated sulfuric acid enters the evaporation step by step. The deaerator generates low steam, and then enters the evaporator to feed the water heater to feed the low-pressure feed water, and enters the desalted water preheater to heat the demineralized water sent from the outside, and after the temperature is lowered, the sulfuric acid is sent to the downstream process for treatment;
(3)外界送入的常温脱盐水，先在脱盐水预热器中加热，之后再送入蒸发除氧器加热，在热力除氧同时产生低压蒸汽，低压蒸汽送反应塔进口与工艺气体中的SO 3反应，蒸发除氧器中的除氧水经低压给水泵加压后，25±15％(质量百分数)的低压给水送混合器降低循环酸浓度，剩余的低压给水送蒸发器给水加热器，加热后再送入蒸发器产生低压蒸汽。 (3) The ambient temperature demineralized water sent by the outside is first heated in the desalinated preheater, then sent to the evaporating deaerator for heating, and the low pressure steam is generated simultaneously with the thermal deaeration, and the low pressure steam is sent to the inlet of the reaction tower and the process gas. After the SO 3 reaction, the deaerated water in the evaporating deaerator is pressurized by the low pressure feed water pump, 25±15% (mass percentage) of the low pressure feed water to the mixer to reduce the circulating acid concentration, and the remaining low pressure feed water is sent to the evaporator feed water heater. After heating, it is sent to the evaporator to generate low pressure steam.
上述方法中：步骤(1)中蒸发除氧器产生的低压蒸汽的压力为0.15±0.05MPa，环泵出口高温硫酸的温度为190±30℃，，蒸发器产生低压蒸汽的压力为0.8±0.4MPa。In the above method, the pressure of the low-pressure steam generated by the evaporating deaerator in step (1) is 0.15±0.05 MPa, the temperature of the high-temperature sulfuric acid at the outlet of the ring pump is 190±30° C., and the pressure of the low-pressure steam generated by the evaporator is 0.8±0.4. MPa.
本发明技术方案中所述的压力均为表压。The pressures described in the technical solutions of the present invention are all gauge pressures.
本发明的有益效果：The beneficial effects of the invention:
采用本发明所述的含S0 3气体制酸能量回收装置及方法，利用外供硫酸的热量直接产生低压蒸汽，而后送入反应塔前工艺气体管路，替代部分混合器加水，减小混合器的工作负荷，降低了循环酸流量，减少循环泵的电力消耗，更重要的是在不另外消耗能量的情况下，低蒸汽(0.15±0.05MPa(g))的热量转为为高温浓酸(190±30℃)的热量，并通过蒸发器中产生更多更高压力(0.8±0.4MPa(g))的低压蒸汽。可现实低热回收系统每生产1吨硫酸可以副产0.55±0.1吨低压蒸汽。 The use of the present invention containing S0 3 acid gas energy recovery system and method using heat produced directly outside of sulfuric acid for low pressure steam, and then fed into the process gas line prior to the reaction tower, water was added to replace part of the mixer, the mixer is reduced The working load reduces the circulating acid flow, reduces the power consumption of the circulating pump, and more importantly, the low steam (0.15 ± 0.05 MPa (g)) heat is converted to high temperature concentrated acid without additional energy consumption. 190 ± 30 ° C) of heat, and through the evaporator to generate more high pressure (0.8 ± 0.4 MPa (g)) of low pressure steam. It can be realized that the low heat recovery system can produce 0.55±0.1 tons of low pressure steam per ton of sulfuric acid produced.
附图说明DRAWINGS
图1为一种含S0 3气体制酸能量回收装置的示意图。 1 as a schematic S0 3 gas energy recovery system containing an acid.
图2为另一种含S0 3气体制酸能量回收装置的示意图。 FIG 2 is a schematic diagram of another S0 3 gas energy recovery system containing an acid.
图3为第三种含S0 3气体制酸能量回收装置的示意图。 3 is a schematic S0 3 gas energy recovery system of the third containing acid.
其中：1为反应塔，2为循环泵，3为蒸发器，4为混合器，5为蒸发器给水加热器，6为蒸发除氧器，7为脱盐水预热器，8为低压给水泵。Among them: 1 is the reaction tower, 2 is the circulation pump, 3 is the evaporator, 4 is the mixer, 5 is the evaporator feed water heater, 6 is the evaporation deaerator, 7 is the desalinated preheater, 8 is the low pressure feed pump .
具体实施方式detailed description
下面结合实施例对本发明做进一步说明，但本发明的保护范围不限于此：技术方案：The present invention will be further described below in conjunction with the embodiments, but the scope of protection of the present invention is not limited thereto:
如图1，一种含S0 3气体制酸能量回收装置，该装置包括反应塔(1)、蒸发器(3)和蒸发除氧器(6)，所述的反应塔(1)的底部通过循环泵(2)与蒸发器(3)相连，所述的蒸发器(3)的一个输出端通过混合器(4)与反应塔(1)的上部相连，所述的蒸发器(3)的另一个输出端依次通过蒸发器给水加热器(5)、蒸发除氧器(6)和脱盐水预热器(7)相连，含SO 3的工艺气体的输出管道与反应塔(1)的底部相连。 1, S0 3 containing acid gas energy recovery system, the apparatus comprising a reaction column (1), an evaporator (3) and evaporated deaerator (6), the bottom of the reaction column (1) by a circulation pump (2) is connected to the evaporator (3), and an output end of the evaporator (3) is connected to an upper portion of the reaction column (1) through a mixer (4), the evaporator (3) The other output is connected in series through the evaporator feed water heater (5), the evaporative deaerator (6) and the desalinated preheater (7), the output line of the process gas containing SO 3 and the bottom of the reaction tower (1). Connected.
脱盐水的输出端通过脱盐水预热器(7)与蒸发除氧器(6)相连，所述的蒸发除氧器(6)底部的一个输出端通过低压给水泵(8)依次与蒸发器给水加热器(5)与蒸发器(3)的输入端相连，另一个输出端通过低压给水泵(8)与混合器(4)相连。The output of the desalted water is connected to the evaporating deaerator (6) through a desalted water preheater (7), and an output end of the evaporating deaerator (6) is sequentially passed through the low pressure feed pump (8) with the evaporator. The feedwater heater (5) is connected to the input of the evaporator (3) and the other output is connected to the mixer (4) via a low pressure feed pump (8).
所述的蒸发除氧器(6)顶部的输出端与含SO 3的工艺气体的输出管道相连。 The output of the evaporator top deaerator (6) and the output duct of the process gas containing SO 3 is connected.
利用图1所示的装置实现含S0 3气体制酸能量回收方法，具体如实施例1-1，1-2，1-3。 1 using the apparatus shown in FIG achieve S0 3 gas energy recovery system of an acid-containing, particularly as in Example 1-1, 1-2.
实施例1-1Example 1-1
含SO 3的工艺气体在进入反应塔(1)前，先与蒸发除氧器(6)产生的0.1MPa(g)低压蒸汽按30:1的质量比混合，工艺气体中部分SO 3与低压蒸汽反应生成硫酸工艺气体温度升高，工艺气体温升为40℃，进入反应塔(1)后工艺气体与上部喷淋下的循环酸继续反应，反应生成200℃的高温硫酸在塔底部汇合后经循环泵(2)加压后送入蒸发器(3)产生0.6MPa(g)的低压蒸汽，反应后尾气送下一工序处理。 The process gas containing SO 3 is mixed with 0.1 MPa (g) of low pressure steam produced by the evaporating deaerator (6) in a mass ratio of 30:1 before entering the reaction column (1), and some SO 3 and low pressure in the process gas. The temperature of the sulfuric acid formed by the steam reaction increases, and the temperature of the process gas rises to 40 ° C. After entering the reaction column (1), the process gas continues to react with the circulating acid under the upper spray, and the reaction forms a high temperature sulfuric acid of 200 ° C after confluence at the bottom of the column. After being pressurized by the circulation pump (2), it is sent to the evaporator (3) to generate 0.6 MPa (g) of low-pressure steam, and after the reaction, the tail gas is sent to the next process.
80％(质量百分数)的高温硫酸出蒸发器(3)后进入混合器(4)，用低压给水降低酸浓后再进入反应塔(1)循环吸收工艺气体中的SO 3，剩余部分的高温硫酸从蒸发器(3)出口循环酸管路上接出，先进入蒸发器给水加热器(5)加热送入低压给水，再进入蒸发除氧器(6)热力除氧并产生低压蒸汽0.1MPa，最后进入脱盐水预热器，预热常温脱盐水，外供硫酸温度下降至105℃送下游工序处理。 80% (mass percentage) of high-temperature sulfuric acid exits the evaporator (3) and then enters the mixer (4). The low-pressure feed water is used to reduce the acid concentration and then enter the reaction column (1) to absorb the SO 3 in the process gas, and the remaining part of the high temperature. Sulfuric acid is taken from the outlet acid pipeline of the evaporator (3) outlet, first enters the evaporator feed water heater (5) and is heated to the low-pressure feed water, and then enters the evaporating deaerator (6) to remove oxygen and generate low-pressure steam 0.1MPa. Finally, the demineralized water preheater is introduced, the salt water is preheated at normal temperature, and the temperature of the external sulfuric acid is lowered to 105 ° C to be sent to the downstream process.
外界送入的常温脱盐水，先在脱盐水预热器(7)中加热至100℃，再送入蒸发除氧器(6)，加热至120℃，热力除氧同时产生0.1MP(g)低压蒸汽，低压蒸汽送反应塔(1)进口与工艺气体中的SO 3反应，蒸发除氧器(6)中的除氧水经低压给水泵(8)加压后， 10％(质量百分数)的低压给水送混合器(4)降低循环酸浓度，剩余的送蒸发器给水加热器(5)，加热至160℃，在送入蒸发器产生0.6MPa的低压蒸汽。 The ambient temperature demineralized water sent by the outside is first heated to 100 ° C in the desalted water preheater (7), then sent to the evaporating deaerator (6), heated to 120 ° C, and the thermal deaeration simultaneously produces 0.1 MP (g) low pressure. Steam, low pressure steam is sent to the reaction tower (1) inlet and reacted with SO 3 in the process gas, and the deaerated water in the evaporating deaerator (6) is pressurized by the low pressure feed pump (8), 10% (mass percentage) The low pressure feed water supply mixer (4) reduces the circulating acid concentration, and the remaining evaporator feed water heater (5) is heated to 160 ° C and sent to the evaporator to produce 0.6 MPa of low pressure steam.
采用本技术方案较现有技术外供硫酸温度显著降低，可实现每吨硫酸副产0.595吨低压蒸汽。Compared with the prior art, the temperature of the sulfuric acid is significantly reduced, and the low-pressure steam of 0.595 tons per ton of sulfuric acid by-product can be realized.
实施例1-2Example 1-2
含SO 3的工艺气体在进入反应塔(1)前，先与蒸发除氧器(6)产生的0.15MPa(g)低压蒸汽按50:1的质量比混合，工艺气体中部分SO 3与低压蒸汽反应生成硫酸工艺气体温度升高，工艺气体温升为55℃，进入反应塔(1)后工艺气体与上部喷淋下的循环酸继续反应，反应生成210℃的高温硫酸在塔底部汇合后经循环泵(2)加压后送入蒸发器(3)产生0.8MPa(g)的低压蒸汽，反应后尾气送下一工序处理。 The SO 3 -containing process gas is mixed with 0.15 MPa (g) of low-pressure steam produced by the evaporating deaerator (6) at a mass ratio of 50:1 before entering the reaction column (1). Part of the process gas contains SO 3 and low pressure. The temperature of the sulfuric acid process gas is increased by steam reaction, and the temperature of the process gas is raised to 55 ° C. After entering the reaction column (1), the process gas continues to react with the circulating acid under the upper spray, and the reaction produces a high temperature sulfuric acid of 210 ° C after confluence at the bottom of the column. After being pressurized by the circulation pump (2), it is sent to the evaporator (3) to generate low pressure steam of 0.8 MPa (g), and the tail gas is sent to the next process after the reaction.
85％(质量百分数)的高温硫酸出蒸发器(3)后大部分进入混合器(4)，用低压给水降低酸浓后再进入反应塔(1)循环吸收工艺气体中的SO 3，剩余的高温硫酸从蒸发器出口循环酸管路上接出，先进入蒸发器给水加热器(5)加热送入低压给水，再进入蒸发除氧器(6)热力除氧并产生低压蒸汽0.15MPa，最后进入脱盐水预热器，预热常温脱盐水，外供硫酸温度下降至115℃送下游工序处理。 85% (mass percent) of high-temperature sulfuric acid exits the evaporator (3) and mostly enters the mixer (4), lowers the acid concentration with low-pressure feed water, and then enters the reaction tower (1) to absorb the SO 3 in the process gas, and the remaining The high-temperature sulfuric acid is taken out from the outlet acid circuit of the evaporator outlet, first enters the evaporator feed water heater (5) and is heated to the low-pressure feed water, and then enters the evaporating deaerator (6) to remove oxygen and generate low-pressure steam 0.15MPa, and finally enters The desalinated preheater is preheated to remove salt water at normal temperature, and the temperature of the external sulfuric acid is lowered to 115 ° C for downstream processing.
外界送入的常温脱盐水，先在脱盐水预热器(7)中加热至110℃，再送入蒸发除氧器(6)，加热至127℃，热力除氧同时产生0.15MP低压蒸汽，低压蒸汽送反应塔(1)进口与工艺气体中的SO 3反应，蒸发除氧器(6)中的除氧水经低压给水泵(8)加压后，20％(质量百分数)的低压给水送混合器(4)降低循环酸浓度，剩余部分送蒸发器给水加热器(5)，加热至170℃，在送入蒸发器产生0.8MPa的低压蒸汽。 The ambient temperature demineralized water sent by the outside is first heated to 110 ° C in the desalted water preheater (7), then sent to the evaporating deaerator (6), heated to 127 ° C, and the heat deoxidation simultaneously generates 0.15 MP low pressure steam, low pressure. The steam is sent to the reaction tower (1) and reacted with SO 3 in the process gas. After the deaerated water in the evaporating deaerator (6) is pressurized by the low pressure feed pump (8), 20% (mass percent) of the low pressure feed water is sent. The mixer (4) reduces the circulating acid concentration, and the remainder is sent to the evaporator feed water heater (5), heated to 170 ° C, and sent to the evaporator to produce 0.8 MPa of low pressure steam.
采用本技术方案较现有技术外供硫酸温度显著降低，可实现每吨硫酸副产0.584吨低压蒸汽。Compared with the prior art, the temperature of the sulfuric acid is significantly reduced, and the low-pressure steam of 0.584 tons per ton of sulfuric acid by-product can be realized.
实施例1-3Examples 1-3
含SO 3的工艺气体在进入反应塔(1)前，先与蒸发除氧器(6)产生的0.2MPa(g)低压蒸汽按90:1的质量比混合，工艺气体中部分SO 3与低压蒸汽反应生成H 2SO工艺气体温度升高，工艺气体温升为70℃，进入反应塔(1)后工艺气体与上部喷淋下的循环酸继续反应，反应生成220℃的高温硫酸在塔底部汇合后经循环泵(2)加压后送入蒸发器(3)产生1.2MPa(g)的低压蒸汽，反应后尾气送下一工序处理。 The process gas containing SO 3 is mixed with 0.2 MPa (g) of low pressure steam generated by the evaporating deaerator (6) at a mass ratio of 90:1 before entering the reaction column (1), and some SO 3 and low pressure in the process gas. The steam reaction generates H 2 SO process gas temperature rise, the process gas temperature rise is 70 ° C, after entering the reaction tower (1), the process gas continues to react with the circulating acid under the upper spray, and the reaction generates 220 ° C high temperature sulfuric acid at the bottom of the tower. After the combination, it is pressurized by the circulating pump (2) and sent to the evaporator (3) to generate 1.2 MPa (g) of low-pressure steam. After the reaction, the tail gas is sent to the next process.
95％(质量百分数)的高温硫酸出蒸发器(3)后混合器(4)，用低压给水降低酸浓后再进入反应塔(1)循环吸收工艺气体中的SO 3，剩余的高温硫酸从蒸发器出口循环酸管路上接出，先进入蒸发器给水加热器(5)加热送入低压给水，再进入蒸发除氧器(6)热力除氧并产生低压蒸汽0.2MPa，最后进入脱盐水预热器，预热常温脱盐水，外供硫酸温度下降至130℃送下游工序处理。 95% (mass percent) of high-temperature sulfuric acid out of the evaporator (3) after the mixer (4), with low-pressure feed water to reduce acid concentration and then into the reaction tower (1) to recycle the SO 3 in the process gas, the remaining high-temperature sulfuric acid from The evaporator outlet is connected to the circulating acid line, first enters the evaporator feed water heater (5) and is heated to the low-pressure feed water, and then enters the evaporating deaerator (6) to remove oxygen and generate low-pressure steam 0.2MPa, and finally enters the desalinated water preheating. The heat exchanger is preheated to remove salt water at normal temperature, and the temperature of the external sulfuric acid is lowered to 130 ° C to be sent to the downstream process.
外界送入的常温脱盐水，先在脱盐水预热器(7)中加热至120℃，再送入蒸发除氧器(6)，加热至133℃，热力除氧同时产生0.2MP(g)低压蒸汽，低压蒸汽送反应塔(1)进口与工艺气体中的SO 3反应，蒸发除氧器(6)中的除氧水经低压给水泵(8)加压后，40％(质量百分数)的低压给水送混合器(4)降低循环酸浓度，剩余部分送蒸发器给水加热器(5)，加热至185℃，在送入蒸发器产生1.2MPa的低压蒸汽。 The normal temperature demineralized water sent from the outside is first heated to 120 ° C in the desalinated preheater (7), then sent to the evaporating deaerator (6), heated to 133 ° C, and the thermal deaeration simultaneously produces 0.2 MP (g) low pressure. Steam, low pressure steam is sent to the reaction tower (1) inlet and reacted with SO 3 in the process gas, and the deaerated water in the evaporating deaerator (6) is pressurized by the low pressure feed pump (8), 40% (mass percentage) The low pressure feed water mixer (4) reduces the circulating acid concentration, and the remainder is sent to the evaporator feed water heater (5), heated to 185 ° C, and sent to the evaporator to produce 1.2 MPa of low pressure steam.
采用本技术方案较现有技术外供硫酸温度显著降低，可实现每吨硫酸副产0.578吨低压蒸汽。Compared with the prior art, the temperature of the sulfuric acid is significantly reduced, and the low-pressure steam of 0.578 tons per ton of sulfuric acid by-product can be realized.
如图2，一种含S0 3气体制酸能量回收装置，该装置包括反应塔(1)、蒸发器(3)、蒸发器给水加热器(5)和蒸发除氧器(6)，所述的反应塔(1)的底部通过循环泵(2)与蒸发器(3)相连，蒸发器(3)的一个输出端通过混合器(4)与反应塔(1)的上部相连，蒸发器(3)的另一个输出端分别和蒸发器给水加热器(5)和蒸发除氧器(6)相连，所述蒸发器给水加热器(5)和蒸发除氧器(6)的输出端均与脱盐水预热器(7)相连，含SO 3的工艺气体的输出管道与反应塔(1)的底部相连。外界脱盐水端通过脱盐水预热器(7)与蒸发除氧器(6)相连，所述的蒸发除氧器(6)底部的一个输出端通过低压给水泵(8)依次与蒸发器给水加热器(5)与蒸发器(3)的输入端相连，另一个输出端通过低压给水泵(8)与混合器(4)相连。所述的蒸发除氧器(6)顶部的输出端与含SO 3的工艺气体的输出管道相连。 2, S0 3 containing acid gas energy recovery system, the apparatus comprising a reaction column (1), an evaporator (3), an evaporator feedwater heater (5) and evaporated deaerator (6), the The bottom of the reaction column (1) is connected to the evaporator (3) through a circulation pump (2), and an output end of the evaporator (3) is connected to the upper portion of the reaction column (1) through a mixer (4), and the evaporator ( The other output of 3) is connected to the evaporator feed water heater (5) and the evaporative deaerator (6), respectively, and the output of the evaporator feed water heater (5) and the evaporating deaerator (6) are The desalted water preheater (7) is connected, and the output pipe of the SO 3 containing process gas is connected to the bottom of the reaction column (1). The external desalted water end is connected to the evaporating deaerator (6) through a desalted water preheater (7), and an output end of the bottom of the evaporating deaerator (6) is sequentially supplied with water through the low pressure feed pump (8) The heater (5) is connected to the input of the evaporator (3) and the other output is connected to the mixer (4) via a low pressure feed pump (8). The output of the evaporator top deaerator (6) and the output duct of the process gas containing SO 3 is connected.
实施例2-1Example 2-1
含SO 3的工艺气体在进入反应塔(1)前，先与蒸发除氧器(6)产生的0.1MPa(g)低压蒸汽按照质量比为30:1混合，工艺气体中部分SO 3与低压蒸汽反应生成硫酸工艺气体温度升高，工艺气体温升为40℃，进入反应塔(1)后工艺气体与上部喷淋下的循环酸继续反应，反应生成200℃的高温硫酸在塔底部汇合后经循环泵(2)加压后送入蒸发器(3)产生0.6MPa(g)的低压蒸汽，反应后尾气送下一工序处理。 The process gas containing SO 3 is mixed with 0.1 MPa (g) of low pressure steam produced by the evaporating deaerator (6) at a mass ratio of 30:1 before entering the reaction column (1), and some SO 3 and low pressure in the process gas. The temperature of the sulfuric acid formed by the steam reaction increases, and the temperature of the process gas rises to 40 ° C. After entering the reaction column (1), the process gas continues to react with the circulating acid under the upper spray, and the reaction forms a high temperature sulfuric acid of 200 ° C after confluence at the bottom of the column. After being pressurized by the circulation pump (2), it is sent to the evaporator (3) to generate 0.6 MPa (g) of low-pressure steam, and after the reaction, the tail gas is sent to the next process.
75％(质量百分数)的高温硫酸出蒸发器(3)后进入混合器(4)，用低压给水降低 酸浓度后再进入反应塔(1)循环吸收工艺气体中的SO 3，剩余的高温硫酸从蒸发器出口循环酸管路上接出，再分为两个部分，40％(质量百分数)进入蒸发器给水加热器(5)加热送入低压给水，60％(质量百分数)进入蒸发除氧器(6)热力除氧并产生低压蒸汽0.1MPa，高温浓硫酸出蒸发器给水加热器(5)和蒸发除氧器(6)后均与进入脱盐水预热器，预热常温脱盐水，外供硫酸温度下降至100℃送下游工序处理。 75% (mass percent) of high-temperature sulfuric acid exits the evaporator (3) and then enters the mixer (4). After lowering the acid concentration with low-pressure feed water, it enters the reaction tower (1) to recycle the SO 3 in the process gas, and the remaining high-temperature sulfuric acid. It is taken out from the outlet acid circuit of the evaporator outlet and divided into two parts. 40% (mass percent) enters the evaporator feed water heater (5) and is heated to the low pressure feed water, and 60% (mass percent) enters the evaporative deaerator. (6) Thermal deaeration and generating low pressure steam 0.1MPa, high temperature concentrated sulfuric acid out of the evaporator feed water heater (5) and evaporative deaerator (6) are both entering the desalinated preheater, preheating the normal temperature desalinated water, outside The sulfuric acid temperature is lowered to 100 ° C and sent to the downstream process.
外界送入的常温脱盐水，先在脱盐水预热器(7)中加热至95℃，再送入蒸发除氧器(6)，加热至120℃，热力除氧同时产生0.1MP低压蒸汽，低压蒸汽送反应塔(1)进口与工艺气体中的SO 3反应，蒸发除氧器(6)中的除氧水经低压给水泵(8)加压后，10％(质量百分数)的低压给水送混合器(4)降低循环酸浓度，剩余部分送蒸发器给水加热器(5)，加热至158℃，在送入蒸发器产生0.6MPa的低压蒸汽。 The normal temperature demineralized water sent from the outside is first heated to 95 ° C in the desalted water preheater (7), then sent to the evaporating deaerator (6), heated to 120 ° C, and the heat deoxidation simultaneously generates 0.1 MP low pressure steam, low pressure The steam is sent to the reaction tower (1) and reacted with SO 3 in the process gas. After the deaerated water in the evaporating deaerator (6) is pressurized by the low pressure feed pump (8), 10% (mass percent) of the low pressure feed water is sent. The mixer (4) reduces the circulating acid concentration, and the remainder is sent to the evaporator feed water heater (5), heated to 158 ° C, and sent to the evaporator to produce 0.6 MPa of low pressure steam.
采用本技术方案较现有技术外供硫酸温度显著降低，可实现每吨硫酸副产0.632吨低压蒸汽。Compared with the prior art, the temperature of the sulfuric acid is significantly reduced, and the low-pressure steam of 0.632 tons per ton of sulfuric acid by-product can be realized.
实施例2-2Example 2-2
含SO 3的工艺气体在进入反应塔(1)前，先与蒸发除氧器(6)产生的0.15MPa低压蒸汽按50:1的质量比混合，工艺气体中部分SO 3与低压蒸汽反应生成硫酸工艺气体温度升高，工艺气体温度升为55℃，进入反应塔(1)后工艺气体与上部喷淋下的循环酸继续反应，反应生成210℃的高温硫酸在塔底部汇合后经循环泵(2)加压后送入蒸发器(3)产生0.8MPa的低压蒸汽，反应后尾气送下一工序处理。 The process gas containing SO 3 is mixed with 0.15 MPa of low pressure steam produced by the evaporating deaerator (6) at a mass ratio of 50:1 before entering the reaction column (1), and some SO 3 in the process gas is reacted with low pressure steam to form The temperature of the sulfuric acid process gas rises, and the temperature of the process gas rises to 55 ° C. After entering the reaction column (1), the process gas continues to react with the circulating acid under the upper spray, and the reaction produces a high temperature sulfuric acid of 210 ° C, which is merged at the bottom of the column and then passed through a circulation pump. (2) After being pressurized, it is sent to the evaporator (3) to generate low-pressure steam of 0.8 MPa, and the tail gas is sent to the next process after the reaction.
85％(质量百分数)的高温硫酸出蒸发器(3)后进入混合器(4)，用低压给水降低酸浓度后再进入反应塔(1)循环吸收工艺气体中的SO 3，剩余的高温硫酸从蒸发器出口循环酸管路上接出，再分为两个部分，40％(质量百分数)进入蒸发器给水加热器(5)加热送入低压给水，60％(质量百分数)进入蒸发除氧器(6)热力除氧并产生低压蒸汽0.15MPa，高温浓酸出蒸发器给水加热器(5)和蒸发除氧器(6)后均与进入脱盐水预热器，预热常温脱盐水，外供硫酸温度下降至111℃送下游工序处理。 85% (mass percent) of high-temperature sulfuric acid exits the evaporator (3) and enters the mixer (4). After lowering the acid concentration with low-pressure feed water, it enters the reaction tower (1) to absorb SO 3 in the process gas, and the remaining high-temperature sulfuric acid. It is taken out from the outlet acid circuit of the evaporator outlet and divided into two parts. 40% (mass percent) enters the evaporator feed water heater (5) and is heated to the low pressure feed water, and 60% (mass percent) enters the evaporative deaerator. (6) Thermal deaeration and generating low pressure steam 0.15MPa, high temperature concentrated acid out of the evaporator feed water heater (5) and evaporative deaerator (6) are both entering the desalinated preheater, preheating the normal temperature to remove the brine, outside The sulfuric acid temperature is lowered to 111 ° C and sent to the downstream process.
外界送入的常温脱盐水，先在脱盐水预热器(7)中加热至98℃，再送入蒸发除氧器(6)，加热至127℃，热力除氧同时产生0.15MP低压蒸汽，低压蒸汽送反应塔(1)进口与工艺气体中的SO 3反应，蒸发除氧器(6)中的除氧水经低压给水泵(8)加压后，20％(质量百分数)的低压给水送混合器(4)降低循环酸浓度，剩余部分送蒸发器给水加热器(5)，加热至163℃，再送入蒸发器产生0.8MPa的低压蒸汽。 The ambient temperature demineralized water sent by the outside is first heated to 98 ° C in the desalted water preheater (7), then sent to the evaporating deaerator (6), heated to 127 ° C, and the heat deoxidation simultaneously generates 0.15 MP low pressure steam, low pressure The steam is sent to the reaction tower (1) and reacted with SO 3 in the process gas. After the deaerated water in the evaporating deaerator (6) is pressurized by the low pressure feed pump (8), 20% (mass percent) of the low pressure feed water is sent. The mixer (4) reduces the circulating acid concentration, and the remainder is sent to the evaporator feed water heater (5), heated to 163 ° C, and sent to the evaporator to produce 0.8 MPa of low pressure steam.
采用本技术方案较现有技术外供硫酸温度显著降低，可实现每吨硫酸副产0.625吨低压蒸汽。Compared with the prior art, the temperature of the sulfuric acid is significantly reduced, and the low-pressure steam of 0.625 tons per ton of sulfuric acid by-product can be realized.
实施例2-3Example 2-3
含SO 3的工艺气体在进入反应塔(1)前，先与蒸发除氧器(6)产生的0.2MPa(g)低压蒸汽按照质量比为90:1混合，工艺气体中部分SO 3与低压蒸汽反应生成硫酸工艺气体温度升高，工艺气体温升为70℃，进入反应塔(1)后工艺气体与上部喷淋下的循环酸继续反应，反应生成220℃的高温硫酸在塔底部汇合后经循环泵(2)加压后送入蒸发器(3)产生1.2MPa(g)的低压蒸汽，反应后尾气送下一工序处理。 The process gas containing SO 3 is mixed with 0.2 MPa (g) of low pressure steam produced by the evaporating deaerator (6) at a mass ratio of 90:1 before entering the reaction column (1), and some SO 3 and low pressure in the process gas. The temperature of the sulfuric acid process gas is increased by steam reaction, and the temperature of the process gas is increased to 70 ° C. After entering the reaction column (1), the process gas continues to react with the circulating acid under the upper spray, and the reaction forms a high temperature sulfuric acid of 220 ° C after confluence at the bottom of the tower. After being pressurized by the circulation pump (2), it is sent to the evaporator (3) to generate 1.2 MPa (g) of low-pressure steam. After the reaction, the tail gas is sent to the next process.
95％(质量百分数)的高温硫酸出蒸发器(3)后进入混合器(4)，用低压给水降低酸浓后再进入反应塔(1)循环吸收工艺气体中的SO 3，剩余的高温硫酸从蒸发器出口循环酸管路上接出，再分为两个部分，40％(质量百分数)进入蒸发器给水加热器(5)加热送入低压给水，60％(质量百分数)进入蒸发除氧器(6)热力除氧并产生低压蒸汽0.15MPa，高温浓硫酸出蒸发器给水加热器(5)和蒸发除氧器(6)后均与进入脱盐水预热器，预热常温脱盐水，外供硫酸温度下降至124℃送下游工序处理。 95% (mass percent) of high-temperature sulfuric acid exits the evaporator (3) and then enters the mixer (4). The low-pressure feed water is used to reduce the acid concentration and then enter the reaction column (1) to absorb the SO 3 in the process gas, and the remaining high-temperature sulfuric acid. It is taken out from the outlet acid circuit of the evaporator outlet and divided into two parts. 40% (mass percent) enters the evaporator feed water heater (5) and is heated to the low pressure feed water, and 60% (mass percent) enters the evaporative deaerator. (6) Thermal deaeration and generation of low pressure steam 0.15MPa, high temperature concentrated sulfuric acid out of the evaporator feed water heater (5) and evaporative deaerator (6) are both entering the desalinated preheater, preheating the normal temperature to remove the brine, outside The temperature of the sulfuric acid is lowered to 124 ° C and sent to the downstream process.
外界送入的常温脱盐水，先在脱盐水预热器(7)中加热至107℃，再送入蒸发除氧器(6)，加热至133℃，热力除氧同时产生0.2MP(g)低压蒸汽，低压蒸汽送反应塔(1)进口与工艺气体中的SO 3反应，蒸发除氧器(6)中的除氧水经低压给水泵(8)加压后，40％(质量百分数)的低压给水送混合器(4)降低循环酸浓度，剩余部分送蒸发器给水加热器(5)，加热至176℃，在送入蒸发器产生1.2MPa的低压蒸汽。 The normal temperature demineralized water sent from the outside is first heated to 107 ° C in the desalinated preheater (7), then sent to the evaporating deaerator (6), heated to 133 ° C, and deactivated by heat to generate 0.2 MP (g) low pressure. Steam, low pressure steam is sent to the reaction tower (1) inlet and reacted with SO 3 in the process gas, and the deaerated water in the evaporating deaerator (6) is pressurized by the low pressure feed pump (8), 40% (mass percentage) The low pressure feed water mixer (4) reduces the circulating acid concentration, and the remainder is sent to the evaporator feed water heater (5), heated to 176 ° C, and sent to the evaporator to produce 1.2 MPa of low pressure steam.
采用本技术方案较现有技术外供硫酸温度显著降低，可实现每吨硫酸副产0.608吨低压蒸汽。Compared with the prior art, the temperature of the sulfuric acid is significantly reduced, and the low-pressure steam of 0.608 tons per ton of sulfuric acid by-product can be realized.
如图3，一种含S0 3气体制酸能量回收装置，该装置包括反应塔(1)、蒸发器(3)、蒸发器给水加热器(5)和蒸发除氧器(6)，所述的反应塔(1)的底部通过循环泵(2)与蒸发器(3)相连，蒸发器(3)的一个输出端通过混合器(4)与反应塔(1)的上部相连，蒸发器(3)的另一个输出端依次与蒸发除氧器(6)、蒸发器给水加热器(5)相连和脱盐水预热器(7)相连，含SO 3的工艺气体的输出管道与反应塔(1)的底部相连。脱盐水的输入端通过脱盐水预热器(7)与蒸发除氧器(6)相连，所述的蒸发除氧器(6)底部的一个输出端通过低压给水泵(8)依次与蒸发器给水加热器(5)与蒸发器(3)的输 入端相连，另一个输出端通过低压给水泵(8)与混合器(4)相连。所述的蒸发除氧器(6)顶部的输出端与含SO 3的工艺气体的输出管道相连。 3, S0 3 containing acid gas energy recovery system, the apparatus comprising a reaction column (1), an evaporator (3), an evaporator feedwater heater (5) and evaporated deaerator (6), the The bottom of the reaction column (1) is connected to the evaporator (3) through a circulation pump (2), and an output end of the evaporator (3) is connected to the upper portion of the reaction column (1) through a mixer (4), and the evaporator ( The other output of 3) is connected to the evaporating deaerator (6), the evaporator feed water heater (5) and the desalinated preheater (7) in sequence, and the output pipe and reaction tower of the process gas containing SO 3 ( 1) The bottom is connected. The input end of the desalted water is connected to the evaporating deaerator (6) through a desalted preheater (7), and an output end of the bottom of the evaporating deaerator (6) is sequentially passed through the low pressure feed pump (8) with the evaporator The feedwater heater (5) is connected to the input of the evaporator (3) and the other output is connected to the mixer (4) via a low pressure feed pump (8). The output of the evaporator top deaerator (6) and the output duct of the process gas containing SO 3 is connected.
实施例3-1Example 3-1
含SO 3的工艺气体在进入反应塔(1)前，先与蒸发除氧器(6)产生的0.1MPa(g)低压蒸汽按质量比30:1混合，工艺气体中部分SO 3与低压蒸汽反应生成硫酸工艺气体温度升高，工艺气体温升为40℃，进入反应塔(1)后工艺气体与上部喷淋下的循环酸继续反应，反应生成200℃的高温硫酸在塔底部汇合后经循环泵(2)加压后送入蒸发器(3)产生0.6MPa(g)的低压蒸汽，反应后尾气送下一工序处理。 The process gas containing SO 3 is mixed with 0.1 MPa (g) of low pressure steam produced by the evaporating deaerator (6) at a mass ratio of 30:1 before entering the reaction column (1), and part of the SO 3 and low pressure steam in the process gas. The temperature of the sulfuric acid produced by the reaction is increased, and the temperature of the process gas is raised to 40 ° C. After entering the reaction column (1), the process gas continues to react with the circulating acid under the upper spray, and the reaction produces a high temperature sulfuric acid at 200 ° C. The circulating pump (2) is pressurized and sent to the evaporator (3) to generate 0.6 MPa (g) of low pressure steam. After the reaction, the tail gas is sent to the next process.
75％(质量百分数)的高温硫酸出蒸发器(3)后进入混合器(4)，用低压给水降低酸浓后再进入反应塔(1)循环吸收工艺气体中的SO 3，剩余的高温硫酸从蒸发器出口循环酸管路上接出，先进入蒸发除氧器(6)热力除氧并产生低压蒸汽0.1MPa，再进入蒸发器给水加热器(5)加热送入低压给水，最后进入脱盐水预热器，预热常温脱盐水，外供硫酸温度下降至100℃送下游工序处理。 75% (mass percent) of high-temperature sulfuric acid exits the evaporator (3) and enters the mixer (4). The low-pressure feed water is used to reduce the acid concentration and then enter the reaction column (1) to absorb the SO 3 in the process gas, and the remaining high-temperature sulfuric acid. From the outlet of the evaporator outlet acid pipeline, first enter the evaporation deaerator (6) thermal deaeration and generate low pressure steam 0.1MPa, then enter the evaporator feed water heater (5) heated to send low pressure feed water, and finally into the desalinated water The preheater is preheated to remove salt water at normal temperature, and the temperature of the external sulfuric acid is lowered to 100 ° C to be sent to the downstream process.
外界送入的常温脱盐水，先在脱盐水预热器(7)中加热至98℃，再送入蒸发除氧器(6)，加热至120℃，热力除氧同时产生0.1MP(g)低压蒸汽，低压蒸汽送反应塔(1)进口与工艺气体中的SO 3反应，蒸发除氧器(6)中的除氧水经低压给水泵(8)加压后，10％(质量百分数)的低压给水送混合器(4)降低循环酸浓度，剩余部分送蒸发器给水加热器(5)，加热至150℃，在送入蒸发器产生0.6MPa的低压蒸汽。 The normal temperature demineralized water sent from the outside is first heated to 98 ° C in the desalted water preheater (7), then sent to the evaporating deaerator (6), heated to 120 ° C, and the thermal deaeration simultaneously produces 0.1 MP (g) low pressure. Steam, low pressure steam is sent to the reaction tower (1) inlet and reacted with SO 3 in the process gas, and the deaerated water in the evaporating deaerator (6) is pressurized by the low pressure feed pump (8), 10% (mass percentage) The low pressure feed water mixer (4) reduces the circulating acid concentration, and the remainder is sent to the evaporator feed water heater (5), heated to 150 ° C, and sent to the evaporator to produce 0.6 MPa of low pressure steam.
采用本技术方案较现有技术外供硫酸温度显著降低，可实现每吨硫酸副产0.615吨低压蒸汽。Compared with the prior art, the temperature of the sulfuric acid is significantly reduced, and the low-pressure steam of 0.615 tons per ton of sulfuric acid by-product can be realized.
实施例3-2Example 3-2
含SO 3的工艺气体在进入反应塔(1)前，先与蒸发除氧器(6)产生的0.15MPa(g)低压蒸汽按照质量比50:1混合，工艺气体中部分SO 3与低压蒸汽反应生成H 2SO工艺气体温度升高，工艺气体温升为55℃，进入反应塔(1)后工艺气体与上部喷淋下的循环酸继续反应，反应生成210℃的高温硫酸在塔底部汇合后经循环泵(2)加压后送入蒸发器(3)产生0.8MPa(g)的低压蒸汽，反应后尾气送下一工序处理。 The process gas containing SO 3 is mixed with 0.15 MPa (g) of low pressure steam produced by the evaporating deaerator (6) at a mass ratio of 50:1 before entering the reaction column (1), and part of the SO 3 and low pressure steam in the process gas. The reaction generates H 2 SO process gas temperature rise, the process gas temperature rise is 55 ° C, after entering the reaction tower (1), the process gas continues to react with the circulating acid under the upper spray, and the reaction produces 210 ° C high temperature sulfuric acid at the bottom of the tower. After being pressurized by the circulation pump (2), it is sent to the evaporator (3) to generate 0.8 MPa (g) of low-pressure steam. After the reaction, the tail gas is sent to the next process.
85％(质量百分数)的高温硫酸出蒸发器(3)后大部分进入混合器(4)，用低压给水降低酸浓度后再进入反应塔(1)循环吸收工艺气体中的SO 3，剩余的高温硫酸从蒸发器出口循环酸管路上接出，先进入蒸发除氧器(6)热力除氧并产生低压蒸汽0.15MPa(g)， 再进入蒸发器给水加热器(5)加热送入低压给水，最后进入脱盐水预热器，预热常温脱盐水，外供硫酸温度下降至108℃送下游工序处理。 85% (mass percent) of high-temperature sulfuric acid exits the evaporator (3) and mostly enters the mixer (4). After lowering the acid concentration with low-pressure feed water, it enters the reaction tower (1) to absorb SO 3 in the process gas, and the remaining The high-temperature sulfuric acid is taken out from the outlet acid circuit of the evaporator outlet, first enters the evaporating deaerator (6) to remove oxygen and generate low-pressure steam of 0.15 MPa (g), and then enters the evaporator feed water heater (5) to heat the low-pressure feed water. Finally, enter the desalinated preheater, preheat the demineralized water at normal temperature, and the temperature of the external sulfuric acid is lowered to 108 °C for downstream processing.
外界送入的常温脱盐水，先在脱盐水预热器(7)中加热至105℃，再送入蒸发除氧器(6)，加热至127℃，热力除氧同时产生0.15MP(g)低压蒸汽，低压蒸汽送反应塔(1)进口与工艺气体中的SO 3反应，蒸发除氧器(6)中的除氧水经低压给水泵(8)加压后，20％(质量百分数)的低压给水送混合器(4)降低循环酸浓度，剩余部分送蒸发器给水加热器(5)，加热至160℃，在送入蒸发器产生0.8MPa的低压蒸汽。 The normal temperature demineralized water sent from the outside is first heated to 105 ° C in the desalted water preheater (7), then sent to the evaporating deaerator (6), heated to 127 ° C, and the thermal deaeration simultaneously produces 0.15 MP (g) low pressure. Steam, low pressure steam is sent to the reaction tower (1) inlet and reacted with SO 3 in the process gas, and the deaerated water in the evaporating deaerator (6) is pressurized by the low pressure feed pump (8), 20% (mass percentage) The low pressure feed water mixer (4) reduces the circulating acid concentration, and the remainder is sent to the evaporator feed water heater (5), heated to 160 ° C, and sent to the evaporator to produce 0.8 MPa of low pressure steam.
采用本技术方案较现有技术外供硫酸温度显著降低，可实现每吨硫酸副产0.603吨低压蒸汽。Compared with the prior art, the temperature of the sulfuric acid is significantly reduced, and the low-pressure steam of 0.603 tons per ton of sulfuric acid by-product can be realized.
实施例3-3Example 3-3
含SO 3的工艺气体在进入反应塔(1)前，先与蒸发除氧器(6)产生的0.2MPa(g)低压蒸汽按照质量比为90:1混合，工艺气体中部分SO 3与低压蒸汽反应生成硫酸工艺气体温度升高，工艺气体温升为70℃，进入反应塔(1)后工艺气体与上部喷淋下的循环酸继续反应，反应生成220℃的高温硫酸在塔底部汇合后经循环泵(2)加压后送入蒸发器(3)产生1.2MPa的低压蒸汽，反应后尾气送下一工序处理。 The process gas containing SO 3 is mixed with 0.2 MPa (g) of low pressure steam produced by the evaporating deaerator (6) at a mass ratio of 90:1 before entering the reaction column (1), and some SO 3 and low pressure in the process gas. The temperature of the sulfuric acid process gas is increased by steam reaction, and the temperature of the process gas is increased to 70 ° C. After entering the reaction column (1), the process gas continues to react with the circulating acid under the upper spray, and the reaction forms a high temperature sulfuric acid of 220 ° C after confluence at the bottom of the tower. After being pressurized by the circulating pump (2), it is sent to the evaporator (3) to generate 1.2 MPa of low-pressure steam. After the reaction, the tail gas is sent to the next process.
95％(质量百分数)的高温硫酸出蒸发器(3)后进入混合器(4)，用低压给水降低酸浓后再进入反应塔(1)循环吸收工艺气体中的SO 3，剩余的高温硫酸从蒸发器出口循环酸管路上接出，先进入蒸发除氧器(6)热力除氧并产生低压蒸汽0.2MPa，再进入蒸发器给水加热器(5)加热送入低压给水，最后进入脱盐水预热器，预热常温脱盐水，外供硫酸温度下降至121℃送下游工序处理。 95% (mass percent) of high-temperature sulfuric acid exits the evaporator (3) and then enters the mixer (4). The low-pressure feed water is used to reduce the acid concentration and then enter the reaction column (1) to absorb the SO 3 in the process gas, and the remaining high-temperature sulfuric acid. From the outlet of the evaporator outlet acid pipeline, first enter the evaporation deaerator (6) thermal deaeration and generate low pressure steam 0.2MPa, then enter the evaporator feed water heater (5) heated to send low pressure feed water, and finally into the desalinated water The preheater is preheated to remove salt water at normal temperature, and the temperature of the external sulfuric acid is lowered to 121 ° C for downstream processing.
外界送入的常温脱盐水，先在脱盐水预热器(7)中加热至115℃，再送入蒸发除氧器(6)，加热至133℃，热力除氧同时产生0.2MP(g)低压蒸汽，低压蒸汽送反应塔(1)进口与工艺气体中的SO 3反应，蒸发除氧器(6)中的除氧水经低压给水泵(8)加压后，35％(质量百分数)的低压给水送混合器(4)降低循环酸浓度，剩余部分送蒸发器给水加热器(5)，加热至171℃，在送入蒸发器产生1.2MPa的低压蒸汽。 The ambient temperature demineralized water sent by the outside is first heated to 115 ° C in the desalted water preheater (7), then sent to the evaporating deaerator (6), heated to 133 ° C, and the thermal deaeration simultaneously produces 0.2 MP (g) low pressure. Steam, low pressure steam is sent to the reaction tower (1) inlet and reacted with SO 3 in the process gas, and the deaerated water in the evaporating deaerator (6) is pressurized by the low pressure feed pump (8), 35% (mass percentage) The low pressure feed water mixer (4) reduces the circulating acid concentration, and the remainder is sent to the evaporator feed water heater (5), heated to 171 ° C, and sent to the evaporator to produce 1.2 MPa of low pressure steam.
采用本技术方案较现有技术外供硫酸温度显著降低，可实现每吨硫酸副产0.596吨低压蒸汽。Compared with the prior art, the temperature of the sulfuric acid is significantly reduced, and the low-pressure steam of 0.596 tons per ton of sulfuric acid by-product can be realized.

Claims (15)

  1. 一种含S0 3气体制酸能量回收装置，其特征在于：该装置包括反应塔(1)、蒸发器(3)和蒸发除氧器(6)，所述的反应塔(1)的底部通过循环泵(2)与蒸发器(3)相连，所述的蒸发器(3)的一个输出端通过混合器(4)与反应塔(1)的上部相连，所述的蒸发器(3)的另一个输出端依次与蒸发器给水加热器(5)、蒸发除氧器(6)和脱盐水预热器(7)相连，含SO 3的工艺气体的输出管道与反应塔(1)的底部相连。 S0 3 containing acid gas energy recovery system, characterized in that: the apparatus comprises a reaction column (1), an evaporator (3) and evaporated deaerator (6), the bottom of the reaction column (1) by a circulation pump (2) is connected to the evaporator (3), and an output end of the evaporator (3) is connected to an upper portion of the reaction column (1) through a mixer (4), the evaporator (3) The other output is connected to the evaporator feed water heater (5), the evaporative deaerator (6) and the desalted water preheater (7) in sequence, and the output line of the process gas containing SO 3 and the bottom of the reaction tower (1) Connected.
  2. 根据权利要求1所述的含S0 3气体制酸能量回收装置，其特征在于：脱盐水的输出端通过脱盐水预热器(7)与蒸发除氧器(6)相连，所述的蒸发除氧器(6)底部的一个输出端通过低压给水泵(8)依次与蒸发器给水加热器(5)和蒸发器(3)的输入端相连，另一个输出端通过低压给水泵(8)与混合器(4)相连。 The SO 3 gas-containing acid recovery device according to claim 1 , wherein the output end of the desalted water is connected to the evaporating deaerator (6) through a desalted preheater (7), and the evaporation is performed. An output of the bottom of the oxygen (6) is connected to the input of the evaporator feed water heater (5) and the evaporator (3) through a low pressure feed pump (8), and the other output is passed through a low pressure feed pump (8) The mixer (4) is connected.
  3. 根据权利要求1所述的含S0 3气体制酸能量回收装置，其特征在于：所述的蒸发除氧器(6)顶部的输出端与含SO 3的工艺气体的输出管道相连。 The SO 3 gas-containing acid recovery device according to claim 1, wherein the output end of the evaporation deaerator (6) is connected to an output pipe of a process gas containing SO 3 .
  4. 一种利用权利要求1所述的装置实现能量回收的方法，其特征在于：该方法包括以下步骤：A method for achieving energy recovery using the apparatus of claim 1 wherein the method comprises the steps of:
    (1)含SO 3的工艺气体在进入反应塔(1)前，先与蒸发除氧器(6)产生的低压蒸汽按60±40:1的质量比混合，含SO 3的工艺气体中部分或全部SO 3与低压蒸汽反应生成H 2SO 4，所述的工艺气体温度升高后进入反应塔(1)后与上部喷淋下的循环酸继续反应，反应生成的高温硫酸在塔底部汇合后经循环泵(2)加压后送入蒸发器(3)产生低压蒸汽，工艺气体反应后尾气送下一工序处理； (1) The process gas containing SO 3 is mixed with the low-pressure steam generated by the evaporating deaerator (6) at a mass ratio of 60±40:1 before entering the reaction column (1), and part of the process gas containing SO 3 Or all of the SO 3 reacts with the low pressure steam to form H 2 SO 4 , and the process gas enters the reaction column after the temperature rises, and then continues to react with the circulating acid under the upper spray, and the high temperature sulfuric acid formed by the reaction converges at the bottom of the tower. After being pressurized by the circulating pump (2), it is sent to the evaporator (3) to generate low-pressure steam. After the process gas is reacted, the tail gas is sent to the next process;
    (2)85±10％的高温硫酸出蒸发器(3)后进入混合器(4)，用低压给水降低酸浓后再进入反应塔(1)循环吸收工艺气体中的SO 3，剩余的高温硫酸从蒸发器(3)出口循环酸管路上接出，先进入蒸发器给水加热器(5)加热送入低压给水，再进入蒸发除氧器(6)热力除氧并产生低压蒸汽，最后进入脱盐水预热器，预热常温脱盐水，降温后硫酸送下游工序处理； (2) 85±10% of high-temperature sulfuric acid exits the evaporator (3) and then enters the mixer (4). The low-pressure feed water is used to reduce the acid concentration and then enter the reaction tower (1) to absorb the SO 3 in the process gas, and the remaining high temperature. Sulfuric acid is taken from the outlet acid pipeline of the evaporator (3) outlet, first enters the evaporator feed water heater (5) and is heated to the low pressure feed water, and then enters the evaporative deaerator (6) to remove oxygen and generate low pressure steam, and finally enters Desalination preheater, preheating to remove salt water at normal temperature, and after cooling, the sulfuric acid is sent to the downstream process;
    (3)外界送入的常温脱盐水，先在脱盐水预热器(7)中加热，之后再送入蒸发除氧器(6)加热，在热力除氧同时产生低压蒸汽，低压蒸汽送反应塔(1)进口与工艺气体中的SO 3反应，蒸发除氧器(6)中的除氧水经低压给水泵(8)加压后，25±15％的低压给水送混合器(4)降低循环酸浓度，剩余的低压给水送蒸发器给水加热器(5)，加热后再送入蒸发器(3)产生低压蒸汽。 (3) The normal temperature demineralized water sent by the outside is first heated in the desalinated preheater (7), then sent to the evaporating deaerator (6) for heating, and the low pressure steam is generated simultaneously by the thermal deaeration, and the low pressure steam is sent to the reaction tower. (1) The inlet reacts with SO 3 in the process gas, and the deaerated water in the evaporating deaerator (6) is pressurized by the low pressure feed pump (8), and 25±15% of the low pressure feed water is fed to the mixer (4). The circulating acid concentration, the remaining low pressure feed water is sent to the evaporator feed water heater (5), heated and sent to the evaporator (3) to produce low pressure steam.
  5. 根据权利要求4所述的实现能量回收的方法，其特征在于：步骤(1)中蒸发除氧器(6)产生的低压蒸汽的压力为0.2±0.1MPa，循环泵(2)出口高温硫酸的温度为190±30℃，蒸发器(3)产生的低压蒸汽压力为0.8±0.4MPa。The method for realizing energy recovery according to claim 4, characterized in that the pressure of the low-pressure steam generated by the evaporating deaerator (6) in the step (1) is 0.2 ± 0.1 MPa, and the circulation pump (2) exits the high-temperature sulfuric acid. The temperature is 190 ± 30 ° C, and the low pressure steam pressure generated by the evaporator (3) is 0.8 ± 0.4 MPa.
  6. 一种含S0 3气体制酸能量回收装置，其特征在于：该装置包括反应塔(1)、蒸发器(3)、蒸发器给水加热器(5)和蒸发除氧器(6)，所述的反应塔(1)的底部通过循环泵(2)与蒸发器(3)相连，蒸发器(3)的一个输出端通过混合器(4)与反应塔(1)的上部相连，蒸发器(3)的另一个输出端分别和蒸发器给水加热器(5)和蒸发除氧器(6)相连，所述蒸发器给水加热器(5)和蒸发除氧器(6)的输出端均与脱盐水预热器(7)相连，含SO 3的工艺气体的输出管道与反应塔(1)的底部相连。 S0 3 containing acid gas energy recovery system, characterized in that: the apparatus comprises a reaction column (1), an evaporator (3), an evaporator feedwater heater (5) and evaporated deaerator (6), the The bottom of the reaction column (1) is connected to the evaporator (3) through a circulation pump (2), and an output end of the evaporator (3) is connected to the upper portion of the reaction column (1) through a mixer (4), and the evaporator ( The other output of 3) is connected to the evaporator feed water heater (5) and the evaporative deaerator (6), respectively, and the output of the evaporator feed water heater (5) and the evaporating deaerator (6) are The desalted water preheater (7) is connected, and the output pipe of the SO 3 containing process gas is connected to the bottom of the reaction column (1).
  7. 根据权利要求6所述的含S0 3气体制酸能量回收装置，其特征在于：脱盐水的输出端通过脱盐水预热器(7)与蒸发除氧器(6)相连，所述的蒸发除氧器(6)底部的一个输出端依次通过低压给水泵(8)、蒸发器给水加热器(5)与蒸发器(3)的输入端相连，另一个输出端通过低压给水泵(8)与混合器(4)相连。 The SO 3 gas-containing acid recovery device according to claim 6, wherein the output end of the desalted water is connected to the evaporating deaerator (6) through a desalted preheater (7), and the evaporation is performed. An output of the bottom of the oxygenator (6) is sequentially connected to the input end of the evaporator (3) through the low pressure feed pump (8), the evaporator feed water heater (5), and the other output through the low pressure feed pump (8) The mixer (4) is connected.
  8. 根据权利要求6所述的含S0 3气体制酸能量回收装置，其特征在于：所述的蒸发除氧器(6)顶部的输出端与含SO 3的工艺气体的输出管道相连。 The SO 3 gas-containing acid recovery device according to claim 6, wherein the output end of the evaporation deaerator (6) is connected to an output pipe of a process gas containing SO 3 .
  9. 一种利用权利要求6所述的装置实现能量回收的方法，其特征在于：该方法包括以下步骤：A method for achieving energy recovery using the apparatus of claim 6, wherein the method comprises the steps of:
    (1)含SO 3的工艺气体在进入反应塔(1)前，先与蒸发除氧器(6)产生的低压蒸汽按60±40：1的质量比混合，含SO 3的工艺气体中部分或全部SO 3与低压蒸汽反应生成H 2SO 4，所述的工艺气体温度升高后进入反应塔(1)后与上部喷淋下的循环酸继续反应，反应生成的高温硫酸在塔底部汇合后经循环泵(2)加压后送入蒸发器(3)产生低压蒸汽，工艺气体反应后尾气送下一工序处理； (1) The process gas containing SO 3 is mixed with the low-pressure steam generated by the evaporating deaerator (6) at a mass ratio of 60±40:1 before entering the reaction column (1), and part of the process gas containing SO 3 Or all of the SO 3 reacts with the low pressure steam to form H 2 SO 4 , and the process gas enters the reaction column after the temperature rises, and then continues to react with the circulating acid under the upper spray, and the high temperature sulfuric acid formed by the reaction converges at the bottom of the tower. After being pressurized by the circulating pump (2), it is sent to the evaporator (3) to generate low-pressure steam. After the process gas is reacted, the tail gas is sent to the next process;
    (2)85±10％的高温硫酸出蒸发器(3)后进入混合器(4)，用低压给水降低酸浓后再进入反应塔(1)循环吸收工艺气体中的SO 3，剩余的高温硫酸再次分为两个部分，60±40％进入蒸发除氧器(6)热力除氧并产生低压蒸汽，剩余的另一部分进入蒸发器给水加热器(5)加热送入低压给水，从蒸发除氧器(6)和蒸发器给水加热器(5)出来的硫酸进入脱盐水预热器(7)，预热常温脱盐水，降温后硫酸送下游工序处理； (2) 85±10% of high-temperature sulfuric acid exits the evaporator (3) and then enters the mixer (4). The low-pressure feed water is used to reduce the acid concentration and then enter the reaction tower (1) to absorb the SO 3 in the process gas, and the remaining high temperature. Sulfuric acid is divided into two parts again, 60±40% enters the evaporating deaerator (6) thermal deaerator and produces low pressure steam, and the other part enters the evaporator feed water heater (5) is heated to feed low pressure feed water, from evaporation The oxygen (6) and the sulfuric acid from the evaporator feed water heater (5) enter the desalinated preheater (7), preheating the normal temperature to remove the brine, and after the temperature is lowered, the sulfuric acid is sent to the downstream process;
    (3)外界送入的常温脱盐水，先在脱盐水预热器(7)中加热，之后再送入蒸发除氧器(6)加热，在热力除氧同时产生低压蒸汽，低压蒸汽送反应塔(1)进口管路与工艺气体中的SO 3反应，蒸发除氧器(6)中的除氧水经低压给水泵(8)加压后，25±15％的低 压给水送混合器(4)降低循环酸浓度，剩余部分送蒸发器给水加热器(5)，加热后再送入蒸发器(3)产生低压蒸汽。 (3) The normal temperature demineralized water sent by the outside is first heated in the desalinated preheater (7), then sent to the evaporating deaerator (6) for heating, and the low pressure steam is generated simultaneously by the thermal deaeration, and the low pressure steam is sent to the reaction tower. (1) The inlet line reacts with SO 3 in the process gas, and the deaerated water in the evaporating deaerator (6) is pressurized by the low pressure feed pump (8), and 25±15% of the low pressure feed water is sent to the mixer (4 The circulating acid concentration is lowered, and the remaining portion is sent to the evaporator feed water heater (5), which is heated and then sent to the evaporator (3) to generate low pressure steam.
  10. 根据权利要求9所述的实现能量回收的方法，其特征在于：步骤(1)中蒸发除氧器(6)产生的低压蒸汽的压力为0.15±0.05MPa，环泵(2)出口高温硫酸的温度为190±30℃，蒸发器(3)产生低压蒸汽的压力为0.8±0.4MPa。The method for realizing energy recovery according to claim 9, characterized in that the pressure of the low-pressure steam generated by the evaporating deaerator (6) in the step (1) is 0.15±0.05 MPa, and the ring pump (2) exits the high-temperature sulfuric acid. The temperature is 190 ± 30 ° C, and the pressure at which the evaporator (3) generates low pressure steam is 0.8 ± 0.4 MPa.
  11. 一种含S0 3气体制酸能量回收装置，其特征在于：该装置包括反应塔(1)、蒸发器(3)、蒸发器给水加热器(5)和蒸发除氧器(6)，所述的反应塔(1)的底部通过循环泵(2)与蒸发器(3)相连，蒸发器(3)的一个输出端通过混合器(4)与反应塔(1)的上部相连，蒸发器(3)的另一个输出端依次与蒸发除氧器(6)和蒸发器给水加热器(5)和脱盐水预热器(7)相连，含SO 3的工艺气体的输出管道与反应塔(1)的底部相连。 S0 3 containing acid gas energy recovery system, characterized in that: the apparatus comprises a reaction column (1), an evaporator (3), an evaporator feedwater heater (5) and evaporated deaerator (6), the The bottom of the reaction column (1) is connected to the evaporator (3) through a circulation pump (2), and an output end of the evaporator (3) is connected to the upper portion of the reaction column (1) through a mixer (4), and the evaporator ( The other output of 3) is connected to the evaporating deaerator (6) and the evaporator feed water heater (5) and the desalted water preheater (7) in sequence, and the output pipe and reaction tower of the process gas containing SO 3 (1) ) connected at the bottom.
  12. 根据权利要求11所述的含S0 3气体制酸能量回收装置，其特征在于：脱盐水的输出端通过脱盐水预热器(7)与蒸发除氧器(6)相连，所述的蒸发除氧器(6)底部的一个输出端通过低压给水泵(8)依次与蒸发器给水加热器(5)和蒸发器(3)相连，另一个输出端通过低压给水泵(8)与混合器(4)相连。 According to claim 11 containing S0 3 acid gas energy recovery system, characterized in that: the desalinated water output connected via desalted water preheater (7) and the evaporator deaerator (6), in addition to the evaporation An output of the bottom of the oxygenator (6) is connected to the evaporator feed water heater (5) and the evaporator (3) through the low pressure feed pump (8) in turn, and the other output through the low pressure feed pump (8) and the mixer ( 4) Connected.
  13. 根据权利要求11所述的含S0 3气体制酸能量回收装置，其特征在于：所述的蒸发除氧器(6)顶部的输出端与含SO 3的工艺气体的输出管道相连。 The SO 3 gas-containing acid recovery device according to claim 11, wherein the output end of the evaporation deaerator (6) is connected to an output pipe of a process gas containing SO 3 .
  14. 一种利用权利要求11所述的装置实现含S0 3气体制酸能量回收的方法，其特征在于：该方法包括以步骤： Utilizing apparatus as claimed in claim 11, wherein the method implemented S0 3 containing acid gas energy recovery system, characterized in that: the method comprising the steps of:
    (1)含SO 3的工艺气体在进入反应塔(1)前，先与蒸发除氧器(6)产生的低压蒸汽按60±40:1的质量比混合，含SO 3的工艺气体中部分或全部SO 3与低压蒸汽反应生成H 2SO 4，所述的工艺气体温度升高后进入反应塔(1)后与上部喷淋下的循环酸继续反应，反应生成的高温硫酸在塔底部汇合后经循环泵(2)加压后送入蒸发器(3)产生低压蒸汽，反应后尾气送下一工序处理； (1) The process gas containing SO 3 is mixed with the low-pressure steam generated by the evaporating deaerator (6) at a mass ratio of 60±40:1 before entering the reaction column (1), and part of the process gas containing SO 3 Or all of the SO 3 reacts with the low pressure steam to form H 2 SO 4 , and the process gas enters the reaction column after the temperature rises, and then continues to react with the circulating acid under the upper spray, and the high temperature sulfuric acid formed by the reaction converges at the bottom of the tower. After being pressurized by the circulating pump (2), it is sent to the evaporator (3) to generate low-pressure steam, and the tail gas is sent to the next process after the reaction;
    (2)85+10％高温硫酸出蒸发器(3)后一部分进入混合器(4)，用低压给水降低酸浓后再进入反应塔(1)循环吸收工艺气体中的SO 3，剩余的高温浓硫酸依次进入蒸发除氧器(6)产生低蒸汽、再进入蒸发器给水加热器(5)加热送入低压给水，在进入脱盐水预热器(7)加热外界送入的脱盐水，降温后硫酸送下游工序处理； (2) 85+10% high-temperature sulfuric acid out of the evaporator (3), the latter part enters the mixer (4), lowers the acid concentration with low-pressure feed water, and then enters the reaction tower (1) to absorb the SO 3 in the process gas, and the remaining high temperature The concentrated sulfuric acid enters the evaporating deaerator (6) in sequence to generate low steam, and then enters the evaporator. The feed water heater (5) is heated to feed the low-pressure feed water, and enters the desalted water preheater (7) to heat the externally sent desalinated water to cool down. After the sulfuric acid is sent to the downstream process;
    (3)外界送入的常温脱盐水，先在脱盐水预热器(7)中加热，之后再送入蒸发除氧器(6)加热，在热力除氧同时产生低压蒸汽，低压蒸汽送反应塔(1)进口与工艺气体中的SO 3反应，蒸发除氧器(6)中的除氧水经低压给水泵(8)加压后，25±15％的低压给 水送混合器(4)降低循环酸浓度，剩余的低压给水送蒸发器给水加热器(5)，加热后再送入蒸发器(3)产生低压蒸汽。 (3) The normal temperature demineralized water sent by the outside is first heated in the desalinated preheater (7), then sent to the evaporating deaerator (6) for heating, and the low pressure steam is generated simultaneously by the thermal deaeration, and the low pressure steam is sent to the reaction tower. (1) The inlet reacts with SO 3 in the process gas, and the deaerated water in the evaporating deaerator (6) is pressurized by the low pressure feed pump (8), and 25±15% of the low pressure feed water is fed to the mixer (4). The circulating acid concentration, the remaining low pressure feed water is sent to the evaporator feed water heater (5), heated and sent to the evaporator (3) to produce low pressure steam.
  15. 根据权利要求14所述的实现能量回收的方法，其特征在于：步骤(1)中蒸发除氧器(6)产生的低压蒸汽的压力为0.15±0.05MPa，环泵(2)出口高温硫酸的温度为190±30℃，蒸发器(3)产生低压蒸汽的压力为0.8±0.4MPa。The method for realizing energy recovery according to claim 14, wherein the pressure of the low-pressure steam generated by the evaporating deaerator (6) in the step (1) is 0.15±0.05 MPa, and the ring pump (2) exits the high-temperature sulfuric acid. The temperature is 190 ± 30 ° C, and the pressure at which the evaporator (3) generates low pressure steam is 0.8 ± 0.4 MPa.
PCT/CN2018/112925 2018-04-02 2018-10-31 Acid generation energy recovery device and method for so3-containing gas WO2019192173A1 (en)

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