CN203238034U - Intermediate absorption subsystem for sulfuric acid production system and bi-absorption system for producing sulfuric acid by oxidizing sulfur dioxide - Google Patents

Intermediate absorption subsystem for sulfuric acid production system and bi-absorption system for producing sulfuric acid by oxidizing sulfur dioxide Download PDF

Info

Publication number
CN203238034U
CN203238034U CN2013200868072U CN201320086807U CN203238034U CN 203238034 U CN203238034 U CN 203238034U CN 2013200868072 U CN2013200868072 U CN 2013200868072U CN 201320086807 U CN201320086807 U CN 201320086807U CN 203238034 U CN203238034 U CN 203238034U
Authority
CN
China
Prior art keywords
subsystem
absorption
sulfuric acid
outlet
entrance
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
CN2013200868072U
Other languages
Chinese (zh)
Inventor
O·佩雷斯
Y·范
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Aker Solutions Canada Inc
Original Assignee
Aker Kvaerner Canada Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Aker Kvaerner Canada Inc filed Critical Aker Kvaerner Canada Inc
Application granted granted Critical
Publication of CN203238034U publication Critical patent/CN203238034U/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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
    • C01B17/765—Multi-stage SO3-conversion
    • C01B17/7655—Multi-stage SO3-conversion with intermediate absorption
    • 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
    • C01B17/806—Absorbers; Heat exchangers
    • 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

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Gas Separation By Absorption (AREA)
  • Treating Waste Gases (AREA)

Abstract

The utility model discloses an intermediate absorption subsystem for a sulfuric acid production system. The intermediate absorption subsystem comprises a co-current open spray tower, an energy recovery subsystem and an intermediate absorption tower, wherein a bottom outlet of the spray tower and a first side inlet of a heat exchanger of the energy recovery subsystem are in fluid connection; a spray inlet of the spray tower and a first side outlet of the heat exchanger are in fluid connection; a water supply and a second side inlet of the heat exchanger are in fluid connection; a second side outlet of the heat exchanger is used for outputting steam; a lower inlet of the middle absorption tower is connected to a lower outlet of the spray tower. The utility model further discloses a bi-absorption system for producing sulfuric acid by oxidizing sulfur dioxide. The bi-absorption system comprises a first oxidization subsystem with a contact catalyst, the intermediate absorption subsystem, a second oxidization subsystem with a contact catalyst, and a final absorption tower, which are connected with one another in sequence.

Description

Be used for the intermediate absorption subsystem of sulfuric acid production system and be used for oxidation sulfurous gas to produce the biabsorption system of sulfuric acid
Technical field
The utility model relates to the energy efficient system for the production of sulfuric acid.It is particularly related to the system that adopts spray tower to absorb.
Background technology
Sulfuric acid is one of chemical goods of in the world turnout maximum, and is widely used in chemical industry and commerical prod.Usually, the production method of sulfuric acid comprises at first Sulphur Dioxide is become sulphur trioxide, and then described sulphur trioxide is changed into sulfuric acid.In 1831, P.Phillips developed the contact process of supplying with for the production of most current sulfuric acid.
The bare bones of described contact process comprises: obtain sulfurous gas and supply with (for example usually obtaining by burning sulphur), then under the condition that has the catalyzer (generally being barium oxide) that is used for the acceleration chemical reaction, come oxidation sulfurous gas with oxygen, to produce sulphur trioxide.Reversible and the heat release of described chemical reaction, and important part is suitably to control the temperature of the gas on the catalyzer, in order under the condition of not damaging the contact device that comprises catalyzer, realize desired conversion.
Then, the sulphur trioxide that produces is inhaled in the concentrated sulfuric acid solution to form oleum, and described oleum is diluted to produce another kind of concentrated sulfuric acid solution again.Can avoid like this sulphur trioxide is directly dissolved in the consequence that the very exothermic reaction in the water causes.
Although the ultimate principle of contact process is relatively simple, expectation maximization sulfurous gas is to the conversion of sulfuric acid.Therefore, often relate to absorption stage more than one for the production of the modern factories of sulfuric acid, transform and absorb to strengthen.Usually adopt the biabsorption flow process, in described biabsorption flow process, gas experiences two contacts and absorption stage (be first catalyzed conversion and follow-up absorption stage, and ensuing second catalyzed conversion and absorption stage) continuously.About the traditional available selection of gas washing in SA production and contact process and the preferential details of selecting are known, and can be for example at " sulfuric acid manufacturing manual (MM) " (Douglas Louie work, ISBN0-9738992-0-4 was published by DKL Engineering company limited at Ontario, Canada in 2005) in find.
Energy requirement during also the expectation minimization sulfuric acid industry is produced.In related a plurality of flow processs, a large amount of thermals source and heat demand are arranged.By arranging to maximize energy recovery with complicated interchanger, can preferably improve efficiency.
In file US4576813, Monsanto discloses a kind of method and apparatus many years ago, is used for significantly improving the efficient of the factory that uses the biabsorption flow process.Disclosed heat recovery system is carried out the temperature rising that sulphur trioxide absorbs with intermediate absorption in the stage.By under these higher temperature, turning round, can with absorb and the heat of dilution generation for generation of useful steam, rather than with hot type to cooling tower.Therefore, can obviously improve whole efficiency.In described device, traditional intermediate absorber is replaced by two-stage absorption tower, recycle pump, interchanger and boiler.The two-stage absorption tower is included in two bed of packings of the series connection in the same absorption tower.But under these higher temperature, the material of structure of the prior art bears obviously higher corrosion rate.In order to make the method commercialization, must should adopt higher sulfuric acid concentration, adopt again different, selected especially structural alloys, so that device can be suitably corrosion-resistant under these higher temperature.
But the shortcoming of aforesaid method is, the function of previous traditional intermediate absorber is integrated in the two-stage absorption tower of energy efficient system.If the recovery of heat subsystem goes wrong in operation process, whole factory need to stop work in order to keep in repair.
Outotec has built the sulfuric acid plant that adopts similar heat recovery method but implement with different devices.In the Outotec system, the intermediate absorption stage is adopted quenching Venturi tube and the bed of packings resorber of combination, rather than independent two-stage absorption tower.The advantage of this method is, quenching Venturi tube and interchanger subsystem are in the situation that running goes wrong can be bypassed.This is so that remaining bed of packings resorber turns round as traditional intermediate absorber (certainly, do not improve recovery of heat), and therefore, sulfuric acid plant is in the situation that the recovery of heat subsystem goes wrong can remain in operation at least.But, use the inferior position of quenching Venturi tube to be, need to operate described quenching Venturi tube and its interior pressure drop is provided by large energy.
As described, because related higher temperature and different sulfuric acid concentrations, the metal alloy that needs to select especially in the recovery of heat subsystem that this efficient improves is to provide acceptable erosion resistance. 100(UNS S32760) be a kind of alloy, it is modified to be used for the sulfuric acid Application in manufacture during up to 200 ° of C in the temperature that raises.
But still expectation further improves the efficiency in the sulfuric acid industry production again.The utility model has solved the problem of relevant this expectation, and following disclosed other benefit is provided.
The utility model content
The utility model provides a kind of energy efficient system for the production of sulfuric acid, and it uses also stream (co-current) the open spray tower that preferably has a plurality of spray water plane.Because the fog nozzle of each horizontal plane all provides the identical motivating force that is used for absorption (because it is basic identical on each horizontal plane to absorb temperature and the concentration of acid), SO 3Absorption strengthened.This compares the advantage of having more with using packing tower or quenching Venturi scrubber, in packing tower or quenching Venturi scrubber, raises SO at the later stage that absorbs owing to absorbing temperature and the concentration of acid 3Absorption will weaken along with the airflow passes device.
Particularly, the utility model comprises the intermediate absorption subsystem for sulfuric acid production system, and it comprises and flows open spray tower, energy recovery subsystem and intermediate absorber.And flow open spray tower and comprise be used to containing SO 2And SO 3Air-flow top entrance, the below outlet that is used for the air-flow after the spray absorber, at least one spraying entrance, in spray tower and be connected to the spraying entrance at least one fog nozzle, be used for the entrance of dilution water and the outlet at bottom that is used for sulfuric acid liquid.The energy recovery subsystem comprises pump and the interchanger of arranged in series, wherein the outlet at bottom fluid of spray tower is connected to the first side entrance of interchanger, the spraying inlet fluid of spray tower is connected to the first side outlet of interchanger, the water supply fluid is connected to the second side entrance of interchanger, and the second side outlet of interchanger is steam output.The energy recovery subsystem produces for example low-pressure steam of about 7 bar (gauge pressure) usually.Intermediate absorber comprises the below entrance that is used for air-flow that is connected to spray tower below outlet, be used in the top outlet, divider entrance, intermediate absorber of the air-flow of bed of packings after absorbing liquid dispenser, the bed of packings in intermediate absorber and below liquid dispenser, for the outlet at bottom of sulfuric acid liquid and outlet at bottom that fluid is connected to intermediate absorber and the pump of divider entrance.
Spray tower in the intermediate absorption subsystem is preferably included at least two horizontal planes, a plurality of fog nozzles on three horizontal planes for example.Preferably, fog nozzle produces mean sizes less than 300 microns spraying, so that drop has relatively large surface-area, thereby absorbs better SO 3
In this system, adopt the inferior position of spray tower to be to produce submicron order fog.But this can be removed by efficient fog stripper, for example pedesis fog strainer.Therefore, the intermediate absorber in the intermediate absorption subsystem can be included in bed of packings and be used for the air-flow of bed of packings after absorbing above fog stripper between the outlet.
As other system that intermediate absorption turned round in the stage, need special corrosion-resistant metal alloys in the interchanger in the energy recovery subsystem under higher temperature.Suitable this corrosion-resistant metal alloys comprises such as UNS and is numbered the super two-phase alloys of S32760 or is numbered the chromium based austenite alloy of R20033 such as UNS.
The utility model comprises that also the complete oxidation sulfurous gas that is used for is to produce the biabsorption system of sulfuric acid.In this biabsorption system, comprise the first oxidation subsystem that contains the contact catalyzer, the aforesaid intermediate absorption subsystem of the present utility model that links to each other in turn, the second oxidation subsystem that contains the contact catalyzer and final absorption tower.
Advantage provided by the utility model is, when energy-recuperation system can not turn round (by walk around spray tower and energy recovery subsystem or by closing simply the pump of energy recovery subsystem), described biabsorption system can also turn round with traditional mode, therefore, described biabsorption system can continue to produce sulfuric acid.The utility model also provides the pressure drop in the spray tower is required lower advantage, and therefore, comparing the quenching venturi arrangement needs still less energy (namely more high energy efficiency).
Description of drawings
Fig. 1 shows the schematic diagram of the intermediate absorption subsystem for sulfuric acid production system of the present utility model, and it comprises spray tower, energy-recuperation system and intermediate absorber;
Fig. 2 shows the schematic diagram for the production of the biabsorption system of sulfuric acid, comprises the intermediate absorption subsystem of Fig. 1 in described biabsorption system.
Embodiment
Unless context has requirement in addition, otherwise in the full content of specification sheets and claims, word " comprises ", " comprising " etc. should be understood to the open meaning that comprises.Word " one ", " one " etc. are considered to mean at least one, and are not limited to only have one.
In the context of relevant numeral, word " approximately/approximately " should be understood to and means and add or deduct 10%.
Fig. 1 shows the schematic diagram of intermediate absorption subsystem of the present utility model, and described intermediate absorption subsystem uses in sulfuric acid production system.As shown, intermediate absorption subsystem 1 comprises open spray tower 2, energy recovery subsystem 9 and intermediate absorber 14.Contain SO 3And SO 2Hot gas flow (for example approximately 200 ° of C) be introduced in the top entrance 3 of spray tower 2.Wherein, SO 3By and the acid with suitable temp (for example approximately 120 ° of C) and concentration (for example 98.5 weight percent) that enters of conductance spray absorbed.As shown, supply with in the cooling acid that spraying entrance 5 places are provided for spraying, and it is caused a plurality of fog nozzle 6a, 6b, 6c.The fog nozzle here is positioned at three different horizontal planes in spray tower 2.Fog nozzle on same horizontal plane represents (being 6a, 6b or 6c) with identical Reference numeral.Preferably, fog nozzle produces mean sizes less than 300 microns spraying, so that drop has relatively large surface-area, thereby absorbs better SO 3
Contain absorbed SO 3In the bottom that interior sulfuric acid is fallen spray tower 2 with the about temperature of 170 ° of C, and suitably diluted by the dilution water that provides at entrance 7 places.Then, these hot acids (for example approximately 170 ° of C) are pumped to interchanger 10 the energy recovery subsystem 9 via pump 11 from outlet at bottom 8.Hot acid is directed to the first side entrance 12a of interchanger 10, so hot acid just carries out heat exchange with the Cold water supply to the second side entrance 13a of interchanger 10 is provided.The acid that is cooled is now got ready, and it is used as absorbing medium, and causes spraying entrance 5 from the first side outlet 12b of interchanger 10.Now fully be heated at the water of the second side and become low-pressure steam, so the steam output of the second side outlet 13b of interchanger 10 for using elsewhere as required.Interchanger 10 is made by special corrosion-resistant metal alloys, is numbered the super two-phase alloys (superduplex alloy) of S32760 or the chromium based austenite alloy (chromium-based austenitic alloy) that UNS is numbered R20033 such as UNS.
In spray tower 2, contain SO 2With unabsorbed SO 3Interior slightly cold air stream (for example approximately 150oC) below outlet 4 places discharge, and be directed to the below entrance 15 of intermediate absorber 14, and then through bed of packings 19, unnecessary SO 3In described bed of packings 19, be absorbed.In order to realize this purpose, will absorb acid at divider entrance 17 places provides to liquid dispenser 18, and described liquid dispenser 18 distributes described acid on bed of packings 19.Contain absorbed SO 3Fall the bottom of intermediate absorber 14 at interior sulfuric acid, become the absorption acid of on bed of packings, using and supply with.(dilution water must or add as required, but not shown in Figure 1.) these acid solutions are pumped to divider entrance 17 via pump 21 from outlet at bottom 20.Efficient pedesis fog stripper 22 is equipped with when using spray tower, can form a large amount of submicron order fog, so intermediate absorber 14.Absorb after the flow process, air-flow exports up 16 places and discharges from middle absorption tower 14.
Fig. 2 shows the schematic diagram for the production of the exemplary biabsorption system 23 of sulfuric acid.Wherein system 23 comprises: contain the first oxidation subsystem of contact catalyzer, the intermediate absorption subsystem 1 of Fig. 1, the second oxidation subsystem that contains the contact catalyzer and final absorption tower.In this complicated system, first oxidation stage occurs in catalyst bed 24-26, next is intermediate absorption, and then second oxidation stage occurs in catalyst bed 27, next is final absorption.Therefore, the first oxidation subsystem comprises catalyst bed 24-26, and the second oxidation subsystem comprises catalyst bed 27.
Biabsorption system 23 among Fig. 2 comprises the contact catalyst bed 24,25,26 and 27 of four separation, and wherein each comprises contact catalyzer heap.System 23 comprises that also intermediate absorption subsystem 1(comprises spray tower 2, energy recovery subsystem 9 and intermediate absorber 14), final absorption tower 28 and output chimney 30.System 23 also comprises the interchanger of four separation, in order to obtain higher transformation efficiency in whole flow process.These interchanger are expressed as cool exchanger 32, heat exchanger 33, resuperheat interchanger 34 and cold again heat exchanger 35.For fear of in Fig. 2, causing confusion, the interior absolute construction of the interchanger shown in these and their various entrance and exits are not shown.Replace, at all wires arrow is set flowing of just processed air-flow is shown.Therefore, be easy to know entrance and exit by inference by the direction of arrow.
Briefly, the biabsorption flow process among Fig. 2 is undertaken by following.The air-flow that contains sulfurous gas and oxygen is provided to cool exchanger 32 with supply temperature, described air-flow herein with have the 4th a catalyst bed temperature out carry out heat exchange than hot gas flow.Then, heat exchanger 33 is discharged and be directed to air-flow from cool exchanger 32, described air-flow herein with have the first catalyst bed temperature out carry out heat exchange than hot gas flow.Then, the first catalyst bed 24 is discharged and be directed to air-flow with the first catalyst bed temperature in from heat exchanger 33.SO in the air-flow 2The oxidation first time occur on the catalyst bed 24, and the air-flow of discharging will have the first higher catalyst bed temperature out.
Carry out in heat exchanger 33 after the heat exchange, air-flow is discharged with the second catalyst bed temperature in, and is directed to the second catalyst bed 25.SO in the air-flow 2The oxidation second time occur on the catalyst bed 25, and the air-flow of discharging will have the second higher catalyst bed temperature out.
Air-flow is directed to resuperheat interchanger 34 with the second catalyst bed temperature out, described air-flow herein with discharge from cold again heat exchanger 35 carry out heat exchange than cold air stream.Then, air-flow with the 3rd catalyst bed temperature in from the centre again heat exchanger 34 discharge and be directed to the 3rd catalyst bed 26.SO in the air-flow 2For the third time oxidation occur on the catalyst bed 26, and the air-flow of discharging will have the 3rd higher catalyst bed temperature out.
Air-flow is directed to cold again heat exchanger 35 with the 3rd catalyst bed temperature out, described air-flow herein with carry out heat exchange from intermediate absorption subsystem 1 than cold air stream.Then, the top entrance 3 of the spray tower 2 the intermediate absorption subsystem 1 is discharged and be directed to air-flow with intermediate absorption subsystem temperature in from cold again heat exchanger 35, carries out the SO from air-flow in intermediate absorption subsystem 1 3The intermediate absorption first time.Absorption and energy recovery are carried out among Fig. 1 as above-mentioned.Air-flow exports up 16 places and discharges from middle absorption tower 14, then is heated in two stages.Fs is included in the cold again heat exchanger 35 carries out heat exchange with the air-flow with the 3rd catalyst bed temperature out, to produce the air-flow of discharging from cold again heat exchanger 35.Then, subordinate phase comprises air-flow is caused resuperheat interchanger 34, described air-flow herein with have the second catalyst bed temperature out carry out heat exchange than hot gas flow, with produce with the 4th catalyst bed temperature in from the centre heat exchanger 34 air-flow of discharging again.
Next, air-flow is directed to the 4th catalyst bed 27 with the 4th catalyst bed temperature in.SO in the air-flow 2The 4th oxidation on catalyst bed 27, carry out, and the air-flow of discharging has the 4th higher catalyst bed temperature out.
Air-flow is directed to cool exchanger 32 with the 4th catalyst bed temperature out, and described air-flow carries out heat exchange with colder supply air flow herein.Then, air-flow is discharged and is directed to final absorption tower 28 from cool exchanger 32 with final absorption temperature in, carries out the SO from air-flow in described final absorption tower 28 2The second time, i.e. final the absorption.Then, the air-flow of discharge is by chimney 30 dischargings.
Biabsorption system among Fig. 2 produces sulfuric acid with high transformation efficiency.And the use of the utility model intermediate absorption subsystem allows higher efficiency.As apparent from Fig. 1 and 2, if because some reasons cause energy-recuperation system or spray tower not to operate, they also are easy to be bypassed, and sulfate system can not have (namely only by using intermediate absorber 14) running under their condition, therefore, system 23 can turn round in previous traditional mode in this case.
Although illustrate and described particular elements of the present utility model, embodiment and application, but should be understandable that, the utility model is not limited to this, because under the condition that does not depart from spirit and scope of the present disclosure, those skilled in the art especially can modify under the guide of aforementioned instruction.Such modification all is considered within the authority and scope of appended claims.

Claims (7)

1. an intermediate absorption subsystem that is used for sulfuric acid production system is characterized in that, comprising:
And flow open spray tower, it comprises:
Be used for containing SO 2And SO 3The top entrance of air-flow;
Be used for the below outlet of spray absorber air-flow afterwards;
At least one entrance of spraying;
In described spray tower and be connected at least one fog nozzle of described spraying entrance;
The entrance that is used for dilution water; And
The outlet at bottom that is used for sulfuric acid liquid;
The energy recovery subsystem, it comprises pump and the interchanger of arranged in series, wherein, the described outlet at bottom fluid of described spray tower is connected to the first side entrance of described interchanger, the described spraying inlet fluid of described spray tower is connected to the first side outlet of described interchanger, the water supply fluid is connected to the second side entrance of described interchanger, and the second side outlet of described interchanger is steam output; And
Intermediate absorber, it comprises:
The below entrance that is used for described air-flow, it is connected to the below outlet of described spray tower;
Be used for the top outlet that bed of packings absorbs air-flow afterwards;
The divider entrance;
Liquid dispenser in described intermediate absorber;
In described intermediate absorber and be positioned at bed of packings below the described liquid dispenser;
The outlet at bottom that is used for sulfuric acid liquid; And
Fluid is connected to the described outlet at bottom of described intermediate absorber and the pump of described divider entrance.
2. intermediate absorption subsystem as claimed in claim 1 is characterized in that, described spray tower is included in a plurality of fog nozzles at least two horizontal planes.
3. intermediate absorption subsystem as claimed in claim 2 is characterized in that, described spray tower is included in a plurality of fog nozzles on three horizontal planes.
4. intermediate absorption subsystem as claimed in claim 2 is characterized in that, described fog nozzle produces mean sizes less than 300 microns spraying.
5. intermediate absorption subsystem as claimed in claim 1 is characterized in that, described intermediate absorber is included in described bed of packings and described for the fog stripper between the top outlet of the air-flow after the bed of packings absorption.
6. intermediate absorption subsystem as claimed in claim 1, it is characterized in that, described interchanger in described energy recovery subsystem comprises metal alloy, and described metal alloy is that UNS is numbered the super two-phase alloys of S32760 or the chromium based austenite alloy that UNS is numbered R20033.
7. one kind is used for oxidation sulfurous gas to produce the biabsorption system of sulfuric acid, it is characterized in that, comprise the first oxidation subsystem that contains the contact catalyzer, the intermediate absorption subsystem as claimed in claim 1 that links to each other in turn, the second oxidation subsystem that contains the contact catalyzer and final absorption tower.
CN2013200868072U 2013-01-17 2013-02-26 Intermediate absorption subsystem for sulfuric acid production system and bi-absorption system for producing sulfuric acid by oxidizing sulfur dioxide Expired - Lifetime CN203238034U (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CA2,802,885 2013-01-17
CA2802885A CA2802885A1 (en) 2013-01-17 2013-01-17 Efficient system for producing sulfuric acid using a spray tower

Publications (1)

Publication Number Publication Date
CN203238034U true CN203238034U (en) 2013-10-16

Family

ID=48040636

Family Applications (1)

Application Number Title Priority Date Filing Date
CN2013200868072U Expired - Lifetime CN203238034U (en) 2013-01-17 2013-02-26 Intermediate absorption subsystem for sulfuric acid production system and bi-absorption system for producing sulfuric acid by oxidizing sulfur dioxide

Country Status (2)

Country Link
CN (1) CN203238034U (en)
CA (1) CA2802885A1 (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108698825A (en) * 2016-03-04 2018-10-23 蒂森克虏伯工业解决方案股份公司 The method and apparatus for being used to prepare sulfuric acid

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10532929B2 (en) 2016-05-03 2020-01-14 Chemetics Inc. Energy efficient sulfuric acid system for humid environments
EP4211073B1 (en) 2020-09-09 2024-10-30 Chemetics Inc. System and method for producing sulfur dioxide and associated sulfuric acid plant
WO2023097389A1 (en) 2021-12-03 2023-06-08 Chemetics Inc. Systems and methods for producing sulfuric acid or liquefied sulfur dioxide

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108698825A (en) * 2016-03-04 2018-10-23 蒂森克虏伯工业解决方案股份公司 The method and apparatus for being used to prepare sulfuric acid

Also Published As

Publication number Publication date
CA2802885A1 (en) 2013-04-01

Similar Documents

Publication Publication Date Title
CN203238034U (en) Intermediate absorption subsystem for sulfuric acid production system and bi-absorption system for producing sulfuric acid by oxidizing sulfur dioxide
CA1256671A (en) Heat recovery from concentrated sulfuric acid
EP2990096A1 (en) Method and apparatus for treating acidic tail gas by using ammonia process flue gas
CN103987443B (en) The nitric acid production improved
CA2968771C (en) Process and plant for improved energy-efficient production of sulfuric acid
CN103920384B (en) A kind of non-pressure process absorbs the equipment of high concentration nitrogen oxide
CA3030835C (en) Plant and process for producing nitric acid
US10556795B2 (en) Single contact, single absorption system for producing sulfuric acid with high conversion efficiency
CN103011092A (en) Technique for preparing sulfuric acid from SO2 by non-equilibrium state high-concentration twice conversion
CN103318850A (en) Low-temperature waste heat recovery system for pyrite and metallurgical off-gas acid making device
CN104495757A (en) System for removing low-temperature thermal energy generated during adsorption of SO3 from sulfuric acid production device
EP3060518B1 (en) Process for operating a sulfuric acid plant
US20150315022A1 (en) Contact apparatus for oxidizing sulfur dioxide and systems for producing sulfuric acid
CN101759156A (en) Two-stage absorption process of fuming sulfuric acid system and equipment thereof
CN106215646B (en) Spent solution regeneration system, cooling system and its regenerated acid production method and cooling means
CN103407971A (en) Novel technology for production of liquid sulfur dioxide
US10532929B2 (en) Energy efficient sulfuric acid system for humid environments
CN203612956U (en) Low-temperature waste heat recovery system used in pyrite and smelting exhaust gas acid preparing device
CN103030115B (en) United acid manufacturing method by utilizing sulfuretted hydrogen and sulphur
CN210030052U (en) Energy-saving sulfuric acid production line
CN107983106A (en) A kind of flue gas purification system of low-temperature ammonium method production aluminium oxide
CN201660444U (en) Two-stage absorption apparatus for oleum systems
Verri et al. Integrated production of liquid sulphur dioxide and sulphuric acid via a low-temperature cryogenic process
WO2023097389A1 (en) Systems and methods for producing sulfuric acid or liquefied sulfur dioxide
CN203461821U (en) Sulfuric acid heat exchange system capable of effectively reducing cost

Legal Events

Date Code Title Description
C14 Grant of patent or utility model
GR01 Patent grant
CX01 Expiry of patent term
CX01 Expiry of patent term

Granted publication date: 20131016