CN108069406B - Regeneration method of alkylation waste sulfuric acid - Google Patents
Regeneration method of alkylation waste sulfuric acid Download PDFInfo
- Publication number
- CN108069406B CN108069406B CN201611002400.1A CN201611002400A CN108069406B CN 108069406 B CN108069406 B CN 108069406B CN 201611002400 A CN201611002400 A CN 201611002400A CN 108069406 B CN108069406 B CN 108069406B
- Authority
- CN
- China
- Prior art keywords
- sulfuric acid
- reactor
- regeneration
- heat carrier
- waste
- 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.)
- Active
Links
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
- C01B17/90—Separation; Purification
- C01B17/92—Recovery from acid tar or the like, e.g. alkylation acids
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Catalysts (AREA)
Abstract
The invention discloses a regeneration method of alkylation waste sulfuric acid, which comprises the following steps: the waste sulfuric acid generated in the alkylation reaction is subjected to heat exchange through a heat exchanger and is mixed with the partially circulated regenerated sulfuric acid at the bottom of the regeneration reactor, a mixed liquid-phase material enters from the top of the regeneration reactor, flows through a first filler layer filled with a heat carrier, is uniformly dispersed and absorbs mass transfer in the first filler layer, flows through a second filler layer filled with the heat carrier, organic matters in the liquid-phase material are coked and carbonized on the surface of the high-temperature heat carrier and are attached to the surface of the heat carrier, the regenerated sulfuric acid without the organic matters is discharged from the bottom of the regeneration reactor, is partially circulated back to the regeneration reactor, is partially cooled, filtered, is mixed with fuming sulfuric acid and then returns to an alkylation production device for continuous use. Aiming at the defects in the prior art, the invention provides a regeneration method of alkylation waste sulfuric acid, which has the advantages of low operation temperature, mild reaction conditions, safe reaction process, low energy consumption and the like.
Description
Technical Field
The invention relates to a method for regenerating waste sulfuric acid generated in alkylation reaction.
Background
in order to improve the quality of gasoline, the light hydrocarbon oil formed after alkylation is added into gasoline, concentrated sulfuric acid is commonly used as a catalyst in the alkylation reaction, about 0.1t of waste sulfuric acid is generally generated when 1t of light hydrocarbon oil is produced, and the components of the waste sulfuric acid except 80-95% of H2SO4Besides, it also contains 3% -8% of organic matter and 2% -8% of water, in which the organic matter mainly is high-molecular olefine, diene, alkyl sulfonic acid, sulfuric ester and mercaptan, etc. The waste alkylated acid is black and sticky, has strong corrosivity and unstable property, emits special odor, has great harm to people and livestock and environment, has no recycling value and needs to be effectively treated.
The methods for treating the alkylated waste acid mainly comprise the following methods: freezing crystallization, solvent extraction, ammonium sulfate and phosphate fertilizer generation, high-temperature pyrolysis, white carbon black and antirust oil generation, oxidation and the like.
CN1031821A discloses a method for producing white carbon black by using alkylated waste sulfuric acid, which comprises diluting waste acid with water according to a certain proportion, standing and separating dilute sulfuric acid and polymer oil to obtain dilute sulfuric acid with a concentration of 7% ~ 18%, wherein the dilute sulfuric acid is used for producing white carbon black, and the polymer oil is used as fuel oil.
CN1034903A discloses a method for recovering waste acid containing organic matters by a catalytic oxidation method, which comprises the steps of firstly increasing the concentration of waste sulfuric acid by a distillation or solvent extraction method, then adding an Hg ~ Co ~ Ba ~ Ca catalyst into an oxidation device, oxidizing the organic matters under the conditions of normal pressure and 300 ~ 330 ℃, and generating a large amount of sulfur trioxide gas in the oxidation process.
CN103771353A discloses a regeneration method of waste alkylated sulfuric acid, which adopts H2O2、O3、HNO3、NOXUnder the condition that any one of the sulfuric acid and the sulfuric acid is used as an oxidizing agent, the waste sulfuric acid and aluminum silicate or silicon dioxide and the like are subjected to oxidation reaction to generate CO2、N2、H2And O. In the reaction process, the regenerated sulfuric acid needs to be stripped after the oxidant is introduced, so that the energy consumption of sulfuric acid stripping is increased.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a regeneration method of alkylation waste sulfuric acid, which has the advantages of low operation temperature, mild reaction conditions, safe reaction process, low energy consumption and the like.
the regeneration method of the alkylation waste sulfuric acid comprises the following steps that waste sulfuric acid generated in an alkylation reaction is subjected to heat exchange through a heat exchanger and is mixed with partially circulated regenerated sulfuric acid at the bottom of a regeneration reactor, a mixed liquid ~ phase material enters from the top of the regeneration reactor and flows through a first filler layer filled with a heat carrier, wherein the temperature of the first filler layer is 100 ~ 300 ℃, the liquid ~ phase material is uniformly dispersed and absorbed in the first filler layer and then flows through a second filler layer filled with the heat carrier, the temperature of a bed layer of the second filler is 500 ~ 700 ℃, preferably 550 ~ 650 ℃, organic matters in the liquid ~ phase material are coked on the surface of the high ~ temperature heat carrier and are attached to the surface of the heat carrier, the regenerated sulfuric acid removed with the organic matters is discharged from the bottom of the regeneration reactor, part of the regenerated sulfuric acid is circulated back to the regeneration reactor, part of the regenerated sulfuric acid is cooled and filtered, and then the regenerated sulfuric acid is.
in the method, the waste sulfuric acid is subjected to heat exchange through a heat exchanger until the temperature is 80 ~ 180 ℃, and preferably 110 ~ 150 ℃.
in the method, the ratio of the height of the first packed bed layer to the height of the second packed bed layer is 1:1 ~ 1.4.
in the method, the heat carrier filled in the packed bed layer is one or more of aluminum silicate, silicon dioxide or aluminum oxide and the like, the shape of the heat carrier can be spherical, strip ~ shaped and the like, the heat carrier is preferably spherical, the particle size of the heat carrier is 5 ~ 20mm, the particle size of the heat carrier is preferably 8 ~ 15mm, the heat carrier filled in the first packed bed layer strengthens the distribution of low ~ temperature waste acid, improves the absorption and dissolution of the low ~ temperature waste acid on sulfur trioxide, reduces the emission of waste gas, and the heat carrier filled in the second packed bed layer strengthens the distribution of the waste acid, absorbs heat, provides a coking and carbonizing surface of organic matters and the like.
In the method, a heating facility is not arranged at the low-temperature section of the first packing bed layer of the regeneration reactor to avoid the decomposition of sulfuric acid, and the low-temperature liquid-phase material in the first packing bed layer absorbs the sulfur trioxide volatilized by the second packing bed layer to reduce the emission of the sulfur trioxide. The heating mode of the second filler bed layer preferably adopts microwave heating, the heat-carrying agent and the sulfuric acid have stronger heat absorption performance to the microwave, the microwave heating speed is high and more uniform, and the temperature distribution of the second filler bed layer can be ensured to be uniform.
In the method, the second filler bed layer of the regeneration reactor is heated by adopting the waveguide for microwave heating, and incoherent synthesis is carried out on a plurality of groups of waveguides, so that the waveguide power is maximized.
in the method, the retention time of the liquid ~ phase material in the reactor is 15 ~ 45 seconds, preferably 20 ~ 35 seconds.
in the method, part of the regenerated sulfuric acid is circulated back to the top of the reactor through a circulating pump and mixed with the alkylated waste sulfuric acid after heat exchange, and part of the regenerated sulfuric acid is discharged to a filter for filtration after heat exchange, wherein the ratio of the circulation volume to the external discharge volume is 1: 0.2 ~ 1, and preferably 1: 0.3 ~ 0.7.
In the method, the filtered concentrated sulfuric acid is cooled to normal temperature by a cooler and then is mixed with fuming sulfuric acid in a pipeline mixer according to a certain proportion to obtain 98.5 percent concentrated sulfuric acid, and the concentrated sulfuric acid is sent to an alkylation production device for reuse.
In the method, the waste sulfuric acid in the regeneration reactor is contacted with a heat carrier, a local boiling phenomenon exists, a part of generated sulfur trioxide and water vapor gas is discharged from the top of the reactor, and the discharged gas can be sent to a waste gas treatment device or a sulfur device for treatment.
in the method, the regeneration reactor can be continuously operated, and when the pressure difference of a second packing bed layer in the reactor is more than 0.5MPa in the later stage of the operation of the reactor, the reactor can be shut down and decoking regeneration can be carried out, the decoking regeneration mode of the reactor is as follows, hot material flow is introduced to sweep and burn the coking and carbon deposition of a reaction bed layer, the carbon deposition is removed, the quantity of the hot material flow is gradually increased by controlling the quantity of the hot material flow, the sulfur trioxide is prevented from being decomposed into sulfur dioxide during regeneration, waste gas generated in the reaction process and waste gas generated in the process of removing the carbon deposition of the reaction bed layer are sent to a waste gas treatment device, a sulfur device or recovery treatment, the hot material flow can be high-temperature flue gas, high-temperature nitrogen or steam, preferably, a sulfur incinerator incineration flue gas, and the temperature of the hot material flow is 500.
The invention also provides an alkylation waste sulfuric acid regeneration device, which comprises a reactor, a circulating pump, a heat exchanger, a filter, a cooler, a pipeline mixer and a waste sulfuric acid storage tank; wherein the material export of waste sulfuric acid storage tank and the cold material access connection of heat exchanger, the cold material export of heat exchanger is through the waste sulfuric acid access connection at pipeline and reactor top, reactor bottom sulphuric acid export is through pipeline and circulating pump access connection, the circulating pump export divides two the tunnel, merge into the connecting line of the cold material export of heat exchanger and reactor top entry all the way, the hot material access connection with the heat exchanger all the way, the hot material export of heat exchanger is through pipeline and filter material access connection, the material export of filter is through the hot material import of pipeline and cooler, the hot material export of cooler is through pipeline and tube mixer access connection, tube mixer exit linkage to alkylation apparatus, tube mixer upper portion sets up fuming sulfuric acid import.
In the regeneration device, the bottom of the reactor is provided with a hot material flow inlet which is communicated with a hot material flow pipe through a pipeline, the top of the reactor is provided with a gas outlet which is connected with a waste gas pipeline through a pipeline, and the waste gas pipeline is connected to a waste gas treatment device or a sulfur device.
In the regeneration device, a plurality of groups of filters can be arranged, at least two groups of filters are switched, and the requirement of the filtering precision is less than 0.5 mm.
Other techniques of the present invention, such as circulating pumps, waste sulfuric acid heating, sulfuric acid filtration, material heat exchange and cooling, are well known to those skilled in the art.
Compared with the prior art, the method has the following advantages:
1. The liquid phase circulation of the waste sulfuric acid in the reactor can avoid the large-scale gasification and decomposition of the waste sulfuric acid in a high-temperature environment; the reactor is filled with a heat carrier, the heat carrier at the high-temperature section is in a high-temperature state, the heat carrier provides a hot spot environment for organic matters in the waste sulfuric acid, and the heat carrier is favorable for gathering, coking and carbonizing the organic matters on the surface of the heat carrier, so that the aim of effectively trapping and separating the organic matters is fulfilled.
2. A low-temperature section (a first packing layer) and a high-temperature section (a second packing layer) are arranged in the regeneration reactor, the low-temperature section can absorb sulfur trioxide gasified and decomposed in the high-temperature section, and the emission of waste gas pollutants is reduced; the high-temperature section adopts microwave heating, heating is uniform and rapid, and waste acid can be continuously regenerated, so that continuous recycling and use of waste sulfuric acid regeneration are realized, the intermediate storage process of waste sulfuric acid is reduced, and the discharge and leakage of waste sulfuric acid pollutants are reduced; a small amount of sulfur-containing waste gas produced in the waste acid regeneration process is sent to a waste gas treatment device or a sulfur device for treatment.
3. The method and the device are applied to treating the waste sulfuric acid, the removal rate of organic matters is high, the waste acid is not required to be diluted, the device has low operation energy consumption and low maintenance cost, and no pollutant is discharged in the regeneration process of the waste sulfuric acid.
drawings
FIG. 1 is a schematic flow diagram of the regeneration process of the present invention.
1-hot stream; 2-regeneration reactor; 3-waste gas; 4-a circulating pump; 5-circulating the liquid; 6-efflux liquid; 7-a heat exchanger; 8-a filter; 9-a cooler; 10-a line mixer; 11-regenerated sulfuric acid; 12-a waveguide; 13-spent sulfuric acid storage tank; 14-oleum.
Detailed Description
The technical solution and effect of the method of the present invention are further illustrated by the following specific examples, but are not limited to the following examples.
As shown in figure 1, the method for regenerating the alkylated waste sulfuric acid is realized by pumping the alkylated waste sulfuric acid from a waste sulfuric acid storage tank 13 to a heat exchanger 7 for heat exchange to 80 ~ 180 ℃, mixing the alkylated waste sulfuric acid with part of circulating liquid 5, and then entering a regeneration reactor 2, wherein the temperature of a first filler bed layer of the regeneration reactor 2 is 100 ~ 300 ℃, the temperature of a second filler bed layer is 500 ~ 700 ℃, the second filler bed layer is heated by adopting a waveguide 12 microwave, as a large amount of liquid circulates in the reactor 2, the sulfuric acid in the regeneration reactor 2 is mainly in a liquid state, organic matters in the liquid state are contacted with a heat carrier of the bed layer, the surface of a high ~ temperature heat carrier coke in a high ~ temperature section of the second filler bed layer is carbonized and attached to the surface of the heat carrier, so that the purpose of separating and purifying the organic matters in the waste;
In the final stage of the operation of the regeneration reactor 2, when the pressure drop of the bed layer of the reactor 2 reaches 0.5MPa, the reactor is shut down and decoking regeneration is carried out, and the decoking regeneration mode of the reactor is as follows: introducing a hot material flow 1 to sweep and burn the coking and carbon deposition of the reaction bed layer, and removing the carbon deposition; circulating part of the regenerated sulfuric acid through a circulating pump 4, discharging part of discharged liquid 6 after heat exchange through a heat exchanger 7 to a filter 8, cooling the filtered liquid to normal temperature through a cooler 9, mixing the filtered liquid and fuming sulfuric acid 14 in a pipeline mixer 10 according to a certain proportion to obtain 98.5% concentrated sulfuric acid 11, and conveying the concentrated sulfuric acid 11 to an alkylation production device for reuse; and part of sulfur trioxide and steam gas generated in the regeneration reaction process is discharged from the top of the reactor 2, and the waste gas 3 is discharged to a waste gas treatment device or a sulfur device for treatment.
Example 1
After heat exchange is carried out on 90wt% of waste sulfuric acid to 120 ℃, the waste sulfuric acid and circulating sulfuric acid liquid are mixed and enter a reactor 2, the ratio of a first packing bed layer to a second packing bed layer in the reactor is 1:1, a heat carrier of the second packing bed layer is heated to about 600 ℃ by microwave, 10mm silicon dioxide spherical particles are selected as heat carriers of the first packing bed layer and the second packing bed layer, and incineration flue gas of a sulfur incinerator is adopted as a regenerative heat material flow 1 of the reactor 2. Coking and carbon deposition are carried out on the waste sulfuric acid in a hot bed layer of a reactor 2, the treated sulfuric acid is discharged outside according to the ratio of 1:0.4, heat is exchanged through a heat exchanger to a filter to filter micro particles, and the filtered sulfuric acid and fuming sulfuric acid are mixed into 98.5% concentrated sulfuric acid and then are sent to an alkylation device for use.
Claims (10)
1. A regeneration method of alkylation waste sulfuric acid is characterized by comprising the following steps of firstly exchanging heat of waste sulfuric acid generated in an alkylation reaction through a heat exchanger, mixing the waste sulfuric acid with partially circulated regenerated sulfuric acid at the bottom of a regeneration reactor, feeding a mixed liquid ~ phase material from the top of the regeneration reactor, firstly flowing through a first filler layer filled with a heat carrier, wherein the temperature of the first filler layer is 100 ~ 300 ℃, uniformly dispersing and absorbing the liquid ~ phase material in the first filler layer, then flowing through a second filler layer filled with the heat carrier, wherein the temperature of a bed layer of the second filler is 500 ~ 700 ℃, coking and carbonizing organic matters in the liquid ~ phase material on the surface of a high ~ temperature heat carrier, attaching to the surface of the heat carrier, discharging the regenerated sulfuric acid without the organic matters from the bottom of the regeneration reactor, partially circulating back to the regeneration reactor, partially cooling and filtering, then mixing with fuming sulfuric acid, and returning to an alkylation production device for continuous use.
2. the method according to claim 1, wherein the waste sulfuric acid is subjected to heat exchange by a heat exchanger to reach a temperature of 80 ~ 180 ℃.
3. the method of claim 1, wherein the second packing bed temperature is 550 ~ 650 ℃.
4. the method of claim 1, wherein the ratio of the height of the first packed bed ~ the height of the second packed bed is from 1:1 ~ 1.4.
5. the method according to claim 1, characterized in that the heat carrier filled in the packed bed layer is one or more of aluminum silicate, silicon dioxide or aluminum oxide, and the particle size of the heat carrier is 5 ~ 20 mm.
6. The method of claim 1, wherein: the heating mode of the second filler bed layer adopts microwave heating.
7. the method according ~ claim 1, wherein the residence time of the liquid-phase material in the reactor is 15 ~ 45 seconds.
8. the method according to claim 1, characterized in that part of the regenerated sulfuric acid is circulated back to the top of the reactor through a circulating pump and mixed with the alkylated waste sulfuric acid after heat exchange, and part of the regenerated sulfuric acid is discharged to a filter for filtration after heat exchange, wherein the ratio of the circulating capacity to the external discharge capacity is 1: 0.2 ~ 1.
9. the method of claim 1, wherein: and cooling the filtered concentrated sulfuric acid to normal temperature by a cooler, mixing the concentrated sulfuric acid with fuming sulfuric acid according to a certain proportion to obtain 98.5% concentrated sulfuric acid, and conveying the concentrated sulfuric acid to an alkylation production device for reuse.
10. The method of claim 1, wherein: and (3) continuously operating the regeneration reactor, and stopping the reactor and performing decoking regeneration when the pressure difference of a second packing bed layer in the reactor is more than 0.5MPa at the final stage of the operation of the reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611002400.1A CN108069406B (en) | 2016-11-15 | 2016-11-15 | Regeneration method of alkylation waste sulfuric acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611002400.1A CN108069406B (en) | 2016-11-15 | 2016-11-15 | Regeneration method of alkylation waste sulfuric acid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108069406A CN108069406A (en) | 2018-05-25 |
| CN108069406B true CN108069406B (en) | 2019-12-13 |
Family
ID=62162477
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201611002400.1A Active CN108069406B (en) | 2016-11-15 | 2016-11-15 | Regeneration method of alkylation waste sulfuric acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108069406B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109095442B (en) * | 2018-08-27 | 2022-01-11 | 青岛惠城环保科技股份有限公司 | Method for treating waste sulfuric acid discharged in alkylation production process |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1154946A (en) * | 1996-01-14 | 1997-07-23 | 王东生 | Method for regenerating waste sulfuric acid for alkylation |
| CN102951617A (en) * | 2012-10-18 | 2013-03-06 | 陕西比迪欧化工有限公司 | Purifying treatment system and method of waste sulfuric acid |
| CN103771353A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Regeneration method for alkylated waste sulfuric acid |
| CN103979502A (en) * | 2014-04-30 | 2014-08-13 | 上海倍能化工技术有限公司 | Regeneration method of waste sulfuric acid, and sulfuric acid produced by the method |
| CN105858622A (en) * | 2016-05-19 | 2016-08-17 | 广西南宁东和新赢环保技术有限公司 | Alkylation waste sulfuric acid resource recycling method |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0970016A2 (en) * | 1997-03-31 | 2000-01-12 | Waterworks International, Inc. | Sulfuric acid purification process |
-
2016
- 2016-11-15 CN CN201611002400.1A patent/CN108069406B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1154946A (en) * | 1996-01-14 | 1997-07-23 | 王东生 | Method for regenerating waste sulfuric acid for alkylation |
| CN102951617A (en) * | 2012-10-18 | 2013-03-06 | 陕西比迪欧化工有限公司 | Purifying treatment system and method of waste sulfuric acid |
| CN103771353A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Regeneration method for alkylated waste sulfuric acid |
| CN103979502A (en) * | 2014-04-30 | 2014-08-13 | 上海倍能化工技术有限公司 | Regeneration method of waste sulfuric acid, and sulfuric acid produced by the method |
| CN105858622A (en) * | 2016-05-19 | 2016-08-17 | 广西南宁东和新赢环保技术有限公司 | Alkylation waste sulfuric acid resource recycling method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108069406A (en) | 2018-05-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102585918B (en) | Process and system for deeply removing tar through biomass gas coupling adsorption | |
| CN103771353B (en) | A kind of renovation process of waste sulfuric acid from alkylation | |
| CN104548902B (en) | Acetylene gas purifier and technique thereof | |
| CN107792836B (en) | Regeneration method and device of alkylation waste sulfuric acid | |
| CN206553478U (en) | Coal oven dithio-gas purifier | |
| CN102585917B (en) | Process and system for deeply removing tar by biomass gas cooling-absorption coupling | |
| CN101820969A (en) | The method and system of the wash solution that contains amine that obtains in the purification for gas process is used for regenerating | |
| CN103446853A (en) | Exhaust gas recovery device and exhaust gas recovery system for processing copper-clad plate | |
| CN102220169B (en) | Pyrolysis gas quenching structural unit of CPP (Catalytic Pyrolysis Production) and process thereof | |
| CN104229746A (en) | New method for preparing sulfur from alkylated waste acid | |
| CN108069406B (en) | Regeneration method of alkylation waste sulfuric acid | |
| CN205528636U (en) | Blue charcoal coal gas integrated device | |
| CN210826085U (en) | Blast furnace gas catalytic desulfurization device | |
| CN102381688A (en) | Concentrated sulfuric acid preparation method using hydrogen sulfide in manufactured gas | |
| CN106744716A (en) | A kind of method that waste sulfuric acid from alkylation Pintsch process produces sulfuric acid | |
| CN105542874A (en) | Integrated process and device for semicoke coal gas | |
| CN101579603A (en) | Process for advanced treatment of waste alkali in hydrogen sulfide removal | |
| CN107311117B (en) | Clean production process and device for combined treatment of sulfur recovery and alkylated waste acid | |
| CN207468199U (en) | For the device of sulphur recovery and alkylation spent acid Combined Treatment clean manufacturing | |
| CN105668524A (en) | Method for treating waste sulfuric acid | |
| CN105502308B (en) | A kind of processing method of Waste Sulfuric Acid | |
| CN114854461B (en) | Method for regenerating hot lean oil under negative pressure debenzolization process condition | |
| CN110591769A (en) | Blast furnace gas catalytic desulfurization device and method | |
| CN104927906B (en) | The device and its sulfur removal technology of sulfide in a kind of deep removal light dydrocarbon | |
| CN210752010U (en) | Desulphurization unit of sulphur process gas among hydrogen fluoride preparation process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |