CN108070416B - Adsorption desulfurization process for liquefied petroleum gas - Google Patents

Adsorption desulfurization process for liquefied petroleum gas Download PDF

Info

Publication number
CN108070416B
CN108070416B CN201610991600.8A CN201610991600A CN108070416B CN 108070416 B CN108070416 B CN 108070416B CN 201610991600 A CN201610991600 A CN 201610991600A CN 108070416 B CN108070416 B CN 108070416B
Authority
CN
China
Prior art keywords
adsorbent
adsorption
molecular sieve
fixed bed
liquefied petroleum
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
Application number
CN201610991600.8A
Other languages
Chinese (zh)
Other versions
CN108070416A (en
Inventor
刘新宇
崔凯燕
王海波
乔凯
王领民
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.)
China Petroleum and Chemical Corp
Sinopec Fushun Research Institute of Petroleum and Petrochemicals
Original Assignee
China Petroleum and Chemical Corp
Sinopec Fushun Research Institute of Petroleum and Petrochemicals
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 China Petroleum and Chemical Corp, Sinopec Fushun Research Institute of Petroleum and Petrochemicals filed Critical China Petroleum and Chemical Corp
Priority to CN201610991600.8A priority Critical patent/CN108070416B/en
Publication of CN108070416A publication Critical patent/CN108070416A/en
Application granted granted Critical
Publication of CN108070416B publication Critical patent/CN108070416B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/12—Liquefied petroleum gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/104—Alumina
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B01D2253/108—Zeolites
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/112—Metals or metal compounds not provided for in B01D2253/104 or B01D2253/106
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/304—Hydrogen sulfide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/306—Organic sulfur compounds, e.g. mercaptans
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/542—Adsorption of impurities during preparation or upgrading of a fuel

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)

Abstract

The invention discloses a liquefied petroleum gas adsorption desulfurization process, which adopts at least two fixed bed reactors, wherein liquefied petroleum gas is firstly sent into the fixed bed reactor filled with an adsorbent to carry out adsorption desulfurization reaction, after the adsorbent reaches an adsorption saturation state, the liquefied petroleum gas is switched into the other fixed bed reactor filled with the adsorbent to continue the adsorption desulfurization reaction, and hydrogen is introduced into the fixed bed reactor reaching the adsorption saturation state to carry out regeneration. The adsorption desulfurization process can remove organic sulfide in the liquefied petroleum gas, and has the advantages of no alkali residue discharge, high desulfurization precision and the like.

Description

Adsorption desulfurization process for liquefied petroleum gas
Technical Field
The invention relates to a liquefied petroleum gas desulfurization process, in particular to a process for removing sulfur in liquefied petroleum gas by an adsorption method.
Background
With the increasing amount of high-sulfur crude oil processed in China, the gas components generated in the oil refining process, especially various sulfur-containing compounds in liquefied petroleum gas, are increasing. In addition to hydrogen sulphide, there are also organic sulphides such as mercaptans, sulphides, carbonyl sulphides and disulphides. The existence of the sulfur-containing compounds can cause corrosion to equipment in the subsequent processing process of the liquefied petroleum gas and poison the catalyst; when the liquefied petroleum gas is used as fuel, sulfur oxides are generated to form acid rain, and the environment is polluted. Therefore, the method for desulfurizing the liquefied petroleum gas has economic benefits and environmental protection significance.
If the liquefied petroleum gas is subjected to sulfide removal, the method can be divided into inorganic sulfur removal and organic sulfur removal. The inorganic sulfur in liquefied petroleum gas is mainly hydrogen sulfide, and the industrial method for removing hydrogen sulfide is quite mature, so the key point of liquefied petroleum gas desulfurization is that the difficulty is to remove organic sulfur. For how to remove organic sulfur in liquefied petroleum gas, researchers and organizations at home and abroad adopt various methods.
At present, the domestic application of the method for removing organic sulfur in liquefied petroleum gas at most is also the method for removing mercaptan by extraction-catalytic oxidation of Merox alkali liquor, which is applied in the last 70 th century. The process comprises contacting a basic solution (including a regenerated basic solution) with a hydrocarbon stream containing mercaptans, the basic solution reacting with mercaptans to form mercaptides; mixing the alkali liquor containing mercaptide with the injected oxidizing gas and the oxidation catalyst, converting the mercaptide into disulfide and regenerating the alkali liquor, finally separating the regenerated alkali liquor and the mixture of the disulfide by settling, and returning the regenerated alkali liquor to the extraction system for continuous use. A great number of patents exist for the application and improvement of the method, and U.S. Pat. Nos. 4705620 and 2921020 and domestic patent No. CN1990828A adopt new technologies to improve the separation technology of the mixture of disulfide and the alkali liquor, reduce the content of disulfide in the alkali liquor and improve the desulfurization rate of liquefied petroleum gas. The conventional melox method still has the following problems: (1) the cobalt phthalocyanine catalyst used is in an alkaline phase and is easy to aggregate and deactivate, so that the catalyst is frequently replaced and the cost of the catalyst is quite high; (2) the desulfurization rate is not stable enough, mainly because the concentration of disulfide in the regenerated alkali liquor is difficult to control, the alkali liquor brings the disulfide into the liquefied petroleum gas again, and the total desulfurization rate is reduced; (3) a large amount of waste caustic sludge is generated, and the damage to the surrounding environment is brought. The Merichem company in the United states adopts a fiber membrane contactor technology to promote the mass transfer rate between an alkali liquor phase and a hydrocarbon phase to be greatly improved, thereby improving the utilization rate of the alkali liquor, reducing the consumption of the alkali liquor and reducing the discharge of alkali residues (USP 4124494 and USP 4159964). But the removal rate of mercaptan by the fiber membrane desulfurization process is still influenced by the regeneration quality of alkali liquor, and the improvement of the total sulfur removal rate is not obvious; and the method still can produce a certain amount of alkaline residue, which causes pollution to the environment; finally, the process requires high purity of the various media, requires the installation of corresponding filters, and requires periodic cleaning, which increases maintenance costs. Finally, although the refined liquefied petroleum gas using the technology can remove a large amount of sulfur compounds in the liquefied petroleum gas, the sulfur content in the obtained refined liquefied petroleum gas is difficult to reduce below 10ppm due to the change of the concentration of the sulfur compounds in the raw material, so that the sulfur content in the MTBE serving as a gasoline additive exceeds the currently specified 10ppm or less. In summary, only the alkali liquor extraction and the fiber membrane desulfurization technology are applied in the field of liquefied petroleum gas desulfurization on a large scale, but the problems caused by the technology are also many.
Adsorption desulfurization is another commonly used method for removing organic sulfur from liquefied petroleum gas. The method adopts a molecular sieve with certain adsorption capacity, active carbon, metal oxide or composite metal oxide and the like as adsorbents, and separates sulfides from the liquefied petroleum gas by utilizing the effects of physical adsorption, van der waals force, chemical adsorption, complex adsorption and the like formed between the adsorbents and the sulfides. The method has the characteristics of simple and convenient operation, low investment and no pollution. Compared with a simple hydrodesulfurization method, the method can not cause octane number loss. Patent 101450302A teaches a method for preparing a desulfurization adsorbent for tetraolefins and the application thereof, wherein the adsorbent has good selectivity to sulfide, high sulfur capacity, no loss of olefins in the adsorption of the hydrogenation reaction, simple preparation process of the catalyst, and no loss of the adsorbent due to the fixed bed operation. However, there is no mention in this patent of how to regenerate the catalyst saturated with adsorption and how the adsorption effect of the regenerated catalyst compares to before. The patent CN 103614178A also adopts an adsorbent to deeply desulfurize the liquefied petroleum gas, and the adsorbent saturated by the adsorption is regenerated under the condition of nitrogen, and the liquefied petroleum gas desulfurized by the method can meet the requirement of deep processing of mixed C4. However, the adsorption temperature is 0-50 ℃ and the regeneration temperature is 180-260 ℃, in the actual operation, the adsorption process and the regeneration process need to be repeatedly switched, the temperature reduction process needs to consume a long time, and adverse effects are caused to the production. And nitrogen is used as regeneration gas, so that the regeneration effect of the adsorbent and adsorbate which are acted by chemical bonds is poor, the regeneration of the adsorbent is insufficient, and the adsorption capacity of the regenerated adsorbent is influenced. Patent CN 1329937A introduces a molecular sieve-based adsorbent for desulfurization of liquefied petroleum gas, which has large adsorption capacity, high removal rate and convenient regeneration. However, there is no mention of how to effectively connect the adsorption process with the regeneration process, which limits the application. And the existing adsorption desulfurizer has low sulfur capacity, so that the switching between the adsorption process and the regeneration process is very frequent, the cost is overhigh, and the industrial popularization of the technology is not facilitated.
Disclosure of Invention
Although the adsorption-method liquefied petroleum gas desulfurization process has a series of advantages of no alkali slag discharge, high desulfurization precision, no change of olefin composition and the like, the adsorption-method liquefied petroleum gas desulfurization is divided into two processes of adsorbent adsorption desulfurization and adsorbent regeneration, in the prior art, the temperature and pressure conditions in the two processes are greatly different, the process needs to be switched back and forth, the energy consumption and the industrial cost are increased, and the popularization and the application of the method are not facilitated.
The invention provides a novel adsorption desulfurization method, aiming at the problems that in the technical field of desulfurization of the existing liquefied petroleum gas, the sulfur capacity of an adsorption desulfurizer is low, so that the switching between the adsorption process and the regeneration process is very frequent, the difference between the process conditions of the adsorption process and the regeneration process is large, and the process needs to be switched back and forth, so that the energy consumption is high, the industrial cost is high, and the popularization and the application are not facilitated.
The invention provides a liquefied petroleum gas adsorption desulfurization process, which adopts at least two fixed bed reactors, and comprises the following steps: firstly, liquefied petroleum gas is sent into a fixed bed reactor filled with an adsorbent to carry out adsorption desulfurization reaction, after the adsorbent reaches an adsorption saturation state, the liquefied petroleum gas is switched into another fixed bed reactor filled with the adsorbent to continue the adsorption desulfurization reaction, and hydrogen is introduced into the fixed bed reactor reaching the adsorption saturation state to regenerate, wherein the adsorption desulfurization reaction conditions are as follows: the adsorption temperature is 150-200 ℃, the adsorption pressure is 2-4 MPa, and the liquid phase space velocity is 0.5-3 h-1(ii) a The regeneration conditions are as follows: the regeneration temperature is 150-200 ℃, the regeneration pressure is 2-4 MPa, and the space velocity of hydrogen is 100-3000 h-1。
The adsorbent used in the invention is a molecular sieve loaded with metal active components, and the adsorbent is based on weightThe content of the medium molecular sieve is 60-90%, the content of the alumina carrier is 9-39%, and the balance is metal active components. The specific surface area of the adsorbent is 120-350 m2A pore volume of 0.10-0.30 cm3(ii) a bulk density of 0.70 to 0.95g/cm3。
In the above adsorbent, the molecular sieve refers to a molecular sieve having an adsorption function, and is selected from, but not limited to, the following molecular sieves: one or more of the silicoaluminophosphate molecular sieves and the silicoaluminophosphate molecular sieves are preferably one or more of faujasite, A-type zeolite, beta molecular sieve, ZSM series molecular sieve, M (mordenite) type molecular sieve, erionite, MCM series molecular sieve and SAPO series molecular sieve. The faujasite can be one or more of X or Y type molecular sieves, and the ZSM series molecular sieve can be one or more of ZSM-5, ZSM-8, ZSM-11 and ZSM-35. The SAPO series molecular sieve can be one or more of SAPO-5 and SAPO-11. The MCM series molecular sieve may be one or several of MCM-22 and MCM-41 molecular sieves. Further preferably one or more of X-type molecular sieve, Y-type molecular sieve and ZSM-5 molecular sieve. The active metal component is a metal in a VIII group or a VIB group, such as platinum, palladium, one or more of cobalt, molybdenum, nickel and tungsten, preferably cobalt, molybdenum, nickel and tungsten.
The adsorbent also comprises a proper amount of metal additives, wherein the metal additives are one or more of calcium, magnesium, strontium, lanthanum, cerium, praseodymium, iron, zirconium, zinc, copper and silver, and the oxidation state mass fraction of the metal additives is 2-7%. The addition of the metal auxiliary agent can improve the adsorption function of the adsorbent and the hydrodesulfurization efficiency of the saturated adsorbent, and improve the adsorption and regeneration performance of the adsorbent.
In the process, an adsorbent is filled in the fixed bed reactor, the adsorbent comprises an adsorbent A and an adsorbent B, the volume ratio of the adsorbent A to the adsorbent B is 0.1-10, preferably 0.5-5, compared with the composition of the adsorbent B, the molecular sieve of the adsorbent A is one or more of an A-type molecular sieve, an X-type molecular sieve and a ZSM series molecular sieve, preferably the X-type molecular sieve, and the molecular sieve of the adsorbent B is a Y-type molecular sieve, an β type molecular sieve and an M series molecular sievePreferably Y-type molecular sieve. More preferably, the metal active components loaded in the adsorbent A are tungsten and nickel, the mass fraction of tungsten is 5-20% and the mass fraction of nickel is 3-10% in terms of metal oxides, the metal active components loaded in the adsorbent B are cobalt and molybdenum, the mass fraction of cobalt is 3-10% and the mass fraction of molybdenum is 5-20% in terms of metal oxides. The bulk density of the adsorbent A is 0.8-0.95 g/cm3The bulk density of the adsorbent B is 0.7-0.85 g/cm3. The bulk density of the adsorbent A is 0.05-0.2 g/cm higher than that of the adsorbent3。
In the process of the invention, the adsorbent is prepared by the following method:
(1) mixing the molecular sieve with an adhesive, a peptizing agent and an extrusion aid, and kneading and molding to obtain a carrier;
(2) loading a metal active component or loading the metal active component and a metal auxiliary agent on the carrier obtained in the step (1) by adopting an isometric impregnation method, and impregnating, drying and roasting to obtain an adsorbent;
(3) sulfurizing the adsorbent obtained in the step (2) to convert the oxidation state metal loaded on the adsorbent into a sulfurization state;
(4) carrying out reduction reaction on the vulcanized adsorbent obtained in the step (3) to obtain a final adsorbent; the reduction reaction conditions are as follows: the reaction temperature is 260-400 ℃, the pressure is 1-4 MPa, and the volume space velocity of hydrogen is 500-4000 h-1And the reaction time is 4-20 h.
In the above method, the binder is activated alumina or a precursor thereof; the peptizing agent is one or more of inorganic acid, organic acid and strong acid anion salt, the strong acid anion salt is aluminum nitrate, the inorganic acid is one or more of nitric acid, hydrochloric acid and sulfuric acid, and the organic acid is one or more of formic acid, acetic acid, oxalic acid and citric acid; the extrusion aid is a substance capable of assisting in the extrusion molding of the alumina, and is one or more of carbon black, sesbania powder, graphite powder and citric acid.
The molecular sieve refers to a molecular sieve with an adsorption function, and is selected from but not limited to the following molecular sieves: one or more of the silicoaluminophosphate molecular sieves and the silicoaluminophosphate molecular sieves are preferably one or more of faujasite, A-type zeolite, beta molecular sieve, ZSM series molecular sieve, M (mordenite) type molecular sieve, erionite, MCM series molecular sieve and SAPO series molecular sieve. The faujasite can be one or more of X or Y type molecular sieves, and the ZSM series molecular sieve can be one or more of ZSM-5, ZSM-8, ZSM-11 and ZSM-35. The SAPO series molecular sieve can be one or more of SAPO-5 and SAPO-11. The MCM series molecular sieve may be one or several of MCM-22 and MCM-41 molecular sieves. Further preferably one or more of X-type molecular sieve, Y-type molecular sieve and ZSM-5 molecular sieve. The metal active component is a metal in a VIII group or a VIB group, such as platinum, palladium, one or more of cobalt, molybdenum, nickel and tungsten, preferably cobalt, molybdenum, nickel and tungsten.
The adsorbent also comprises a proper amount of metal additives, wherein the metal additives are one or more of calcium, magnesium, strontium, lanthanum, cerium, praseodymium, iron, zirconium, zinc, copper and silver, and the oxidation state mass fraction of the metal additives is 2-7%. The addition of the metal auxiliary agent can improve the adsorption function of the adsorbent and the hydrodesulfurization efficiency of the saturated adsorbent, and improve the adsorption and regeneration performance of the adsorbent.
In the process, the preparation method of the adsorbent is improved, the sulfurized adsorbent is subjected to hydrogenation reduction reaction at a higher temperature, and the part of sulfurized metal generates more anion vacancies through the hydrogenation reduction reaction, so that the sulfurized metal can adsorb more sulfides, and the sulfur adsorption capacity of the adsorbent is remarkably improved. The energy consumption and the cost increase caused by the over-small sulfur adsorption capacity of the adsorbent are reduced to a certain extent.
Compared with the prior art, the adsorption desulfurization process can remove the organic sulfide in the liquefied petroleum gas, and has the advantages of no alkali slag discharge, high desulfurization precision (the sulfur-containing compound can be removed to be less than 10 ppm), no change of the composition of each component in the liquefied petroleum gas and the like.
In the process, the fixed bed reactor is adopted, and the reaction temperature and the pressure in the adsorption process and the regeneration process are kept consistent, so that the energy consumption and the cost increase caused by temperature change or pressure change in the switching process of the two processes are avoided; meanwhile, the adsorption capacity of the adsorbent is remarkably improved, the sulfur adsorption capacity is improved by 25%, the interaction between sulfide and metal active sites can be enhanced due to the adsorption process at high temperature (150-200 ℃), and the chemical adsorption effect is enhanced although the physical adsorption effect is weakened, so that the adsorption capacity is improved to a certain extent. The adsorption process and the adsorbent regeneration process are simply linked, and long-term operation can be realized.
In the process, by adopting an adsorbent grading mode and through different types and contents of molecular sieves with different contents and different proportions of loaded active metals, multiple organic sulfides in the liquefied petroleum gas can be removed in a targeted manner, the molecular sieve required by the adsorbent A has a unique pore structure and acid property, and the synergistic effect among different active metals is beneficial to removing thiol sulfides in the liquefied petroleum gas, the molecular sieve required by the adsorbent B has a pore structure and acid property, and the synergistic effect among different active metals is beneficial to removing disulfide compounds in the liquefied petroleum gas. Therefore, the grading method can effectively remove various sulfides in the liquefied petroleum gas and achieve the aim of deep desulfurization.
In the process, the preparation method of the adsorbent is improved, the sulfurized adsorbent is subjected to hydrogenation reduction reaction at a higher temperature, and the part of sulfurized metal generates more anion vacancies through the hydrogenation reduction reaction, so that the sulfurized metal can adsorb more sulfides, and the sulfur adsorption capacity of the adsorbent is remarkably improved. The energy consumption and the cost increase caused by the over-small sulfur adsorption capacity of the adsorbent are reduced to a certain extent.
Detailed Description
The present invention is further described in detail with reference to the following examples, which are not intended to limit the scope of the present invention, and those skilled in the art can appropriately extend the scope of the present invention in combination with the description and the entirety of the present invention. The specific surface area and the pore volume in the process are measured by adopting a low-temperature liquid nitrogen adsorption method. The sulfur content analysis adopts a coulombic sulfur analysis method.
The process for adsorbing, regenerating and desulfurizing the liquefied petroleum gas comprises the following steps: filling an adsorbent into a fixed bed reactor, introducing an unrefined liquefied petroleum gas raw material at one end of the fixed bed reactor at a certain airspeed, then adsorbing and removing organic sulfides in the liquefied petroleum gas by the adsorbent at a certain temperature and under a certain pressure, detecting the content of sulfur-containing compounds in the adsorbed liquefied petroleum gas, immediately switching the liquefied petroleum gas into another fixed bed reactor filled with a fresh adsorbent when the content of the sulfur-containing compounds in the adsorbed liquefied petroleum gas exceeds a certain range, and continuously adsorbing the liquefied petroleum gas according to the same conditions; and the fixed bed reactor filled with the original adsorbent saturated by adsorption is regenerated under the same conditions, hydrogen is continuously introduced in the regeneration process, the hydrodesulfurization reaction is realized to achieve the full regeneration of the adsorbent, the content of hydrogen sulfide in tail gas is detected, the regeneration is stopped when the content of hydrogen sulfide in the tail gas is reduced to a certain concentration, and the next adsorption process is waited after the regeneration of the adsorbent is considered to be finished. The long-term operation of the desulfurization process can be realized and the purpose of deep desulfurization can be achieved by switching the adsorption and hydrogenation regeneration processes of at least two fixed bed reactors.
Example 1:
preparation of the adsorbent
Adsorbent A
Taking Al2O350g of distilled water and 8g of concentrated nitric acid are added and mixed evenly, 100g of 13X type molecular sieve and 3g of sesbania powder are added into the mixture, extruded into strips and formed, dried for 4 hours at 110 ℃, calcined for 5 hours at 550 ℃, and the carrier of the catalyst is prepared. 15g of ammonium metatungstate and 3g of nickel nitrate are dissolved by distilled water to prepare 200g of solution. The support was immersed in the solution and shaken for about 6 hours, after which the support was filtered off, dried at 110 ℃ for 6 hours and then calcined at 550 ℃ for 5 hours. The tungsten-nickel loaded adsorbent A is prepared.
Adsorbent B
Taking Al2O320g, adding 30g of distilled water and 8g of concentrated nitric acid, uniformly mixing, adding 100g of Y-type molecular sieve and 3g of sesbania powder into the mixture, extruding into strips, forming, drying at 110 ℃ for 4 hours, and calcining at 550 ℃ for 5 hours to prepare the carrier of the catalyst. 15g of ammonium molybdate and 3g of cobalt acetate are dissolved by distilled water to prepare 200g of solution. The support was immersed in the solution and shaken for about 6 hours, after which the support was filtered off, dried at 110 ℃ for 6 hours and then calcined at 550 ℃ for 5 hours. The adsorbent B loaded with cobalt and molybdenum is prepared.
And (3) sulfurization and reduction: an adsorbent A and an adsorbent B were packed in a fixed bed reactor, and the packing volume ratio of the adsorbent A to the adsorbent B was 1.5. Heating to 170 ℃ at the speed of 30 ℃/H, and starting to introduce H2S/H2(the volume concentration of hydrogen sulfide is 10 percent), the pressure is ensured to be 1MPa, and the air space velocity is 50h-1Then heating to 220 ℃ at the speed of 3 ℃/h, keeping the temperature for 15h, heating to 290 ℃ at the speed of 4 ℃/h, keeping the temperature for 8h, heating to 360 ℃ at the speed of 6 ℃/h, and keeping the temperature for 8 h. Cooling to 300 ℃, introducing hydrogen and setting the volume space velocity at 1000h-1The pressure is 2MPa, and the reaction time is 10 h. The adsorbent after sulfidation is ready for use.
After dewatering the liquefied gas raw material, introducing the liquefied gas raw material into a fixed bed reactor for adsorption and absorption, wherein the adsorption temperature is 150 ℃, the adsorption pressure is 4MPa, and the space velocity of a liquid phase is 1h-1. After the adsorbed gas is detected to be overproof in sulfide, immediately switching the feed gas into another fixed bed reactor filled with a fresh adsorbent for gas purification; the original fixed bed reactor filled with the adsorption saturated adsorbent is used for 1000h-1Is introduced into H2Purging, wherein temperature and pressure conditions are not changed, purging is carried out for 20h, and the adsorption process can be carried out again after the regeneration of the adsorbent is finished. The adsorbent can be reused for more than 1000 times while keeping the adsorption capacity unchanged. The adsorption-regeneration results are shown in table 1.
Example 2
Preparation of the adsorbent
Adsorbent A
Taking Al2O320g, addAdding 50g of distilled water and 8g of concentrated nitric acid, uniformly mixing, adding 100g of 13X molecular sieve and 3g of sesbania powder into the mixture, extruding into strips, drying at 110 ℃ for 4 hours, and calcining at 550 ℃ for 5 hours to prepare the carrier of the catalyst. 15g of ammonium metatungstate, 5g of nickel nitrate and 1g of cerium nitrate are dissolved by distilled water to prepare 200g of solution. The support was immersed in the solution and shaken for about 6 hours, after which the support was filtered off, dried at 110 ℃ for 6 hours and then calcined at 550 ℃ for 5 hours. The tungsten-nickel-cerium loaded adsorbent A is prepared.
Adsorbent B
Taking Al2O360g of distilled water and 8g of concentrated nitric acid are added and mixed uniformly, 100g of Y-shaped molecular sieve and 3g of sesbania powder are added into the mixture, extruded into strips and formed, dried for 4 hours at 110 ℃, calcined for 5 hours at 550 ℃, and the carrier of the catalyst is prepared. 20g of ammonium molybdate, 5g of cobalt acetate and 1g of copper nitrate are dissolved in distilled water to prepare 200g of solution. The support was immersed in the solution and shaken for about 6 hours, after which the support was filtered off, dried at 110 ℃ for 6 hours and then calcined at 550 ℃ for 5 hours. The adsorbent B loaded with cobalt, molybdenum and copper is prepared.
And (3) sulfurization and reduction: an adsorbent A and an adsorbent B were packed in a fixed bed reactor, and the packing volume ratio of the adsorbent A to the adsorbent B was 5. Heating to 170 ℃ at the speed of 30 ℃/H, and starting to introduce H2S/H2(the volume concentration of hydrogen sulfide is 10 percent), the pressure is ensured to be 1MPa, and the air space velocity is 50h-1Then heating to 220 ℃ at the speed of 3 ℃/h, keeping the temperature for 15h, heating to 290 ℃ at the speed of 4 ℃/h, keeping the temperature for 8h, heating to 360 ℃ at the speed of 6 ℃/h, and keeping the temperature for 8 h. Cooling to 350 ℃, introducing hydrogen and leading in the hydrogen at a volume space velocity of 2000h-1The pressure is 3MPa, and the reaction time is 8 h. The adsorbent after sulfidation is ready for use.
After dewatering the liquefied gas raw material, introducing the liquefied gas raw material into a fixed bed reactor for adsorption and absorption, wherein the adsorption temperature is 160 ℃, the adsorption pressure is 3MPa, and the space velocity of a liquid phase is 2h-1. After the adsorbed gas is detected to exceed the standard, the raw material gas is immediately switched into another fixed bed reactor filled with fresh adsorbent for gas generationPurifying the body; the original fixed bed reactor filled with the adsorption saturated adsorbent is used for 2000h-1Is introduced into H2Purging, wherein temperature and pressure conditions are not changed, purging is carried out for 20h, and the adsorption process can be carried out again after the regeneration of the adsorbent is finished. The adsorbent can be reused for more than 1000 times while keeping the adsorption capacity unchanged. The adsorption-regeneration results are shown in table 1.
Example 3:
preparation of the adsorbent
Adsorbent A
Taking Al2O330g, adding 50g of distilled water and 8g of concentrated nitric acid, uniformly mixing, adding 100g of A-type molecular sieve and 3g of sesbania powder into the mixture, extruding into strips, forming, drying at 110 ℃ for 4 hours, and calcining at 550 ℃ for 5 hours to prepare the carrier of the catalyst. 20g of ammonium metatungstate, 6g of nickel nitrate and 5g of cerium nitrate are dissolved by distilled water to prepare 200g of solution. The support was immersed in the solution and shaken for about 6 hours, after which the support was filtered off, dried at 110 ℃ for 6 hours and then calcined at 550 ℃ for 5 hours. The tungsten-nickel-cerium loaded adsorbent A is prepared.
Adsorbent B
Taking Al2O360g of distilled water and 8g of concentrated nitric acid are added and mixed uniformly, 100g of β type molecular sieve and 3g of sesbania powder are added into the mixture, extruded to be shaped, dried for 4 hours at 110 ℃, calcined for 5 hours at 550 ℃ to prepare a carrier of the catalyst, 25g of ammonium molybdate, 8g of cobalt acetate and 2g of copper nitrate are dissolved by distilled water to prepare 200g of solution, the carrier is soaked in the solution and vibrated, after about 6 hours, the carrier is filtered out, dried for 6 hours at 110 ℃, and then calcined for 5 hours at 550 ℃, and the cobalt-copper loaded adsorbent B is prepared.
And (3) sulfurization and reduction: an adsorbent A and an adsorbent B were packed in a fixed bed reactor, and the packing volume ratio of the adsorbent A to the adsorbent B was 0.4. Heating to 170 ℃ at the speed of 30 ℃/H, and starting to introduce H2S/H2(the volume concentration of hydrogen sulfide is 10 percent), the pressure is ensured to be 1MPa, and the air space velocity is 50h-1Heating to 220 deg.C at a rate of 3 deg.C/h, maintaining for 15h, and heating at a rate of 4 deg.C/hThe temperature is increased to 290 ℃, the temperature is kept for 8h, the temperature is increased to 360 ℃ at the temperature increasing speed of 6 ℃/h, and the temperature is kept for 8 h. Keeping the temperature at 360 ℃, introducing hydrogen and leading in the reactor at a volume space velocity of 3000h-1The pressure is 4MPa, and the reaction time is 6 h. The adsorbent after sulfidation is ready for use.
After dewatering the liquefied gas raw material, introducing the liquefied gas raw material into a fixed bed reactor for adsorption and absorption, wherein the adsorption temperature is 170 ℃, the adsorption pressure is 5MPa, and the space velocity of a liquid phase is 1.5h-1. After the adsorbed gas is detected to be overproof in sulfide, immediately switching the feed gas into another fixed bed reactor filled with a fresh adsorbent for gas purification; the original fixed bed reactor filled with the adsorption saturated adsorbent is used for 2000h-1Is introduced into H2Purging, wherein temperature and pressure conditions are not changed, purging is carried out for 20h, and the adsorption process can be carried out again after the regeneration of the adsorbent is finished. The adsorbent can be reused for more than 1000 times while keeping the adsorption capacity unchanged. The adsorption-regeneration results are shown in table 1.
Example 4:
preparation of the adsorbent
Adsorbent A
Taking Al2O320g, adding 50g of distilled water and 8g of concentrated nitric acid, uniformly mixing, adding 100g of ZSM-5 type molecular sieve and 3g of sesbania powder into the mixture, extruding into strips, forming, drying at 110 ℃ for 4 hours, and calcining at 550 ℃ for 5 hours to prepare the carrier of the catalyst. 16g of ammonium metatungstate, 3g of nickel nitrate and 3g of cerium nitrate are dissolved by distilled water to prepare 200g of solution. The support was immersed in the solution and shaken for about 6 hours, after which the support was filtered off, dried at 110 ℃ for 6 hours and then calcined at 550 ℃ for 5 hours. The tungsten-nickel-cerium loaded adsorbent A is prepared.
Adsorbent B
Taking Al2O315g, adding 40g of distilled water and 8g of concentrated nitric acid, uniformly mixing, adding 100g of M-type molecular sieve and 3g of sesbania powder into the mixture, extruding into strips, forming, drying at 110 ℃ for 4 hours, and calcining at 550 ℃ for 5 hours to prepare the carrier of the catalyst. 15g of ammonium molybdate, 3g of cobalt acetate and 3g of copper nitrate are dissolved in distilled water to prepare 200g of solution. Impregnating the carrier in the solutionAfter shaking the solution for about 6 hours, the support was filtered off, dried at 110 ℃ for 6 hours and calcined at 550 ℃ for 5 hours. The adsorbent B loaded with cobalt, molybdenum and copper is prepared.
And (3) sulfurization and reduction: an adsorbent A and an adsorbent B were packed in a fixed bed reactor, and the packing volume ratio of the adsorbent A to the adsorbent B was 1.5. Heating to 170 ℃ at the speed of 30 ℃/H, and starting to introduce H2S/H2(the volume concentration of hydrogen sulfide is 10 percent), the pressure is ensured to be 1MPa, and the air space velocity is 50h-1Then heating to 220 ℃ at the speed of 3 ℃/h, keeping the temperature for 15h, heating to 290 ℃ at the speed of 4 ℃/h, keeping the temperature for 8h, heating to 360 ℃ at the speed of 6 ℃/h, and keeping the temperature for 8 h. Raising the temperature to 400 ℃, introducing hydrogen and ensuring the volume space velocity to be 4000h-1The pressure is 1MPa, and the reaction time is 15 h. The adsorbent after sulfidation is ready for use.
After dewatering the liquefied gas raw material, introducing the liquefied gas raw material into a fixed bed reactor for adsorption and absorption, wherein the adsorption temperature is 180 ℃, the adsorption pressure is 4MPa, and the space velocity of a liquid phase is 2.5h-1. After the adsorbed gas is detected to be overproof in sulfide, immediately switching the feed gas into another fixed bed reactor filled with a fresh adsorbent for gas purification; the original fixed bed reactor filled with the adsorption saturated adsorbent is used for 2000h-1Is introduced into H2Purging, wherein temperature and pressure conditions are not changed, purging is carried out for 18h, and the adsorption process can be carried out again after the regeneration of the adsorbent is finished. The adsorbent can be reused for more than 1000 times while keeping the adsorption capacity unchanged. The adsorption-regeneration results are shown in table 1.
Example 5:
preparation of the adsorbent
Adsorbent A
Taking Al2O330g, adding 60g of distilled water and 8g of concentrated nitric acid, uniformly mixing, adding 100g of A-type molecular sieve and 3g of sesbania powder into the mixture, extruding into strips, forming, drying at 110 ℃ for 4 hours, and calcining at 550 ℃ for 5 hours to prepare the carrier of the catalyst. 22g of ammonium metatungstate, 10g of nickel nitrate and 2g of lanthanum nitrate are dissolved in distilled water to prepare 200g of solution. The carrier is immersed in the solution and shaken to be largeAfter about 6 hours, the support is filtered off, dried at 110 ℃ for 6 hours and then calcined at 550 ℃ for 5 hours. The tungsten-nickel-lanthanum loaded adsorbent A is prepared.
Adsorbent B
Taking Al2O3Adding 50g of distilled water and 8g of concentrated nitric acid into 25g of the mixed solution, uniformly mixing, adding 100g of M-type molecular sieve and 3g of sesbania powder into the mixture, extruding the mixture into strips, forming the strips, drying the strips at 110 ℃ for 4 hours, and calcining the strips at 550 ℃ for 5 hours to prepare the carrier of the catalyst. 23g of ammonium molybdate, 4g of cobalt acetate and 2g of copper nitrate were dissolved in distilled water to prepare 200g of a solution. The support was immersed in the solution and shaken for about 6 hours, after which the support was filtered off, dried at 110 ℃ for 6 hours and then calcined at 550 ℃ for 5 hours. The adsorbent B loaded with cobalt, molybdenum and copper is prepared.
And (3) sulfurization and reduction: an adsorbent A and an adsorbent B were packed in a fixed bed reactor, and the packing volume ratio of the adsorbent A to the adsorbent B was 4. Heating to 170 ℃ at the speed of 30 ℃/H, and starting to introduce H2S/H2(the volume concentration of hydrogen sulfide is 5 percent), the pressure is ensured to be 2MPa, and the air space velocity is 50h-1Then heating to 220 ℃ at the speed of 3 ℃/h, keeping the temperature for 15h, heating to 290 ℃ at the speed of 4 ℃/h, keeping the temperature for 8h, heating to 360 ℃ at the speed of 6 ℃/h, and keeping the temperature for 8 h. Cooling to 290 ℃, introducing hydrogen and having a volume space velocity of 3000h-1The pressure is 2MPa, and the reaction time is 12 h. The adsorbent after sulfidation is ready for use.
After dewatering the liquefied gas raw material, introducing the liquefied gas raw material into a fixed bed reactor for adsorption and absorption, wherein the adsorption temperature is 190 ℃, the adsorption pressure is 2MPa, and the space velocity of a liquid phase is 3h-1. After the adsorbed gas is detected to be overproof in sulfide, immediately switching the feed gas into another fixed bed reactor filled with a fresh adsorbent for gas purification; in the fixed bed reactor filled with the adsorption saturated adsorbent, 3000 hours are required-1Is introduced into H2Purging, wherein the temperature and pressure conditions are not changed, purging is carried out for 14h, and the adsorption process can be carried out again after the regeneration of the adsorbent is finished. The adsorbent can be reused for more than 1000 times while keeping the adsorption capacity unchanged. The adsorption-regeneration results are shown in table 1.
Comparative example 1
The same as in example 1, except that only the adsorbent A was charged in the fixed bed reactor. The adsorption-regeneration results are shown in table 1.
Comparative example 2
The same as in example 2, except that only the adsorbent B was packed in the fixed bed reactors. The adsorption-regeneration results are shown in table 1.
Table 1 adsorption-regeneration results are shown in table 1.
Figure 722637DEST_PATH_IMAGE002

Claims (8)

1. The utility model provides a liquefied petroleum gas adsorbs desulfurization process, adopts fixed bed reactor, fixed bed reactor sets up two at least, the process includes as follows: firstly, liquefied petroleum gas is sent into a fixed bed reactor filled with an adsorbent to carry out adsorption desulfurization reaction, after the adsorbent reaches an adsorption saturation state, the liquefied petroleum gas is switched into another fixed bed reactor filled with the adsorbent to continue the adsorption desulfurization reaction, and hydrogen is introduced into the fixed bed reactor reaching the adsorption saturation state to regenerate, wherein the adsorption desulfurization reaction conditions are as follows: the adsorption temperature is 150-200 ℃, the adsorption pressure is 2-4 MPa, and the liquid phase space velocity is 0.5-3 h-1(ii) a The regeneration conditions are as follows: the regeneration temperature is 150-200 ℃, the regeneration pressure is 2-4 MPa, and the space velocity of hydrogen is 100-3000 h-1；
Wherein, the adsorbent is prepared by the following method:
(1) mixing the molecular sieve with an adhesive, a peptizing agent and an extrusion aid, and kneading and molding to obtain a carrier;
(2) loading a metal active component or loading the metal active component and a metal auxiliary agent on the carrier obtained in the step (1) by adopting an isometric impregnation method, and impregnating, drying and roasting to obtain an adsorbent;
(3) sulfurizing the adsorbent obtained in the step (2) to convert the oxidation state metal loaded on the adsorbent into a sulfurization state;
(4) carrying out reduction reaction on the vulcanized adsorbent obtained in the step (3) to obtain a final adsorbent; the reduction reaction conditions are as follows: the reaction temperature is 260-400 ℃, the pressure is 1-4 MPa, and the volume space velocity of hydrogen is 500-4000 h-1The reaction time is 4-20 h;
adsorbents are filled in the fixed bed reactors and comprise an adsorbent A and an adsorbent B, and the volume ratio of the adsorbent A to the adsorbent B is 0.1-10; the molecular sieve of the adsorbent A is one or more of an A-type molecular sieve, an X-type molecular sieve and a ZSM series molecular sieve; the molecular sieve of the adsorbent B is one or more of a Y-type molecular sieve, a beta-type molecular sieve and an M-series molecular sieve; the metal active components loaded in the adsorbent A are tungsten and nickel, wherein the mass fraction of the tungsten is 5-20%, and the mass fraction of the nickel is 3-10%; the metal active components loaded in the adsorbent B are cobalt and molybdenum, wherein the mass fraction of the cobalt is 3-10%, and the mass fraction of the molybdenum is 5-20%.
2. The process of claim 1, wherein: the specific surface area of the adsorbent is 120-350 m2A pore volume of 0.10-0.30 cm3(ii) a bulk density of 0.70 to 0.95g/cm3。
3. The process of claim 1, wherein: the ZSM series molecular sieve is one or more of ZSM-5, ZSM-8, ZSM-11 and ZSM-35 molecular sieves.
4. The process of claim 1, wherein: the adsorbent contains a metal auxiliary agent, the metal auxiliary agent is one or more of calcium, magnesium, strontium, lanthanum, cerium, praseodymium, iron, zirconium, zinc, copper and silver, and the oxidation state mass fraction of the metal auxiliary agent is 2-7%.
5. The process of claim 1, wherein: the volume ratio of the adsorbent A to the adsorbent B is 0.5-5.
6. The process of claim 1, wherein: the bulk density of the adsorbent A is 0.8-0.95 g/cm3The bulk density of the adsorbent B is 0.7-0.85 g/cm3The bulk density of the adsorbent A is 0.05-0.2 g/cm higher than that of the adsorbent B3。
7. The process of claim 1, wherein: the adhesive is activated alumina or a precursor thereof; the peptizing agent is one or more of inorganic acid, organic acid and strong acid anion salt, the strong acid anion salt is aluminum nitrate, the inorganic acid is one or more of nitric acid, hydrochloric acid and sulfuric acid, and the organic acid is one or more of formic acid, acetic acid, oxalic acid and citric acid; the extrusion aid is one or more of carbon black, sesbania powder, graphite powder and citric acid.
8. The process of claim 7, wherein: the adsorbent is a molecular sieve loaded with metal active components, wherein the content of the molecular sieve in the adsorbent is 60-90% by weight, the content of active alumina is 9-39% by weight, and the balance is the metal active components.
CN201610991600.8A 2016-11-11 2016-11-11 Adsorption desulfurization process for liquefied petroleum gas Active CN108070416B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201610991600.8A CN108070416B (en) 2016-11-11 2016-11-11 Adsorption desulfurization process for liquefied petroleum gas

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201610991600.8A CN108070416B (en) 2016-11-11 2016-11-11 Adsorption desulfurization process for liquefied petroleum gas

Publications (2)

Publication Number Publication Date
CN108070416A CN108070416A (en) 2018-05-25
CN108070416B true CN108070416B (en) 2020-08-11

Family

ID=62153566

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201610991600.8A Active CN108070416B (en) 2016-11-11 2016-11-11 Adsorption desulfurization process for liquefied petroleum gas

Country Status (1)

Country Link
CN (1) CN108070416B (en)

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP3941571B2 (en) * 2002-04-19 2007-07-04 松下電工株式会社 Method for desulfurization of liquefied petroleum gas
CN1782032A (en) * 2004-12-01 2006-06-07 中国石油天然气股份有限公司 Process for preparing diesel oil hydrog-refining catalyst using TiO2-SiO2 compound oxide as carrier
US7846869B2 (en) * 2008-04-23 2010-12-07 China Petroleum & Chemical Corporation Process for pre-treating a desulfurization sorbent
CN103721668B (en) * 2012-10-10 2016-07-13 中国科学院大连化学物理研究所 A kind of Gasoline ultra-deep desulfurization adsorbent and application thereof
CN104557388A (en) * 2013-10-23 2015-04-29 中国石油化工股份有限公司 Deep desulfurization method of refinery C4
CN104028208B (en) * 2014-05-29 2016-04-27 上海应用技术学院 A kind of gasoline high selectivity desulfuration adsorbent and preparation method and application
CN104028217B (en) * 2014-05-29 2016-08-17 上海应用技术学院 A kind of gasoline high-selectivity adsorption desulfurizing agent and preparation method and application
CN104262116A (en) * 2014-06-23 2015-01-07 贺立明 MTBE deep desulfurization device and method thereof

Also Published As

Publication number Publication date
CN108070416A (en) 2018-05-25

Similar Documents

Publication Publication Date Title
KR100743323B1 (en) Desulfurization process and novel bimetallic sorbent systems for same
CN104557388A (en) Deep desulfurization method of refinery C4
RU2230608C2 (en) Sorbent composition, method for preparation thereof and applying it in desulfurization process
EP1609842B1 (en) Method for purifying a liquid medium
KR20020080331A (en) Desulfurization and novel sorbents for same
CN101314727B (en) Desulfurization method for gasoline
CN103031143B (en) Method for simultaneously removing sulfides in gasoline and liquefied gas through single reactor
CN1261533C (en) Process for adsorption desulfurization of gasoline
KR20020047307A (en) Desulfurization and novel sorbents for same
RU2517639C2 (en) Adsorbent, method for production thereof and method of removing sulphur from cracked petrol or diesel fuel
CN102294222A (en) Hydrocarbon oil desulfurization adsorbent and preparation method and application thereof
CN103240117B (en) Gasoline desulfurization catalyst and preparation method thereof and gasoline desulfurization method
CN101619231A (en) Fuel oil adsorption desulfurization adsorbent and method for preparing same
CN103031150B (en) Double-reactor removes the method for gasoline and liquefied gas medium sulphide content simultaneously
US7427581B2 (en) Desulfurization process and novel bimetallic sorbent systems for same
CN104560123B (en) A kind of method adsorbing desulfurization
US4442221A (en) Process for regenerating a spent copper composite sulfur sorbent
CN108070415B (en) Adsorption desulfurization method for liquefied petroleum gas
CN104673378B (en) A kind of production method of sulfur-free gasoline
CN103031149B (en) A kind of double-reactor removes the method for gasoline and liquefied gas medium sulphide content simultaneously
CN108070416B (en) Adsorption desulfurization process for liquefied petroleum gas
US4409124A (en) Process for regenerating sulfur sorbent by oxidation and leaching
CN104673376A (en) Gasoline desulfurization method
CN104673379A (en) Deep gasoline desulfurization method
CN1478863A (en) Desulfur adsorber used for refined light oil product and its preparation method

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