CN116425705A - Application of solvent for co-production of maleic anhydride and succinic anhydride - Google Patents
Application of solvent for co-production of maleic anhydride and succinic anhydride Download PDFInfo
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- CN116425705A CN116425705A CN202310379570.5A CN202310379570A CN116425705A CN 116425705 A CN116425705 A CN 116425705A CN 202310379570 A CN202310379570 A CN 202310379570A CN 116425705 A CN116425705 A CN 116425705A
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- C07D307/02—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings
- C07D307/34—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members
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Abstract
The invention provides an application of a solvent for co-producing maleic anhydride and succinic anhydride, wherein the solvent is saturated ether, ester, ketone, phosphite or phosphate. The solvent is used as a common solvent for the joint production of maleic anhydride and succinic anhydride, so that the absorption liquid in the maleic anhydride production process is used as a raw material for producing succinic anhydride through hydrogenation, the investment of a device for producing succinic anhydride, the material consumption and the three-waste emission are reduced, and the production cost is reduced.
Description
The application is a divisional application, and the application date of the original application is: 2021, 03, 09, application number: CN202110255926.5, invention creation name: a solvent capable of simultaneously satisfying maleic anhydride and succinic anhydride production and application thereof.
Technical Field
The invention relates to a solvent capable of simultaneously meeting the production of maleic anhydride and succinic anhydride and an application method of the solvent, in particular to a reaction solvent for preparing succinic anhydride by hydrogenation of a gas absorption solvent for producing maleic anhydride by a butane or benzene oxidation method and a maleic anhydride solvent method and a separation, purification and recovery method of the reaction solvent.
Background
At present, maleic anhydride is the third largest organic anhydride chemical raw material next to phthalic anhydride and acetic anhydride, has wide application field, is used for producing unsaturated polyester resin, lubricating oil, fumaric acid, succinic anhydride and other chemical products, and is mainly used for synthetic resin, pesticides, foods, other fine chemicals and the like. The statistics shows that the maleic anhydride yield and the maleic anhydride yield in the China in 2020 are about 180 ten thousand tons and 96 ten thousand tons respectively, and the excess yield in the industry is serious. Therefore, how to improve the current maleic anhydride production process to reduce the production cost and develop new products downstream of the maleic anhydride has important significance for the development of the maleic anhydride industry and even the whole chemical industry.
The maleic anhydride prepared by oxidizing n-butane has been developed rapidly by virtue of the characteristics of low raw material price, high yield, good product quality and the like, and both the catalyst and the production process have been developed to a relatively mature stage at present, but the process still has some defects, in particular a post-treatment system of oxidation reaction product gas. The existing post-treatment system mainly comprises two processes: a water absorption process and a solvent absorption process. The water absorption process is from the early process of preparing maleic anhydride by benzene oxidation, but because the water yield of preparing maleic anhydride by n-butane oxidation is doubled as compared with that of the benzene oxidation method, and the n-butane oxidation method also generates byproducts such as acetic acid, acrylic acid and the like, the byproducts bring adverse factors such as equipment corrosion, blockage and the like, so the gas water absorption process of preparing maleic anhydride by n-butane oxidation reaction products is gradually eliminated. The solvent absorption is a new treatment process designed according to the characteristics of maleic anhydride reaction product gas prepared by n-butane oxidation, and the maleic anhydride produced by the process has the advantages of high yield, good product quality, less equipment blockage and low corrosiveness. There are three types of solvent absorption processes which are mature at present, namely an ALMA process, a Conser process and a Huntsman process. The ALMA process is a solvent absorption technology jointly developed by ABB Lumms company and Italy Lonza company in the United states for the maleic anhydride production process by fluidized bed oxidation of n-butane, and the absorbent used is Diisobutylhexahydrophthalate (DIBE). The Conser process and the Huntsman process are product gas-solvent absorption processes developed for the maleic anhydride production process by fixed bed oxidation of n-butane, and the solvent is di-n-butyl phthalate (DBP).
At present, the industrial production of maleic anhydride basically adopts an absorption process with DIBE or DBP as a solvent. For example, CN105111171 is effective in recovering maleic anhydride by using DIBE as a solventThe problem that the traditional organic solvent is easy to decompose when meeting water is avoided, and the method is suitable for large-scale continuous maleic anhydride production by taking n-butane as a raw material. CN110156727 provides a novel two-stage solvent absorption maleic anhydride production process, wherein the solvent is DIBE or DBP, which further reduces absorption and cooling load of the absorption tower system, and forwards moves the gateway of the impurity removal system, thereby avoiding the aggregation of impurities in the subsequent system, and being suitable for large-scale continuous maleic anhydride production. CN103044368 discloses a method for producing maleic anhydride by benzene method and absorbing solvent, which adopts a non-aqueous maleic anhydride recovery process and uses DBP as absorption solvent, thus saving a great amount of energy consumption of evaporation and dehydration, avoiding the generation of impurities such as fumaric acid, improving the recovery rate of maleic anhydride, reducing equipment investment and saving cost. In addition, there are also patent reports of using other solvents as maleic anhydride absorption solvents, including phthalates and their hydrides, and C 3 ～C 8 C of dibasic fatty acids 3 ～C 5 Fatty alcohol diesters. For example, US4118403, WO29323 and CN1503773 disclose organic solvents for the absorption of maleic anhydride which have a boiling point higher than the boiling points of the low boilers maleic, fumaric and phthalic anhydride, so that these components can be separated off as low boilers; while the boiling point of the solvent is low enough to separate from the tarry polymer without decomposition under vacuum in commercial use, including dialkyl phthalates and dialkyl dihydro, tetrahydro or hexahydrophthalates having 2 to 8 carbon atoms in the alkyl chain, and dimethyl benzophenone, dichlorobenzyl oxide or monoalkyl substituted succinic acids having 12 to 16 carbon atoms. CN103476812 provides an improved solvent for recovering maleic anhydride from a gas stream, the solvent having a normal boiling point of 250-350 ℃, a fumaric acid solubility of at least 0.06wt% at 60 ℃, a maleic anhydride solubility of at least 10wt% at 60 ℃, a water solubility of not more than 100mg/L, a density difference from water of at least 0.020g/mL and a molecular weight of not more than pentanol, may be acyclic, non-aromatic, linear and/or branched and has the general structure R 1 COOR 2 COOR 3 Wherein R is 1 And R is 3 Each being a straight or branched chain C 3 ～C 5 A group R 2 Is straight-chain or branched C 3 ～C 8 A group.
Succinic anhydride is an important fine chemical raw material and is widely applied to the fields of foods, surfactants, coatings, medicines, agriculture, plastics and the like. Poly (butylene succinate)/ethylene glycol ester (PBS/PES) can be prepared by polycondensation of succinic anhydride or hydrolysis product succinic acid thereof with 1, 4-butanediol/ethylene glycol, poly (butylene succinate) -adipic acid-butanediol/ethylene glycol ester (PBSA/PESA) or poly (butylene succinate) -terephthalic acid-butanediol/ethylene glycol ester (PBST/PEST) can be prepared by ternary polycondensation of adipic acid or terephthalic acid, and the poly (butylene succinate)/ethylene glycol ester is biodegradable or semi-degradable plastic with excellent performance. In recent years, with the increasing severity of environmental pollution problems of traditional plastics, the PBS/PES biodegradable materials have very broad market prospects, so that the market demand of the upstream product succinic anhydride is greatly stimulated and driven.
The maleic anhydride direct hydrogenation method is the most efficient process for producing succinic anhydride at present, has the advantages of simple process flow, convenient operation, high equipment utilization rate, low running cost and high product purity, and is especially the continuous liquid-phase hydrogenation reaction process of the maleic anhydride solvent method, and the method is the most promising method for preparing the succinic anhydride at present due to the mild operation condition, high succinic anhydride selectivity, long service life of the catalyst and easy mass production. Yuan et Al (J.chem. Sci.,2014,126 (1): 141-145) use the solvents 1, 4-dioxane and Pd/Al 2 O 3 The catalyst is subjected to maleic anhydride hydrogenation to prepare succinic anhydride, and the succinic anhydride is continuously operated on a fixed bed micro-reaction device for 1600 hours under the hydrogen pressure of 1.0MPa at the temperature of 80 ℃, wherein the maleic anhydride conversion rate and the succinic anhydride selectivity are both more than 99 percent. CN105801536 uses dimethyl succinate, ethyl acetate, butyl acetate, gamma-butyrolactone and the like as solvents, adopts a two-stage low-temperature low-pressure maleic anhydride liquid phase selective hydrogenation process to prepare succinic anhydride, uses two hydrogenation reactors in series at 40-120 ℃ and 0.2-2.0 MPa, and ensures that the maleic anhydride conversion rate is not less than 99.9% and the succinic anhydride selectivity is not less than 99.0%. CN102311332 uses gamma-butyrolactone as solvent, adopts fixed bed reactor to continuously make maleic anhydride hydrogenation reaction, and makes maleic anhydride conversion rate be 100% and succinic anhydride selectivity be 99.2% under the condition of 70 deg.C and 1.5MPa hydrogen pressure on Pd-Fe/C catalyst. CN101735182 is tetrahydrofuran, dioxane, gamma-butyl lactoneThe maleic anhydride is continuously produced by hydrogenating maleic anhydride by using solvents such as ester, isoamyl acetate, dimethyl succinate and the like and a supported nickel catalyst, and the maleic anhydride conversion rate is more than 99% and the succinic anhydride selectivity is more than 99.5% under the conditions that the hydrogen pressure is 0.9-10.0 MPa and the space velocity of maleic anhydride solution with the concentration of 0.04-0.08 g/ml is 0.13-0.16 h < -1 >. The method adopts the continuous hydrogenation reaction process of maleic anhydride by a solvent method to prepare succinic anhydride, and obtains good reaction effect, but the boiling point of the adopted solvent is low (lower than 261 ℃ below zero) and is far different from the boiling point of low-volatility organic solvents such as DIBE and DBP (about 340 ℃) adopted in the industrial production of maleic anhydride, and the solvent cannot be used together with the absorption solvent in the production of maleic anhydride.
In summary, at present, the catalytic oxidation method using benzene or butane as raw material and the high boiling point low volatility organic solvent such as DIBE or DBP absorption process are basically adopted in industry to produce single product maleic anhydride, and no report of switching production or co-production of other products and production of downstream products by using crude maleic anhydride which is not separated and refined as raw material has been made, and the production of the downstream products of the maleic anhydride takes commodity or finished maleic anhydride as raw material; the main stream preparation technology of succinic anhydride basically adopts maleic anhydride products with the content of more than or equal to 99 weight percent as raw materials, and the maleic anhydride is synthesized by the maleic anhydride hydrogenation by a solvent method (adopting solvents with low boiling points such as tetrahydrofuran, dioxane, gamma-butyrolactone, ethyl acetate, butyl acetate, isoamyl acetate, dimethyl succinate and the like), the report that solvents with high boiling points (more than 261 ℃) such as DIBE or DBP and the like are adopted as hydrogenation reaction solvents, and the report that maleic anhydride gas absorption liquid generated by benzene or butane oxidation reaction is directly used as raw materials for hydrogenation production of the succinic anhydride is not shared because the variety and the property of the adopted hydrogenation reaction solvents are different from those of the absorption solvents produced by the maleic anhydride, so that the succinic anhydride can only be produced by adopting the maleic anhydride as the raw materials, thereby improving the raw material cost; because the solvents cannot be shared, the maleic anhydride and the succinic anhydride can be produced by only two sets of independent devices, and the switching production and the co-production of the maleic anhydride and the succinic anhydride cannot be realized from the initial raw materials benzene or butane, so that the solvent resolving, purifying and recycling devices and the product separating and refining devices cannot be shared, thereby reducing the device investment, the energy consumption, the material consumption and the wastewater discharge.
Disclosure of Invention
Aiming at the defects existing in the prior art, the invention provides a solvent capable of simultaneously meeting the production requirements of maleic anhydride and succinic anhydride, and the combined production of maleic anhydride and/or succinic acid is realized by the sharing of the solvent, so as to solve the problems that the cost of raw materials for producing succinic anhydride is high, the investment of equipment is large, the energy consumption and the material consumption are high and the like because two sets of independent solvent separation recovery and product separation refining devices are needed to be used for the use of solvents with different varieties and properties, and the raw materials for producing succinic anhydride by a hydrogenation method only adopt maleic anhydride finished products.
The selection principle of the solvent of the invention: in the process of oxidizing raw material benzene or butane to generate maleic anhydride gas and condensing and absorbing the maleic anhydride gas by a solvent, target product maleic anhydride and organic byproducts generated by the reaction are absorbed into an absorption liquid by the solvent, so that a series of acidic impurities such as acetic acid, propionic acid, acrylic acid, succinic acid, maleic acid, fumaric acid, phthalic anhydride and the like exist in the absorption liquid, and in the subsequent treatment process, in order to obtain high-quality maleic anhydride and/or succinic anhydride products, the impurities need to be removed one by one. Therefore, the selection of the solvent and the subsequent treatment method are very important, and the problems of purification and recovery of the product and the solvent are related, so that the purity and the yield of the product and the solvent are affected.
In order to solve the above technical problems and achieve the object of obtaining a product of high purity and high yield, facilitating the purification of the solvent and recycling at high recovery, the solvent to be selected must satisfy the following conditions:
(1) Has excellent chemical stability. The solvent cannot be subjected to chemical changes such as condensation, decomposition and the like in the solvent absorption and subsequent treatment processes, and chemical reactions can be carried out between the solvent and other substances in the system;
(2) Has a lower freezing point. The freezing point is not higher than the lower line operation temperature of 60 ℃ of the condensation absorption of the oxidizing gas, preferably a solvent (40 ℃ selected) which is lower than the freezing point of 52.8 ℃ of maleic anhydride of the target absorbing substance by less than 10 ℃, and more preferably a solvent with the freezing point lower than 25 ℃ so as to ensure that the absorbing liquid is not solidified and has good fluidity in the subsequent operation process;
(3) Has good solubility. In order to ensure good solvent absorption effect and prevent materials from separating out and blocking equipment and pipelines at a condensation absorption temperature, the solvent is required to have good solubility for the target product maleic anhydride and succinic anhydride, and certain solubility for impurity fumaric acid (boiling point 355.5 ℃ and melting point near 300 ℃) which has the highest boiling point and is difficult to remove by distillation and is easier to solidify and separate out, the solubility for maleic anhydride and succinic anhydride at 60 ℃ is selected to be not lower than 10wt%, the solubility for fumaric acid is not lower than 0.05wt%, preferably the solubility for maleic anhydride and succinic anhydride is not lower than 12wt%, the solubility for fumaric acid is not lower than 0.10wt%, more preferably the solubility for maleic anhydride and succinic anhydride is not lower than 15wt%, and the solubility for fumaric acid is not lower than 0.20wt%;
(4) Has a high and suitable boiling point. The boiling point of the solvent is higher than that of the target product maleic anhydride (boiling point 202 ℃) generated by oxidizing benzene or butane and the target product succinic anhydride (boiling point 261 ℃) generated by hydrogenating the maleic anhydride, preferably the solvent (boiling point 271 ℃) which is 10 ℃ higher than that of the succinic anhydride, more preferably the solvent (boiling point 271 ℃) which is 10 ℃ higher than that of the byproduct acetic acid (117.9 ℃), propionic acid (141.1 ℃), acrylic acid (141.6 ℃), maleic acid (160 ℃) dehydrated to maleic anhydride), fumaric acid (250 ℃) dehydrated to maleic acid, succinic acid (235 ℃) dehydrated to succinic anhydride), phthalic acid (230 ℃) dehydrated to phthalic anhydride), phthalic anhydride (284 ℃) and those solvents (boiling point 300 ℃) with the highest boiling point or the highest dehydration temperature of 15 ℃ among the added polymerization inhibitor hydroquinone (285 ℃), so that the components can be separated as low-boiling point substances, thereby facilitating the resolution of the solvent and the separation from products, impurities, polymerization inhibitors and the like; at the same time the boiling point of the solvent should be low enough (not exceeding 400 ℃, preferably below 380 ℃) to allow it to be efficiently separated from the tarry polymer without decomposition under industrially applicable vacuum conditions;
(5) Has low water solubility and has a large density difference from water. In order to purify the solvent and recycle it efficiently, the impurities are not brought back into the system in a large amount and accumulated by the recycled solvent, and to facilitate the dissolution and extraction of the residual organic acid and acid tar by washing with water, and to recover the solvent in a high yield by centrifugation, it is required that the solubility of the solvent in water is as low as possible and the density difference from water is as large as possible, and the organic solvent having a solubility in water of not more than 100mg/L at 25℃and a density difference from water of not less than 0.020g/mL is selected, preferably the solvent having a solubility in water of not more than 75mg/L and a density difference from water of not less than 0.025g/mL, more preferably the solvent having a solubility in water of not more than 50mg/L and a density difference from water of not less than 0.030 g/mL.
In order to solve the technical problems, the solvent and the application technical scheme adopted by the invention are as follows:
a solvent which satisfies both maleic anhydride and succinic anhydride production and has stable chemical properties, a freezing point of less than 60 ℃, a boiling point of greater than 261 ℃, a solubility of not less than 0.05 wt.% to fumaric acid at 60 ℃ and not less than 10 wt.% to both maleic anhydride and succinic anhydride, a solubility in water of not more than 100mg/L at 25 ℃ and a density difference from water of not less than 0.020g/mL, comprises C 7 ～C 12 Saturated aliphatic or cycloalkyl or aromatic ethers, C 2 ～C 10 Saturated C of saturated dihydric alcohol 2 ～C 10 Fatty acid diester or naphthenic acid diester or aromatic acid diester, C of glycerin 3 ～C 6 Triesters of saturated fatty acids, C 2 ～C 10 C of dibasic saturated fatty acids 1 ～C 10 Alkyl or cycloalkyl or aryl diesters, C 8 C of dibasic aromatic acid or naphthenic acid 2 ～C 8 Alkyl diester, C 12 ～C 18 Saturated aromatic ketone, C 3 ～C 8 Alkyl phosphotriester or triphenyl phosphite, or a combination of any two or more thereof; preferably an organic solvent having stable chemical properties, a freezing point of less than 40 ℃, a boiling point of greater than 271 ℃, a solubility of not less than 0.10 wt.% for fumaric acid at 60 ℃ and not less than 12 wt.% for both maleic anhydride and succinic anhydride, a solubility in water of not more than 75mg/L at 25 ℃ and a density difference from water of not less than 0.025g/mL, including didecyl ether, dibenzyl ether, or 2, 4-trimethyl-1, 3-pentanediol diisobutyrate, glyceryl tripropionate, glyceryl triisobutyrate, glyceryl tributyrate, dibutyl or dipentyl succinate, adipic acid C 4 ～C 6 Alkyl diesters, dimethyl or diethyl suberates, azelaic acid C 1 ～C 4 Alkyl diester, sebacic acid C 1 ～C 4 Alkyl diester, dibutyl terephthalate, diethyl isophthalate, and phthalic acid C 1 ～C 8 Alkyl diester, hexahydrophthalic acid C 2 ～C 8 Alkyl diester, phenyl hexyl ketone, phenyl heptyl ketone, triphenyl phosphite or tributyl phosphate, or a combination of any two or more thereof; more preferred are organic solvents that are chemically stable, have a freezing point below 25 ℃, a boiling point between 300 and 380 ℃, a solubility of not less than 0.20wt% for fumaric acid at 60 ℃ and not less than 15wt% for both maleic anhydride and succinic anhydride, a solubility in water of not more than 50mg/L and a density difference from water of not less than 0.030g/mL, including didecyl ether, tributyrin, dipentyl succinate, dibutyl adipate, diethyl sebacate, diisobutyl sebacate, dibutyl sebacate, diisobutyl phthalate, dibutyl phthalate, diethyl isophthalate, dipropyl hexahydrophthalate, diisobutyl hexahydrophthalate, dibutyl hexahydrophthalate or triphenyl phosphite, or a combination of any two or more thereof.
Aiming at the solvent which simultaneously meets the production of maleic anhydride and succinic anhydride, the application technical scheme is as follows:
the scheme for producing maleic anhydride by using butane or benzene as raw material is as follows: the maleic anhydride gas generated by butane or benzene oxidation reaction is sent to a solvent absorption system for gas-liquid separation, the gas is sent to an oxidation reaction system for recycling after washing by desalted water or sent to a tail gas incinerator for burning, the absorption liquid is sent to a solvent analysis system, the crude maleic anhydride containing light components and the solvent containing heavy components are separated by negative pressure flash evaporation, the crude maleic anhydride is sent to a product refining system, after the light components are removed by negative pressure of a light component removal tower, the bottom material is sent to a product tower for rectification to obtain maleic anhydride products, the solvent containing heavy components is sent to a solvent purification recovery system, after washing by desalted water and extracting acidic components, the solvent is sent to a centrifuge for separating aqueous phase and solvent phase, the solvent is sent to the solvent absorption system for recycling, and the aqueous phase is sent to a wastewater treatment system.
(ii) the scheme applied to the production of succinic anhydride by taking maleic anhydride products as raw materials is as follows: maleic anhydride is dissolved in a solvent to prepare maleic anhydride solution with a certain concentration, the maleic anhydride solution is sent to a hydrogenation reaction system to carry out complete hydrogenation on maleic anhydride, generated succinic anhydride mixture is sent to a hydrogenation reaction system to be recycled after gas-liquid separation, reaction liquid is sent to a solvent analysis system again, crude succinic anhydride containing light components and solvent containing heavy components are separated through negative pressure flash evaporation, crude succinic anhydride is sent to a product refining system, after the light components are removed by negative pressure of a light component removing tower, tower bottom materials are sent to a product tower to be rectified to obtain succinic anhydride products, and solvent containing heavy components is sent to a solvent purification recovery system, after acidic components in the succinic anhydride mixture are washed and extracted by desalted water, the solvent is sent to a centrifuge to separate water phase and solvent phase, and the solvent is sent to a solvent absorption system to be recycled, and the water phase is sent to a wastewater treatment system.
(iii) the scheme applied to the production of succinic anhydride by using butane or benzene as raw materials is as follows: the maleic anhydride gas generated by butane or benzene oxidation reaction is sent to a solvent absorption system for gas-liquid separation, the gas is sent to an oxidation reaction system for recycling after washing by desalted water or sent to a tail gas incinerator for burning, the absorption liquid is sent to a hydrogenation reaction system for generating succinic anhydride mixture through total hydrogenation, hydrogen is sent to the hydrogenation reaction system for recycling after gas-liquid separation, the reaction liquid is sent to a solvent analysis system for separating crude succinic anhydride containing light components and solvent containing heavy components through negative pressure flash evaporation, the crude succinic anhydride is sent to a product refining system, after the light components are removed by negative pressure of a light component removing tower, the tower bottom material is sent to a product tower for rectification to obtain succinic anhydride product, the solvent containing heavy components is sent to a solvent purification recovery system for washing by desalted water and extracting acid components therein, then sent to a centrifuge for separating water phase and solvent phase, and the solvent is sent to the solvent absorption system for recycling, and the water phase is sent to a wastewater treatment system.
(iv) the scheme for switching production of maleic anhydride and succinic anhydride by taking butane or benzene as raw materials is as follows: the maleic anhydride gas generated by butane or benzene oxidation reaction is sent to a solvent absorption system for gas-liquid separation, the gas is sent to an oxidation reaction system for recycling after washing by desalted water or sent to a tail gas incinerator for incineration, the absorption liquid is selectively switched in two modes, (1) sent to a solvent analysis system for separating coarse maleic anhydride containing light components and solvent containing heavy components by negative pressure flash evaporation, the coarse maleic anhydride is sent to a product refining system, after the light components are removed by negative pressure of a light component removal tower, the material at the bottom of the tower is sent to a product tower for rectification to obtain maleic anhydride products, and the solvent containing heavy components is sent to a solvent purification recovery system; or (2) feeding the mixture into a hydrogenation reaction system, generating a succinic anhydride mixture through total hydrogenation, separating gas from liquid, feeding hydrogen into the hydrogenation reaction system for recycling, feeding the reaction liquid into a solvent analysis system, separating crude succinic anhydride containing light components and a solvent containing heavy components through negative pressure flash evaporation, feeding the crude succinic anhydride into a product refining system, feeding a tower bottom material into a product tower for rectifying after the light components are removed from the tower through negative pressure, and feeding the solvent containing heavy components into a solvent purification and recovery system; the solvent containing heavy components is washed by desalted water in a solvent recovery system, the acidic components in the solvent are extracted, the solvent is sent to a centrifuge to separate a water phase and a solvent phase, the solvent is sent back to a solvent absorption system for recycling, and the water phase is sent to a wastewater treatment system.
The scheme for co-producing maleic anhydride and succinic anhydride by using butane or benzene as raw materials is as follows: the maleic anhydride gas generated by butane or benzene oxidation reaction is sent to a solvent absorption system for gas-liquid separation, the gas is sent to an oxidation reaction system for recycling after washing by desalted water or sent to a tail gas incinerator for burning, the absorption liquid is sent to a hydrogenation reaction system for obtaining succinic anhydride and maleic anhydride mixed materials through partial hydrogenation, after gas-liquid separation, hydrogen is sent to the hydrogenation reaction system for recycling, the reaction liquid is sent to a solvent analysis system again, light components, maleic anhydride and succinic anhydride materials are separated from solvent and heavy component materials through negative pressure flash evaporation, the maleic anhydride and succinic anhydride materials containing the light components are sent to a product refining system, after the light components are removed by a light component removing tower under negative pressure, the bottom materials are sent to a product tower for fractional distillation to obtain two products of maleic anhydride and succinic anhydride, the solvent containing the heavy components is sent to a solvent purification recovery system, after washing by desalted water and extracting acid components therein, then sent to a centrifugal separator for separating water phase and solvent phase, the solvent is sent to the solvent absorption tower for recycling, and the water phase is sent to a wastewater treatment system.
In the above solvent application scheme, benzene or butane is used as a starting material, and maleic anhydride can be produced separately by the scheme (i); by butt joint of the schemes (i) and (ii), maleic anhydride is taken as a raw material for producing succinic anhydride by hydrogenation, and the maleic anhydride and the succinic anhydride respectively adopt a set of independent post-treatment systems, so that two products of maleic anhydride and succinic anhydride can be produced in series; by the scheme (iii), succinic anhydride can be produced independently by taking absorption liquid (crude maleic anhydride containing solvent) as hydrogenation raw material; two products of maleic anhydride and succinic anhydride can be produced separately by operating the two processes and devices independently; by sharing one set of oxidation reaction and solvent absorption system, the absorption liquid is divided into two paths and respectively enters two independent subsequent treatment systems, so that two products of maleic anhydride and succinic anhydride can be produced in parallel; by sharing one set of oxidation reaction and solvent absorption system with (i) and (iii), the absorption liquid selectively enters a post-treatment system, or enters the same set of post-treatment system after all hydrogenation of a hydrogenation system is carried out, namely (iv), two products of maleic anhydride and succinic anhydride can be switched to be produced; by sharing one set of oxidation reaction and solvent absorption system in (i) and (iii), the absorption liquid directly enters a hydrogenation system, and after partial hydrogenation, the absorption liquid enters a post-treatment system, namely (v), so that two products of maleic anhydride and succinic anhydride can be co-produced.
In the application scheme of the solvent, benzene or butane is used as a starting material, and the prepared maleic anhydride solution or maleic anhydride absorption liquid is fed into Pd/Al filling equipment for separate production of succinic anhydride or serial production, parallel production or switching production of maleic anhydride 2 O 3 The trickle bed reactor of the catalyst is used for carrying out all liquid phase hydrogenation reaction, and the reaction conditions are as follows: the reaction temperature is 60-90 ℃, the reaction pressure is 1.0-2.5 MPa, the molar ratio of the circulating hydrogen to the fresh hydrogen to the maleic anhydride is 20-80:1 and the weight ratio of the maleic anhydride to the solvent is 1:1-10.
Application of the above solventIn the scheme, benzene or butane is used as a starting material, and maleic anhydride and succinic anhydride are co-produced by feeding maleic anhydride absorption liquid into Pd/Al filling equipment 2 O 3 The trickle bed reactor of the catalyst is used for carrying out partial liquid phase hydrogenation reaction, and the reaction conditions are as follows: the reaction temperature is 40-70 ℃, the reaction pressure is 0.5-1.0 MPa, the molar ratio of the circulating hydrogen to the fresh hydrogen to the maleic anhydride is 5-50:1 and the molar ratio of the maleic anhydride to the solvent is 0.5-1.0:1 respectively, and the weight ratio of the maleic anhydride to the solvent is 1:0.5-5.
Compared with the prior art, the solvent capable of simultaneously meeting the production of maleic anhydride and succinic anhydride and the application method thereof have the following characteristics:
1) The invention is characterized in that the provided solvent not only meets the requirement of the absorption solvent of maleic anhydride gas generated by butane or benzene oxidation, but also meets the requirement of the reaction solvent for producing succinic anhydride by liquid phase hydrogenation of maleic anhydride, thus the provided solvent has the dual functions of absorbing organic acid gas in the oxidation generated gas and dissolving maleic anhydride which is a hydrogenation reaction raw material, can be used as a solvent for independently producing maleic anhydride by taking benzene or butane as a raw material, can also be used as a solvent for independently producing maleic anhydride, and can be used as a common solvent for jointly producing (series, parallel, switching and co-producing) maleic anhydride and succinic anhydride.
2) The second characteristic of the invention is that by adopting the difunctional solvent and realizing the sharing of the gas absorption solvent generated by oxidation and the hydrogenation reaction medium solvent, and adopting the hydrogenation catalyst with excellent catalytic performance and strong tolerance to impurities, the solvent absorption liquid is directly used as the hydrogenation reaction raw material, thus the problem of high raw material cost caused by adopting the high-purity maleic anhydride as the raw material in the prior art for producing the succinic anhydride can be avoided, meanwhile, the direct production of the succinic anhydride by taking benzene or butane as the raw material can be realized without solvent analysis, purification and recovery of the maleic anhydride production and refining links of crude maleic anhydride, the investment of the device, the energy consumption and the waste water amount can be reduced, and especially, the maleic anhydride and the succinic anhydride are adopted to switch the production or co-production process, so that not only can the oxidation reaction system and the solvent absorption system be shared, but also the solvent analysis and purification recovery system and the product refining system can be greatly reduced, meanwhile, the production scheme of the succinic anhydride can be more flexibly adjusted at any time according to the market demand.
3) The invention has the third characteristic that the co-production process of maleic anhydride and succinic anhydride is adopted, because the hydrogenation saturation of the absorption liquid is carried out firstly, unsaturated acidic impurities such as acrylic acid, maleic acid, fumaric acid and the like in the absorption liquid are also hydrogenated and converted into saturated propionic acid and succinic acid while the maleic anhydride is partially converted into the succinic anhydride, the polymerization tendency of thermosensitive unsaturated compounds in the post-treatment process, which occurs when the maleic anhydride is produced independently, and the equipment and pipeline blockage problems caused by the easy solidification and precipitation of fumaric acid with extremely high solidifying point and boiling point are avoided, meanwhile, the impurity components of liquid phase materials are more single and the boiling point of residual saturated organic acid impurities is lower, on the one hand, the operation of the whole post-treatment process is more facilitated, and the product quality is higher; on the other hand, propionic acid is taken out as a light component along with the product in a solvent analysis system, succinic acid is dehydrated to generate succinic anhydride, and heavy components maleic acid and fumaric acid are converted into target products, so that the succinic anhydride has a certain yield increase; thirdly, as the impurity quantity and variety of the heavy components are reduced, the main residual impurities of phthalic anhydride, polymerization inhibitor hydroquinone and tar are reduced, the load of a solvent purification and recovery system is reduced, the water consumption for washing and extracting acidic impurity components by desalted water can be reduced, the wastewater discharge and COD total amount are greatly reduced, and the operation cost of solvent purification and recovery and the environmental protection treatment cost of wastewater can be reduced.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely, and it is apparent that the described embodiments are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
Examples 1 to 4 maleic anhydride was produced from butane as a raw material by the following procedure: maleic anhydride gas generated by butane oxidation reaction is sent to a solvent absorption system for gas-liquid separation, the gas is sent to an oxidation reaction system for recycling after being washed by desalted water or sent to a tail gas incinerator for incineration, and washing liquid is sent to a solvent recovery system for being used as a solvent washing agent; the absorption liquid is sent to a solvent analysis system, crude maleic anhydride containing light components and a solvent containing heavy components are separated through negative pressure flash evaporation, the crude maleic anhydride is sent to a product refining system, after the light components are removed from a light component removing tower under negative pressure, the material at the bottom of the tower is sent to a product tower for rectification, and a maleic anhydride product is obtained; the solvent containing heavy components is sent to a solvent purification recovery system, washed by desalted water and extracted with acidic components, then sent to a centrifuge to separate water phase and solvent phase, the solvent is sent back to a solvent absorption system for recycling, and the water phase is sent to a wastewater treatment system.
The operating conditions adopted in the implementation process are the same as those of a Conser process for industrially producing maleic anhydride. The solvents used were dibutyl sebacate, didecyl ether, triphenyl phosphite and tributyrin, respectively, from examples 1 to 4, and the properties of the corresponding solvents are shown in Table 1. After the device was operated stably, the results of maleic anhydride yield, butane unit consumption, solvent recovery rate, product purity, etc. are shown in Table 2.
The raw materials, operating conditions and implementation procedures used in comparative examples 1-2 are the same as those used in example 1, except that the common solvents used in the current industrial production of maleic anhydride, namely butyl phthalate (DBP) and diisobutyl hexahydrophthalate (DIBE), are used, and when DIBE is used as the solvent, the materials fed into the solvent purification and recovery system are washed with alkaline liquor before being washed with desalted water.
Examples 5 to 8 succinic anhydride is produced from maleic anhydride as a raw material by the following steps: maleic anhydride is dissolved in a solvent to prepare maleic anhydride solution with the concentration of 20 weight percent, the maleic anhydride solution is sent to a hydrogenation reaction system to carry out complete hydrogenation on maleic anhydride, generated succinic anhydride mixture is sent to a hydrogenation reaction system to be recycled after gas-liquid separation, reaction liquid is sent to a solvent analysis system again, crude succinic anhydride containing light components and solvent containing heavy components are separated through negative pressure flash evaporation, crude succinic anhydride is sent to a product refining system, after the light components are removed by negative pressure of a light component removing tower, tower bottom materials are sent to a product tower to be rectified to obtain succinic anhydride products, solvent containing heavy components is sent to a solvent purification recovery system, aqueous phase and solvent phase are sent to a centrifuge to be separated after desalted water is used for washing and acid components are extracted, and the solvent is sent to a solvent absorption system to be recycled, and the aqueous phase is sent to a wastewater treatment system.
The total hydrogenation reaction conditions of the maleic anhydride are as follows: the reaction temperature is 60 ℃, the reaction pressure is 2.0MPa, the molar ratio of the circulating hydrogen to the fresh hydrogen to the maleic anhydride is 50:1 and the molar ratio of the fresh hydrogen to the maleic anhydride is 1.5:1, and the weight ratio of the maleic anhydride to the solvent is 1:4.
The operation conditions of the product refining system are as follows: the pressure of the top of the light component removal tower is 20kPa, the temperature of the top of the tower is 140 ℃, and the temperature of the bottom of the tower is 208 ℃; the tower top pressure of the product tower is 5kPa, the tower top temperature is 156 ℃, and the tower bottom temperature is 205 ℃.
The operating conditions of the solvent purification and recovery system are the same as those of the embodiment 1.
The solvents used were DBP, diethyl sebacate, diethyl isophthalate and dipentyl succinate, respectively, from examples 5 to 8, the properties of the corresponding solvents being shown in Table 1. After the device runs steadily, the results of succinic anhydride yield, converted butane unit consumption, solvent recovery rate, product purity and the like are shown in Table 2.
The raw materials, hydrogenation reactions and gas-liquid separation conditions used in comparative examples 3 to 4 were the same as in example 5, except that: the adopted solvent is the general 1, 4-dioxane and gamma-butyrolactone for preparing succinic anhydride at present, in addition, the subsequent treatment of hydrogenation reaction liquid is that the solvent is sent into a solvent analysis system, after the negative pressure of a light component removal tower is used for removing the solvent, the solvent is sent into a product tower for rectification to obtain succinic anhydride product, and the recombination at the bottom of the tower is sent into a waste liquid treatment system.
Example 9 succinic anhydride was produced from butane as a starting material by the following procedure: the maleic anhydride gas generated by butane oxidation reaction is sent to a solvent absorption system for gas-liquid separation, the gas is sent to an oxidation reaction system for recycling after washing by desalted water or sent to a tail gas incinerator for burning, the absorption liquid is sent to a hydrogenation reaction system for generating succinic anhydride mixed material through total hydrogenation, hydrogen is sent to a hydrogenation reaction system for recycling after gas-liquid separation, the reaction liquid is sent to a solvent analysis system for separating crude succinic anhydride containing light components and solvent containing heavy components through negative pressure flash evaporation, the crude succinic anhydride is sent to a product refining system for removing the light components through negative pressure, after the light components are removed through a light component removing tower, the tower bottom material is sent to a product tower for rectification to obtain succinic anhydride product, the solvent containing heavy components is sent to a solvent purification recovery system for recycling after washing by desalted water and extracting the acid components, the solvent is sent to a centrifuge for separating water phase and solvent phase, and the solvent is sent to the solvent absorption system for recycling, and the water phase is sent to a wastewater treatment system.
The operating conditions of the solvent absorption system are the same as those of the embodiment 1, and the operating conditions of the maleic anhydride total hydrogenation reaction system, the product refining system and the solvent purification recovery system are the same as those of the embodiment 5.
The solvent used was diisobutyl phthalate and the properties of the corresponding solvents are shown in Table 1. After the device runs steadily, the results of succinic anhydride yield, butane unit consumption, solvent recovery rate, product purity and the like are shown in Table 2.
Example 10 maleic anhydride and succinic anhydride were produced in parallel from butane as raw material, the implementation procedure was as follows: the maleic anhydride gas generated by butane oxidation reaction is sent to a solvent absorption system for gas-liquid separation, the gas is sent to an oxidation reaction system for recycling after washing by desalted water or sent to a tail gas incinerator for incineration, the absorption liquid is divided into two paths, one path is directly sent to a solvent analysis system, the crude maleic anhydride containing light components and the solvent containing heavy components are separated by negative pressure flash evaporation, the crude maleic anhydride is sent to a product refining system, after the light components are removed by a light component removal tower under negative pressure, the material at the bottom of the tower is sent to a product tower for rectification to obtain maleic anhydride products, and the solvent containing heavy components is sent to a solvent purification recovery system; the other path is sent to a hydrogenation reaction system, after all hydrogenation is carried out to generate a succinic anhydride mixture material and gas-liquid separation, hydrogen is sent back to the hydrogenation reaction system for recycling, reaction liquid is sent to a solvent analysis system, crude succinic anhydride containing light components and solvent containing heavy components are separated through negative pressure flash evaporation, the crude succinic anhydride is sent to a product refining system, after the light components are removed by a light component removing tower under negative pressure, tower bottom materials are sent to a product tower for rectification to obtain succinic anhydride products, and solvent containing heavy components is sent to a solvent purification recovery system; the solvent containing heavy components is washed by desalted water in a solvent recovery system, the acidic components in the solvent are extracted, the solvent is sent to a centrifuge to separate a water phase and a solvent phase, the solvent is sent back to a solvent absorption system for recycling, and the water phase is sent to a wastewater treatment system.
The operating conditions of the solvent absorption system are the same as those of the embodiment 1, the operating conditions of the product refining system for producing maleic anhydride and the operating conditions of the solvent purifying and recovering system are the same as those of the embodiment 1, and the hydrogenation reaction condition for producing succinic anhydride, the operating conditions of the product refining system and the operating conditions of the solvent purifying and recovering system are the same as those of the embodiment 5.
The solvent used was diisobutyl phthalate and the properties of the corresponding solvents are shown in Table 1. After the device runs steadily, the results of succinic anhydride yield, butane unit consumption, solvent recovery rate, product purity and the like are shown in Table 2.
Example 11 maleic anhydride and succinic anhydride were produced by switching butane as a raw material, and the process was carried out as follows: the maleic anhydride gas generated by butane oxidation reaction is sent to a solvent absorption system for gas-liquid separation, the gas is sent to an oxidation reaction system for recycling after washing by desalted water or sent to a tail gas incinerator for incineration, the absorption liquid is selectively switched between two modes for operation, (1) sent to a solvent analysis system for separating coarse maleic anhydride containing light components and solvent containing heavy components by negative pressure flash evaporation, the coarse maleic anhydride is sent to a product refining system, after the light components are removed by negative pressure of a light component removal tower, the material at the bottom of the tower is sent to a product tower for rectification to obtain maleic anhydride products, and the solvent containing heavy components is sent to a solvent purification recovery system; or (2) feeding the mixture into a hydrogenation reaction system, generating a succinic anhydride mixture through total hydrogenation, carrying out gas-liquid separation, feeding hydrogen into the hydrogenation reaction system for recycling, feeding the reaction liquid into a solvent analysis system, carrying out negative pressure flash evaporation to separate crude succinic anhydride containing light components and a solvent containing heavy components, feeding the crude succinic anhydride into a product refining system, feeding a tower bottom material into a product tower for rectification after the light components are removed from a light component removing tower at negative pressure to obtain a succinic anhydride product, and feeding the solvent containing heavy components into a solvent purification recovery system; the solvent containing heavy components is washed by desalted water in a solvent recovery system, the acidic components in the solvent are extracted, the solvent is sent to a centrifuge to separate a water phase and a solvent phase, the solvent is sent back to a solvent absorption system for recycling, and the water phase is sent to a wastewater treatment system.
All operating conditions were the same as in example 10. The solvent used was dibutyl adipate and the properties of the corresponding solvents are shown in table 1. After the device runs steadily, the results of succinic anhydride yield, butane unit consumption, solvent recovery rate, product purity and the like are shown in Table 2.
Example 12 co-production of maleic anhydride and succinic anhydride from butane was performed as follows: the maleic anhydride gas generated by butane oxidation reaction is sent to a solvent absorption system for gas-liquid separation, the gas is sent to an oxidation reaction system for recycling after washing by desalted water or sent to a tail gas incinerator for burning, the absorption liquid is sent to a hydrogenation reaction system for obtaining mixed materials of succinic anhydride and maleic anhydride after partial hydrogenation, hydrogen is sent to the hydrogenation reaction system for recycling after gas-liquid separation, the reaction liquid is sent to a solvent analysis system again, light components, maleic anhydride and succinic anhydride materials are separated from solvent and heavy component materials through negative pressure flash evaporation, the maleic anhydride and succinic anhydride materials containing the light components are sent to a product refining system, after the light components are removed by a light component removal tower under negative pressure, the bottom materials are sent to a product tower for fractional distillation to obtain two products of maleic anhydride and succinic anhydride, the solvent containing the heavy components is sent to a solvent purification recovery system, after washing by desalted water and extracting the acid components therein, the water phase and the solvent phase are separated by a centrifuge, the solvent is sent to the solvent absorption tower for recycling, and the water phase is sent to a wastewater treatment system.
The operating conditions of the solvent absorption system and the operating conditions of the solvent purification and recovery system are the same as those of the embodiment 1.
The maleic anhydride partial hydrogenation reaction conditions are as follows: the reaction temperature is 60 ℃, the reaction pressure is 0.5MPa, the molar ratio of the circulating hydrogen to the fresh hydrogen to the maleic anhydride is 30:1 and the molar ratio of the maleic anhydride to the solvent is 0.5:1 respectively, and the weight ratio of the maleic anhydride to the solvent is 1:3.
The operation conditions of the product refining system are as follows: the pressure of the top of the light component removal tower is 10kPa, the temperature of the top of the tower is 130 ℃, and the temperature of the bottom of the tower is 170 ℃; the tower top pressure of the maleic anhydride product is 5kPa, the tower top temperature is 130 ℃, and the tower bottom temperature is 140 ℃; the tower top pressure of the succinic anhydride product is 5kPa, the tower top temperature is 156 ℃, and the tower bottom temperature is 205 ℃.
The solvent used was dibutyl adipate and the properties of the corresponding solvents are shown in table 1. After the device runs steadily, the results of maleic anhydride and succinic anhydride yield, butane unit consumption, solvent recovery rate, product purity and the like are shown in table 2.
Example 13 succinic anhydride is produced from benzene as a raw material by the following steps: the maleic anhydride gas generated by benzene oxidation reaction is sent to a solvent absorption system for gas-liquid separation, the gas is sent to an oxidation reaction system for recycling after washing by desalted water or sent to a tail gas incinerator for burning, the absorption liquid is sent to a hydrogenation reaction system for generating succinic anhydride mixed material through total hydrogenation, hydrogen is sent to a hydrogenation reaction system for recycling after gas-liquid separation, the reaction liquid is sent to a solvent analysis system for separating crude succinic anhydride containing light components and solvent containing heavy components through negative pressure flash evaporation, the crude succinic anhydride is sent to a product refining system for separating the light components through negative pressure, after the light components are removed through a light component removing tower, the bottom material is sent to a product tower for rectification to obtain succinic anhydride products, the solvent containing heavy components is sent to a solvent purification recovery system for washing and extracting acidic components, then sent to a centrifuge for separating water phase and solvent phase, and the solvent is sent to the solvent absorption system for recycling, and the water phase is sent to a wastewater treatment system.
The operating conditions of the solvent absorption system, the operating conditions of the maleic anhydride total hydrogenation reaction system, the operating conditions of the product refining system and the operating conditions of the solvent purification recovery system are the same as those of the example 9.
The solvent used was dibutyl hexahydrophthalate and the properties of the corresponding solvents are shown in Table 1. After the device runs steadily, the results of succinic anhydride yield, benzene unit consumption, solvent recovery rate, product purity and the like are shown in Table 2.
Example 14 co-production of maleic anhydride and succinic anhydride from benzene as raw material is carried out as follows: the maleic anhydride gas generated by benzene oxidation reaction is sent to a solvent absorption system for gas-liquid separation, the gas is sent to an oxidation reaction system for recycling after washing by desalted water or sent to a tail gas incinerator for burning, the absorption liquid is sent to a hydrogenation reaction system for obtaining succinic anhydride and maleic anhydride mixed materials through partial hydrogenation, after gas-liquid separation, hydrogen is sent to the hydrogenation reaction system for recycling, the reaction liquid is sent to a solvent analysis system again, light components, maleic anhydride and succinic anhydride materials are separated from solvent and heavy component materials through negative pressure flash evaporation, the maleic anhydride and succinic anhydride materials containing the light components are sent to a product refining system, after the light components are removed by a light component removal tower under negative pressure, the bottom materials are sent to a product tower for fractional distillation to obtain maleic anhydride and succinic anhydride, the solvent containing the heavy components is sent to a solvent purification recovery system, after washing by desalted water and extracting the acid components therein, the solvent is sent to a centrifuge for separating water phase and solvent phase, the solvent is sent to a solvent absorption tower for recycling, and the water phase is sent to a wastewater treatment system.
The solvent absorption system operating conditions, maleic anhydride partial hydrogenation reaction conditions, product refining system operating conditions and solvent purification recovery system operating conditions were the same as in example 12.
The solvent used was dibutyl sebacate and the properties of the corresponding solvents are shown in Table 1. After the device runs steadily, the results of maleic anhydride and succinic anhydride yield, benzene unit consumption, solvent recovery rate, product purity and the like are shown in table 2.
TABLE 1 physical Properties of the Main byproduct and part of the solvent for the production of maleic anhydride and succinic anhydride
TABLE 2 application Effect of solvents satisfying both Maleic Anhydride (MA) and Succinic Anhydride (SA) production
The foregoing description of the preferred embodiments of the invention is not intended to limit the invention to the precise form disclosed, and any such modifications, equivalents, and alternatives falling within the spirit and scope of the invention are intended to be included within the scope of the invention.
Claims (4)
1. The application of the solvent for co-producing maleic anhydride and succinic anhydride is characterized in that the solvent is C 7 ～C 12 Saturated aliphatic or cycloalkyl or aromatic ethers, C 2 ～C 10 Saturated C of saturated dihydric alcohol 2 ～C 10 Fatty acid diester or naphthenic acid diester or aromatic acid diester, C of glycerin 3 ～C 6 Triesters of saturated fatty acids, C 2 ～C 10 C of dibasic saturated fatty acids 1 ～C 10 Alkyl or cycloalkyl or aryl diesters, C 8 C of dibasic aromatic acid or naphthenic acid 2 ～C 8 Alkyl diester, C 12 ～C 18 Saturated aromatic ketone, C 3 ～C 8 Alkyl phosphotriester or triphenyl phosphite, or a combination of any two or more thereof;
the solvent is used for co-producing maleic anhydride and succinic anhydride, and specifically comprises the following steps: the method comprises the steps of sending maleic anhydride gas generated by butane or benzene oxidation reaction of raw materials into a solvent absorption system for gas-liquid separation, sending the gas back to an oxidation reaction system for recycling or sending the gas back to a tail gas incinerator for incineration after washing by desalted water, sending absorption liquid into a hydrogenation reaction system for obtaining succinic anhydride and maleic anhydride mixed materials through partial hydrogenation, sending hydrogen back to the hydrogenation reaction system for recycling after gas-liquid separation, sending reaction liquid into a solvent analysis system again, separating light components, maleic anhydride and succinic anhydride materials from solvent and heavy component materials through negative pressure flash evaporation, sending the maleic anhydride and succinic anhydride materials containing the light components into a product refining system, sending the bottom materials into a product tower for fractional distillation to obtain two products of maleic anhydride and succinic anhydride after removing the light components by negative pressure of a light component removing tower, sending the solvent containing the heavy components into a solvent purification recovery system, sending the solvent to a centrifuge for separating water phase and a solvent phase after washing by desalted water and extracting the acid components, sending the solvent back to the solvent absorption tower for recycling, and sending the water phase into a wastewater treatment system.
2. Use of a solvent for co-production of maleic anhydride and succinic anhydride according to claim 1, wherein the solvent is didecyl ether, dibenzyl ether, or 2, 4-trimethyl-1, 3-pentanediol diisobutyrate, tripropionic acid glyceride, triisobutyric acid glyceride, tributyrin, dibutyl or dipentyl succinate, adipic acid C 4 ～C 6 Alkyl diesters, dimethyl or diethyl suberate, nonyldioatesAcid C 1 ～C 4 Alkyl diester, sebacic acid C 1 ～C 4 Alkyl diester, dibutyl terephthalate, diethyl isophthalate, and phthalic acid C 1 ～C 8 Alkyl diester, hexahydrophthalic acid C 2 ～C 8 Alkyl diester, phenyl hexyl ketone, phenyl heptyl ketone, triphenyl phosphite or tributyl phosphate, or a combination of any two or more thereof.
3. The use of a solvent for co-production of maleic anhydride and succinic anhydride according to claim 1, wherein the solvent is didecyl ether, tributyrin, dipentyl succinate, dibutyl adipate, diethyl sebacate, diisobutyl sebacate, dibutyl sebacate, diisobutyl phthalate, dibutyl phthalate, diethyl isophthalate, dipropyl hexahydrophthalate, diisobutyl hexahydrophthalate, dibutyl hexahydrophthalate or triphenyl phosphite, or a combination of any two or more thereof.
4. Use of a solvent for co-production of maleic anhydride and succinic anhydride according to any one of claims 1 to 3, characterized in that maleic anhydride absorption liquid is fed to Pd/Al packing 2 O 3 The trickle bed reactor of the catalyst carries out partial liquid phase hydrogenation reaction at the reaction temperature of 40-70 ℃ and the reaction pressure of 0.5-1.0 MPa, the molar ratio of circulating hydrogen to fresh hydrogen to maleic anhydride is 5-50:1 and the molar ratio of maleic anhydride to solvent is 0.5-1.0:1 respectively, and the weight ratio of maleic anhydride to solvent is 1:0.5-5.
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| CN113651783A (en) * | 2021-08-18 | 2021-11-16 | 上海师范大学 | Method for producing maleic anhydride and succinic anhydride in switching mode |
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| EP1435354A4 (en) * | 2001-10-09 | 2005-01-19 | Nippon Catalytic Chem Ind | Succinic anhydride, process for preparation of the same and use thereof |
| MY155387A (en) * | 2008-10-21 | 2015-10-15 | Huntsman Petrochemical Llc | High pore volume vpo catalyst for maleic anhydride production |
| CN101891718B (en) * | 2009-05-22 | 2012-07-25 | 山西侨友化工股份有限公司 | Continuous production process for preparing succinyl oxide by maleic anhydride hydrogenation |
| CN101735182B (en) * | 2009-12-07 | 2011-08-17 | 山西大学 | Process for continuously producing succinic anhydride through hydrogenation of maleic anhydride |
| US8901321B2 (en) * | 2010-12-13 | 2014-12-02 | Conser Spa | Process for recovery of maleic anhydride by using organic solvent |
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| CN103570650B (en) * | 2013-11-13 | 2015-05-13 | 山西大学 | Technological process for continuously producing succinic anhydride and co-producing succinic acid through maleic anhydride hydrogenation |
| CN104193708B (en) * | 2014-07-31 | 2016-04-13 | 常州瑞华化工工程技术有限公司 | A kind of method and apparatus isolating cis-butenedioic anhydride from the gaseous stream containing cis-butenedioic anhydride |
| CN105111171B (en) * | 2015-09-09 | 2017-11-07 | 淄博齐翔腾达化工股份有限公司 | Using hexahydro-phthalic acid diisobutyl ester as the technique of solvent recovery cis-butenedioic anhydride |
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