CN110054542B - Method for removing butadiene by hydrogenation of C4 component added with regulator - Google Patents
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- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/03—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of non-aromatic carbon-to-carbon double bonds
- C07C5/05—Partial hydrogenation
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Abstract
The invention discloses a method for removing butadiene by hydrogenating C4 component added with a regulator, wherein the loading amount of catalysts of a first-stage hydrogenation reactor and a second-stage hydrogenation reactor is 5m3The catalyst consists of an active component, a selective assistant and a support carrier, wherein the active component is Pd, the selective assistant is Co, Ru and Ag, and the support carrier is a mixture of gamma Al2O3, CeO2-ZrO2 and attapulgite; the molar ratio of the total input of H2 to the diolefins in the raw materials is 2-4, the input of hydrogen of the first-stage hydrogenation reactor accounts for 50-90% of the total input, and the input of hydrogen of the second-stage hydrogenation reactor accounts for 10-50% of the total input; the hydrogenation reaction pressure is 2.2Mpa, after the reaction is stable, a regulator with the flow rate of 0.2Nm/h is introduced into the hydrogenation main for 10h, the regulator is a mixed gas of hydrogen sulfide and N2, the volume concentration of the hydrogen sulfide in the regulator is 0.05-1%, and the balance is N2.
Description
Technical Field
The invention relates to a method for removing butadiene through selective hydrogenation of four carbon groups, in particular to a method for removing butadiene through hydrogenation of C4 component added with a regulator, which has the depth of butadiene removal and the yield of 1-butene.
Background
The carbon four components are the general names of alkane, mono-olefin and dialkene and mainly come from petroleum olefin cracking and coal chemical engineering MTO device products. The petroleum olefin cracking device mainly produces ethylene and co-produces propylene and four carbon components, wherein the four carbon components mainly produce MTBE and mono-butylene; the coal chemical MTO device is used for preparing olefin, ethylene and propylene, and simultaneously generating partial C-IV products, wherein the C-IV products are used for producing MTBE, 1-butylene, 2PH and other products. Since the four carbon components contain diolefins, which tend to polymerize under certain conditions and block the catalyst channels of the integrated units producing MTBE, 1-butene and 2PH, they must be removed prior to subsequent processing. The removal method currently in common use is selective hydrogenation. The selective hydrogenation is that the carbon four components react with hydrogen under the action of a catalyst, and besides main reactions such as diene removal, side reactions are also accompanied, such as diene isomerization reaction, 1-butene hydrogenation saturation reaction, isobutene hydrogenation saturation reaction and the like, and the side reactions can cause loss of valuable components (1-butene and the like) in the raw materials.
The existing selective hydrogenation equipment for four carbon groups comprises two-section selective hydrogenation, and is provided with a first-section hydrogenation reactor, a second-section hydrogenation reactor, a buffer tank, a preheater, a flow control valve, a hydrogenation device and the like, wherein the hydrogenation device is divided into two branches after passing through a hydrogenation main path, each branch is divided into a middle branch and a lower branch, the two branches enter the hydrogenation reactor from the middle part and the lower part of the hydrogenation reactor respectively, and the hydrogenation amount of each hydrogenation reactor is distributed by a flow valve in a pipeline. The upstream C4 raw material is dehydrated, preheated, mixed with hydrogen in the lower branch path, then enters the lower part of the first-stage hydrogenation reactor, is subjected to primary catalytic hydrogenation reaction, then is mixed with hydrogen in the lower branch path of the second-stage hydrogenation reactor, enters the second-stage hydrogenation reactor, and is condensed and flashed after secondary catalytic hydrogenation reaction, and then is output. The catalyst used at present has high striving activity and large specific surface area, increases side reactions while pursuing a main reaction, basically has the problem that the depth of butadiene removal and the yield of 1-butene cannot be considered simultaneously, the depth of butadiene removal (residual amount) is more than 1ppm, and the yield of 1-butene is less than 99%.
Disclosure of Invention
The invention aims to solve the technical problems in the prior art and provides a method for removing butadiene by hydrogenation of a C4 component added with a regulator, which has the depth of butadiene removal and the yield of 1-butene.
The technical solution of the invention is as follows: a method for removing butadiene by hydrogenation of C4 component added with a regulator adopts a two-stage selective hydrogenation device with a first-stage hydrogenation reactor and a second-stage hydrogenation reactor, and is characterized in that:
the loading of the catalyst in the first-stage hydrogenation reactor and the second-stage hydrogenation reactor is 5m3The catalyst consists of an active component, a selective assistant and a support carrier, wherein the active component is Pd, the selective assistant is Co, Ru and Ag, and the support carrier is a mixture of gamma Al2O3, CeO2-ZrO2 and attapulgite; the mass percentages of the Pd, the selective assistants Co, Ru and Ag and the gamma Al2O3, CeO2-ZrO2 and the attapulgite in the support carrier are respectively 50-60%, 30-40% and 10-20%;
the molar ratio of the total input of H2 to the diolefins in the raw materials is 2-4, the input of hydrogen of a first-stage hydrogenation reactor accounts for 50-90% of the total input, the input of hydrogen of a second-stage hydrogenation reactor accounts for 10-50% of the total input, and the hydrogen of a middle branch and a lower branch of each section of hydrogenation reactor respectively accounts for 50%;
the hydrogenation reaction pressure is 2.2Mpa, after the reaction is stable, a regulator with the flow rate of 0.2Nm/h is introduced into the hydrogenation main for 10h, the regulator is a mixed gas of hydrogen sulfide and N2, the volume concentration of the hydrogen sulfide in the regulator is 0.05-1%, and the balance is N2.
The invention is a two-stage selective hydrogenation process, which adopts a high-selectivity hydrogenation catalyst and a regulator and controls H2The concentration and the addition of the S can partially inactivate the active components on the surface of the catalyst, thus meeting the requirement of generating the 1-butene by butadiene hydrogenation, leading the depth of butadiene removal to be 0.97ppm, avoiding generating excessive side reactions, leading the yield of the 1-butene to be 100.29 percent and being widely applicable to large-scale industrial production.
Detailed Description
The method for removing butadiene by hydrogenating the C4 component added with the regulator adopts two-stage selective hydrogenation equipment with a first-stage hydrogenation reactor and a second-stage hydrogenation reactor, and is specifically designed as follows:
the loading of the catalyst in the first-stage hydrogenation reactor and the second-stage hydrogenation reactor is 5m3The catalyst consists of an active component, a selective assistant and a support carrier, wherein the active component is Pd, the selective assistant is Co, Ru and Ag, and the support carrier is a mixture of gamma Al2O3, CeO2-ZrO2 and attapulgite; the mass percentages of the Pd and the selective assistants Co, Ru and Ag in the support carrier are respectively 50%, 40% and 10%, and the mass percentages of the gamma Al2O3, the CeO2-ZrO2 and the attapulgite in the support carrier are respectively 1% of the mass of the support carrier;
the preparation method of the catalyst is carried out according to the following steps in sequence:
a. weighing 1000g of CeCl3 and 1000g of ZrCl4, preparing 2L of aqueous solution and 0.35% ammonia aqueous solution by mass concentration, generating a CeO2-ZrO2 mixture by a coprecipitation method, washing the CeO2-ZrO2 until the mixture is free of Cl < - >, and drying the mixture at 120 ℃ for 5 hours to prepare 1150g of CeO2-ZrO2Mixing;
b. taking 400g of CeO2-ZrO2, 500g of gamma Al2O3 and 100g of attapulgite, uniformly mixing the materials by using a stirrer, extruding the materials into 1/8' strips by using a strip extruding machine or preparing the strips into 1.7-2.5mm spherical particles by using a sugar coating machine, curing the particles for 24 hours by using water mist, airing the particles, heating the particles to 450 ℃ by using an N2 protection program, and roasting the particles to prepare a catalyst support carrier;
c. with quantitative PdCl2, CoCl2Heating and dissolving RuCl3, AgNO3, 2ml of concentrated hydrochloric acid with the mass concentration of 37% and 200ml of deionized water to prepare a mixed solution;
d. soaking 500g of the prepared catalyst support carrier in an equal volume of mixed solution for 1h, then soaking the catalyst support carrier in 500ml of glucose (reduction catalyst) with the mass concentration of 2% for 1h, washing the catalyst support carrier with water until no Cl < - >, drying the catalyst support carrier at 120 ℃ for 12h after air drying.
The C4 feeding amount (the index is shown in table 1) is 15t/h, the total hydrogen addition amount is 9.93-19.86 Kg/h, the hydrogen addition amount of the first-stage hydrogenation reactor accounts for 80% of the total hydrogen addition amount, the hydrogen addition amount of the second-stage hydrogenation reactor accounts for 20% of the total hydrogen addition amount, and the hydrogen of the middle branch and the lower branch of each-stage hydrogenation reactor respectively accounts for 50%;
the hydrogenation reaction pressure is 2.2Mpa, after the first device is started and operated, the contents of raw materials, diene products and 1-butene are detected by chromatography, when the reaction is stable, a regulator with the flow rate of 0.2Nm/h is introduced into a hydrogenation main path for 10h, the regulator is mixed gas of hydrogen sulfide and N2, the volume concentration of the hydrogen sulfide in the regulator is 0.01%, and the balance is N2.
After 1 month of operation, the high selectivity regulator (comparative example) and the inventive example were not injected and the indexes are shown in tables 2 and 3, respectively.
TABLE 1
| Serial number | Components | kg/h | wt% |
| 1 | Propylene (PA) | 133.5 | 0.89 |
| 2 | Propane | 87 | 0.58 |
| 3 | Isobutane | 22.5 | 0.15 |
| 4 | N-butane | 685.5 | 4.57 |
| 5 | Isobutene | 841.5 | 5.61 |
| 6 | N-butene | 3858 | 25.72 |
| 7 | Cis-butenediol | 3913.5 | 26.09 |
| 8 | Butene of trans-butene | 5190 | 34.6 |
| 9 | Butadiene | 268.5 | 1.79 |
| Total of | 15000 | 100 |
TABLE 2
| Serial number | Components | kg/h | wt% |
| 1 | Propylene (PA) | 133.50 | 0.89 |
| 2 | Propane | 87.00 | 0.58 |
| 3 | Isobutane | 32.50 | 0.22 |
| 4 | N-butane | 754.30 | 5.03 |
| 5 | Isobutene | 925.40 | 6.17 |
| 6 | N-butene | 3840.38 | 25.60 |
| 7 | Cis-butenediol | 3962.40 | 26.42 |
| 8 | Butene of trans-butene | 5263.10 | 35.09 |
| 9 | Butadiene | 1.43 | 0.000095 |
| Total of | 15000 | 100 |
TABLE 3
| Serial number | Components | kg/h | wt% |
| 1 | Propylene (PA) | 133.50 | 0.89 |
| 2 | Propane | 87.00 | 0.58 |
| 3 | Isobutane | 27.50 | 0.18 |
| 4 | N-butane | 704.30 | 4.70 |
| 5 | Isobutene | 922.30 | 6.15 |
| 6 | N-butene | 3869.25 | 25.80 |
| 7 | Cis-butenediol | 3971.60 | 26.48 |
| 8 | Butene of trans-butene | 5283.10 | 35.22 |
| 9 | Butadiene | 1.450 | 0.000097 |
| Total of | 15000 | 100 |
The performance comparison of the inventive examples and comparative examples is shown in Table 4.
TABLE 4
| Item | Depth ppm of butadiene removal | 1-butene yield% |
| Comparative example | 0.95 | 99.16 |
| Examples of the invention | 0.97 | 100.29 |
As can be seen by comparison, the diene removal depth of the embodiment of the invention is 0.97ppm, the 1-butene yield is 100.29%, the butadiene removal depth and the 1-butene yield are both considered, and the large-scale industrial production can be satisfied.
Claims (1)
1. A method for removing butadiene by hydrogenation of C4 component added with a regulator adopts a two-stage selective hydrogenation device with a first-stage hydrogenation reactor and a second-stage hydrogenation reactor, and is characterized in that:
the loading of the catalyst in the first-stage hydrogenation reactor and the second-stage hydrogenation reactor is 5m3The catalyst consists of an active component, a selective assistant and a support carrier, wherein the active component is Pd, the selective assistant is Co, Ru and Ag, and the support carrier is gamma Al2O3、CeO2-ZrO2And a mixture of attapulgite; pd is 1.5% of the mass of the support carrier, the selective assistants Co, Ru and Ag are respectively 1% of the mass of the support carrier, and gamma Al2O in the support carrier3、CeO2-ZrO2The mass percentages of the attapulgite are respectively 50%, 40% and 10%;
the preparation method of the catalyst is carried out according to the following steps in sequence:
a. weighing 1000g of CeCl3And 1000g ZrCl4Preparing 2L of aqueous solution and 0.35 mass percent ammonia solution, and generating CeO by coprecipitation method2-ZrO2Mixture, washing CeO with water2-ZrO2Until the mixture is Cl-free, drying at 120 ℃ for 5h to obtain 1150gCeO2-ZrO2Mixing;
b. taking 400g CeO2-ZrO2、500gγAl2O3And 100g of attapulgite, evenly mixing the mixture by a stirrer, extruding the mixture into 1/8-shaped strips by a strip extruding machine or preparing the strips into 1.7-2.5mm spherical particles by a sugar coating machine, curing the particles for 24 hours by water mist, drying the particles in the air, heating the particles to 450 ℃ by adopting an N2 protection program, and roasting the particles to prepare a catalyst support carrier;
c. with quantitative PdCl2、CoCl2、RuCl3、AgNO32ml mass concentration ofHeating and dissolving 37% concentrated hydrochloric acid and 200ml deionized water to prepare a mixed solution;
d. soaking 500g of the prepared catalyst support carrier in an equal volume of mixed solution for 1h, then soaking the catalyst support carrier in 500ml of glucose with the mass concentration of 2% for 1h, washing the catalyst support carrier with water until no Cl & lt- & gt exists, drying the catalyst support carrier in the air, and drying the catalyst support carrier at 120 ℃ for 12 h;
the C4 feeding amount is 15t/h, the total hydrogen addition amount is 9.93-19.86 Kg/h, the hydrogen input amount of the first-stage hydrogenation reactor accounts for 80% of the total hydrogen input amount, the hydrogen input amount of the second-stage hydrogenation reactor accounts for 20% of the total hydrogen input amount, and the hydrogen of the middle branch and the hydrogen of the lower branch of each-stage hydrogenation reactor respectively account for 50%;
the hydrogenation reaction pressure is 2.2Mpa, after the first device is started and operated, the contents of raw materials, products of alkadiene and 1-butene are detected by chromatography, when the reaction is stable, a regulator with the flow rate of 0.2Nm/h is introduced into the hydrogenation main path for 10h, and the regulator is hydrogen sulfide and N2The volume concentration of hydrogen sulfide in the mixed gas and the regulator is 0.01 percent, and the balance is N2。
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