CN115710153A - Carbon four-alkyne hydrogenation method and device - Google Patents
Carbon four-alkyne hydrogenation method and device Download PDFInfo
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- CN115710153A CN115710153A CN202110970714.5A CN202110970714A CN115710153A CN 115710153 A CN115710153 A CN 115710153A CN 202110970714 A CN202110970714 A CN 202110970714A CN 115710153 A CN115710153 A CN 115710153A
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Abstract
The invention belongs to the field of acetylene-rich C4 recovery, and discloses a C-C four alkyne hydrogenation method and device. The apparatus of the present invention comprises: the device comprises a supercharging device, a condenser, a water washing tower, a dewatering device, a hydrogenation reactor, a hydrogenation separation tank, a hydrogenation aftercooler, a circulation cooler, a stabilizer condenser and a stabilizer reboiler. Three alkyne-rich carbon four-hydrogenation reaction processes are realized through pressurization, liquefaction, washing for impurity removal, dehydration, hydrogenation and separation processes, all tail gas containing alkyne and impurity in the butadiene device can be treated, the problem of treatment of carbon four alkyne is solved, and the economic benefit of the device is increased.
Description
Technical Field
The invention belongs to the field of acetylene-rich C4 recovery, and particularly relates to a C4 alkyne hydrogenation method and device.
Background
In the past, because no proper recovery method exists for acetylene-rich carbon four tail gas of a butadiene extraction device, a large amount of carbon four raffinate is usually needed to dilute the tail gas and then the tail gas is used as fuel gas or directly discharged to a torch, so that great waste is caused. At present, the acetylene hydrocarbon tail gas hydrogenation process which is successfully developed at home and abroad can selectively hydrogenate and convert the acetylene carbon-rich four tail gas into butene-1 or butadiene so as to achieve the aim of changing waste into valuable, thereby achieving the effects of reducing acetylene hydrocarbon emission and preventing environmental pollution. The liquid phase hydrogenation technical route has the advantages of small hydrogen and hydrocarbon ratio, low reaction temperature, low energy consumption and good economic benefit and is gradually and widely applied. And the butadiene device, especially the carbon tetraalkyne tail gas of the DMF method, is sent out of a battery limit area in a low-pressure gas phase mode, so a pressurizing and liquefying process is needed in the butt joint process with the liquid phase hydrogenation, and the requirements of the liquid phase hydrogenation reactor catalyst on water content and solvent content are very strict, so a water washing impurity removal and dehydration process is needed. The liquid phase hydrogenation is divided into a full hydrogenation process, a selective hydrogenation butene-1 preparation process and a selective hydrogenation butadiene preparation process, and the prior art does not mention the realization of the three processes by using one-stage liquid phase hydrogenation.
CN102294203A discloses a carbon four two-stage hydrogenation device and a process in the preparation of ethylene by catalytic thermal cracking, which avoid the problems of coking of a reactor and reduction of the service life of a catalyst and the operation period of the device caused by deep hydrogenation of 1, 3-butadiene by adopting two-stage selective hydrogenation, can directly hydrogenate mixed carbon four, and improve the utilization rate of raw materials. But the flow is longer, the second-stage hydrogenation needs a recycle hydrogen compressor and the like, and the investment is higher.
CN105566032 discloses a selective hydrogenation process of alkyne-rich C four, namely, C four alkyne which is a byproduct of a butadiene extraction device is firstly separated by a rectifying tower, and a material at the top of the tower is extracted after selective hydrogenation and alkyne removal.
CN1590513A discloses a process for the selective hydrogenation of hydrocarbon streams rich in acetylenes. The method is characterized in that a residual alkyne-rich material in a butadiene extraction device passes through a fixed bed hydrogenation reactor with a circulating device, hydrogen and alkyne are returned to remove alkyne by selective hydrogenation in a liquid state, and then the hydrogen and alkyne are returned to the butadiene extraction device. The technology has the characteristics that firstly, the route is single, only the acetylene hydrocarbon hydrogenation is involved to prepare butadiene, and the butene-1 preparation is not involved; secondly, a stabilizing tower is not used for removing light components and heavy components, so that the conditions that the light components and the heavy components entering a butadiene device are too high, the load of equipment and pipelines is increased or blocked and the like can easily occur; and finally, the hydrogenation circulating material is not cooled, so that the temperature of a reaction inlet cannot be controlled, the temperature is easy to fly, and the top of a vapor-liquid separation tank is not provided with an aftercooler, so that the loss of light components with carbon IV is easily caused. The process operability is poor.
CN110963878A discloses a recovery method of carbon tetraalkyne tail gas. The patent recovers carbon four through liquefaction, impurity removal and hydrogenation reactions. According to the technology, only the heavy components are removed through the buffer tank, the requirement of the reactor catalyst on the impurity content cannot be met, two sections of hydrogenation reactors are adopted, the equipment investment is high, the product of the light component removal tower kettle is easy to contain polymers produced in the reaction process, the product purity cannot be guaranteed, and the flare directly discharged from the top of the tower is easy to carry four components of carbon to cause material loss.
Therefore, aiming at the defects of the existing liquid phase hydrogenation process and solving the problem of utilization of alkyne-rich C-IV tail gas of the existing butadiene device, a new C-IV alkyne hydrogenation device and a method are urgently needed to be provided.
Disclosure of Invention
The invention aims to provide a method and a device for hydrogenating C-C alkyne, aiming at the defects of the prior art. The invention realizes three alkyne-rich carbon four-hydrogenation reaction processes through pressurization, liquefaction, washing for impurity removal, dehydration, hydrogenation and separation processes, can treat all tail gases containing alkyne and impurity in a butadiene device, solves the problem of treatment of carbon four alkyne, and increases the economic benefit of the device.
In order to achieve the above objects, the present invention provides a four-carbon alkyne hydrogenation apparatus, which comprises a pressurizing device, a liquefaction condensation unit, a dehydration unit, a hydrogenation reactor, a hydrogenation separation tank, a hydrogenation aftercooler, a circulation cooler, a stabilization tower, and optionally a water washing tower;
the gas-phase impurity-containing alkyne-carbon-rich four-raw material feeding pipeline is connected with the inlet of the pressurizing device;
the outlet of the pressure boosting device is connected with the inlet of the liquefaction condensation unit;
the outlet of the liquefaction condensation unit is connected with the inlet of the dehydration unit; optionally, the outlet of the liquefaction condensation unit is connected with the inlet of the water washing tower, and the top outlet of the water washing tower is connected with the inlet of the dehydration unit;
the outlet of the organic phase of the dehydration unit is connected with a four-feed pipeline for removing impurities, dehydrating and enriching alkyne carbon;
the four alkyne-enriched carbon feeding pipeline for impurity removal and dehydration, the outlet connecting pipeline of the circulating cooler and the hydrogen feeding pipeline are connected to the inlet pipeline of the hydrogenation reactor;
the outlet of the hydrogenation reactor is connected with the first inlet of the hydrogenation separation tank;
the outlet at the top of the hydrogenation separation tank is connected with the inlet of the hydrogenation aftercooler; the liquid phase outlet of the hydrogenation aftercooler is connected with the second inlet of the hydrogenation separation tank, and the gas phase outlet of the hydrogenation aftercooler is connected with a purge gas output pipeline; an outlet pipeline at the bottom of the hydrogenation separation tank is respectively connected with a four hydrogenation cycle carbon pipeline and a middle inlet of the stabilizing tower; the four hydrogenation circulating carbon pipelines are connected with the inlet of the circulating cooler.
In another aspect, the present invention provides a carbon tetraalkyne hydrogenation method, which uses the carbon tetraalkyne hydrogenation apparatus, and includes the following steps:
s1: sequentially passing the gas-phase impurity-containing alkyne-rich carbon four raw material through the supercharging equipment, the liquefaction condensation unit and the dehydration unit, and sequentially performing supercharging, condensation liquefaction and dehydration treatment to obtain impurity-removed dehydrated alkyne-rich carbon four and a water phase of the dehydration unit; optionally, washing impurity removal treatment is further included between the condensation treatment and the dehydration treatment to obtain a water phase of the washing tower;
s2: the impurity-removed and dehydrated alkyne-enriched C4, hydrogen and hydrogenation cycle C4 are sent to the hydrogenation reactor together for hydrogenation reaction;
s3: sending the discharge of the hydrogenation reactor to the hydrogenation separation tank through a first inlet of the hydrogenation separation tank; sending the light components separated from the hydrogenation separation tank into the hydrogenation aftercooler, sending the liquid phase obtained by cooling through the hydrogenation aftercooler back into the hydrogenation separation tank through a second inlet of the hydrogenation separation tank, and sending the uncondensed purge gas obtained by cooling through the hydrogenation aftercooler out of the device;
s4: and cooling a part of the bottom liquid phase separated by the hydrogenation separation tank by the circulating cooler, sending the cooled part of the bottom liquid phase to the hydrogenation reactor as the hydrogenation circulating carbon IV, sending the other part of the bottom liquid phase to the middle part of the stabilizing tower, and treating the cooled part of the bottom liquid phase by the stabilizing tower to obtain a gas phase product at the top of the stabilizing tower, a bottom product of the stabilizing tower and a hydrogenation product.
The technical scheme of the invention has the following beneficial effects:
1) The energy consumption of the liquefaction process of the liquefaction condensation unit is reduced through the acetylene-rich carbon four-tail gas pressurization process;
2) According to the invention, water-soluble impurities such as a solvent in the alkyne-rich carbon four tail gas are removed through a washing process of the washing tower, so that the influence on the hydrogenation catalyst is avoided;
3) According to the invention, through reasonably setting the heat exchange sequence, the energy of the first-stage condenser and the second-stage condenser is utilized in a grading manner, the energy consumption of the system is reduced, and the economic benefit of the device is improved;
4) According to the invention, the decanter, the settler and the coalescer are arranged in the dehydration unit in a grading manner, so that the water content is reduced to the maximum extent, and the influence on the catalyst of the hydrogenation reactor is avoided;
5) The invention can process all the acetylene-rich tail gas by-products of the butadiene device by the processes of pressurization, liquefaction, water washing, dehydration and hydrogenation, and further can carry out hydrogenation treatment on all the gas-phase unsaturated carbon IV, and the water washing step can be eliminated if the raw material does not contain water-soluble impurities.
6) The invention can realize three acetylene-rich carbon four-hydrogenation reaction processes such as a full-hydrogenation butane preparation process, a selective hydrogenation butene-1 preparation process, a selective hydrogenation butadiene preparation process and the like through a one-stage liquid phase hydrogenation device.
7) The device of the invention obtains the hydrogenation product through the side line extraction of the rectifying tower, ensures the product purity and saves the equipment investment.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The above and other objects, features and advantages of the present invention will become more apparent by describing in detail exemplary embodiments thereof with reference to the attached drawings, wherein like reference numerals generally represent like parts in the exemplary embodiments of the present invention.
FIG. 1 shows a schematic diagram of a four-carbon alkyne hydrogenation apparatus provided by the present invention.
Fig. 2 shows a schematic diagram of a four-carbon alkyne hydrogenation apparatus provided in example 1 of the present invention.
Description of reference numerals:
1. a pressure boosting device; 2. a liquefaction and condensation unit; 2-1, a first-stage condenser; 2-2, a secondary condenser; 3. washing the tower with water; 4. a dehydration unit; 4-1, a decanter; 4-2, a settler; 4-3, a coalescer; 5. a hydrogenation reactor; 6. a hydrogenation separation tank; 7. a hydrogenation aftercooler; 8. a circulation pump; 9. a circulating cooler; 10. a stabilizer tower; 11. a stabilizer condenser; 12. a stabilizer reboiler; 13. a reaction feed pump; 14. a gas-phase impurity-containing alkyne-carbon-rich four-raw material feed line; 15. a condensing medium; 15-1, cooling water; 15-2, propylene; 16. a washing water feed line of the water wash tower; 17. a waste water discharge line; 18. a hydrogen feed line; 19. a purge gas output line; 20. a hydrogenated product discharge line; 21. a stabilizer column bottoms discharge line; 22. an alkyne knockout drum; 23. a water washing pump; 24. a de-impurity and de-water alkyne-rich carbon four feed line; 25. a water phase outlet line of the dehydration unit; 26. a decanter aqueous phase outlet line; 27. a settler aqueous phase outlet line; 28. a coalescer aqueous phase outlet line; 29. a water phase outlet pipeline at the bottom of the water washing tower; 30. the outlet of the circulating cooler is connected with a pipeline; 31. a first inlet of the hydro-separation tank; 32. a second inlet of the hydro-separation tank; 33. a carbon four hydrogenation cycle line; 34. an inlet line to the hydrogenation reactor; 35. a middle inlet of the stabilizer column; 36. a gas phase product discharge pipeline at the top of the stabilizer tower.
Detailed Description
Preferred embodiments of the present invention will be described in more detail below. While the following describes preferred embodiments of the present invention, it should be understood that the present invention may be embodied in various forms and should not be limited by the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art.
The invention provides a carbon tetraalkyne hydrogenation device which comprises a supercharging device, a liquefaction condensation unit, a dehydration unit, a hydrogenation reactor, a hydrogenation separation tank, a hydrogenation aftercooler, a circulating cooler, a stabilizing tower and an optional water washing tower, wherein the water washing tower is arranged in the hydrogenation separation tank;
the gas-phase impurity-containing alkyne-carbon-rich four-raw material feeding pipeline is connected with the inlet of the pressurizing device;
the outlet of the pressure boosting device is connected with the inlet of the liquefaction condensation unit;
the outlet of the liquefaction condensation unit is connected with the inlet of the dehydration unit; optionally, the outlet of the liquefaction condensation unit is connected with the inlet of the water washing tower, and the top outlet of the water washing tower is connected with the inlet of the dehydration unit;
the organic phase outlet of the dehydration unit is connected with a four-feeding pipeline for impurity-removing, dehydration and alkyne-rich carbon;
the four alkyne-enriched carbon feeding pipeline for impurity removal and dehydration, the outlet connecting pipeline of the circulating cooler and the hydrogen feeding pipeline are connected to the inlet pipeline of the hydrogenation reactor;
the outlet of the hydrogenation reactor is connected with the first inlet of the hydrogenation separation tank;
the outlet at the top of the hydrogenation separation tank is connected with the inlet of the hydrogenation aftercooler; the liquid phase outlet of the hydrogenation aftercooler is connected with the second inlet of the hydrogenation separation tank, and the gas phase outlet of the hydrogenation aftercooler is connected with a purge gas output pipeline; an outlet pipeline at the bottom of the hydrogenation separation tank is respectively connected with a four hydrogenation cycle carbon pipeline and a middle inlet of the stabilizing tower; the four hydrogenation circulating carbon pipelines are connected with the inlet of the circulating cooler.
In the invention, an outlet pipeline at the bottom of the hydrogenation separation tank is divided into two paths after passing through a circulating pump, one path is connected with an inlet of a circulating cooler through four hydrogenation circulating carbon pipelines, and an outlet connecting pipeline of the circulating cooler is connected with an inlet pipeline of the hydrogenation reactor; the other path is connected to the inlet of the middle part of the stabilizing tower.
According to the present invention, preferably, the pressure boosting device is a blower or a compressor.
According to the invention, preferably, the liquefaction condensation unit comprises a primary condenser and/or a secondary condenser.
According to the invention, preferably, the top of the water washing tower is connected with a washing water feeding pipeline of the water washing tower, and the bottom of the water washing tower is connected with a water phase outlet pipeline at the bottom of the water washing tower.
According to the invention, preferably, an alkyne knockout drum and a water washing pump are further arranged between the outlet of the liquefaction condensation unit and the inlet of the water washing tower in sequence.
According to the invention, preferably, the outlet of the organic phase of the dehydration unit is connected to a de-miscellaneous dehydrated alkyne-rich carbon-four feed line via a reaction feed pump.
According to the present invention, preferably, the dewatering unit comprises at least one of a decanter, a settler and a coalescer.
According to the present invention, preferably, the dewatering unit is further provided with a dewatering unit aqueous phase outlet line comprising at least one of a decanter aqueous phase outlet line, a settler aqueous phase outlet line and a coalescer aqueous phase outlet line.
According to the present invention, preferably, the hydrogenation reactor is a downflow trickle bed reactor or an upflow reactor.
According to the invention, preferably, the outlet pipeline at the bottom of the hydrogenation separation tank is respectively connected with a four-pipeline of hydrogenation recycle carbon and the inlet at the middle part of the stabilizing tower through a circulating pump.
According to the invention, preferably, the top of the stabilizer is provided with a stabilizer condenser and a stabilizer top gas-phase product discharge line, the bottom of the stabilizer is provided with a stabilizer reboiler and a stabilizer bottom product discharge line, and the upper part of the rectifying section of the stabilizer is provided with a hydrogenated product discharge line.
In another aspect, the present invention provides a method for hydrogenating carbon tetraalkyne, which uses the apparatus for hydrogenating carbon tetraalkyne, and comprises the following steps:
s1: sequentially passing the gas-phase impurity-containing alkyne-rich carbon four raw material through the supercharging equipment, the liquefaction condensation unit and the dehydration unit, and sequentially performing supercharging, condensation liquefaction and dehydration treatment to obtain impurity-removed dehydrated alkyne-rich carbon four and a water phase of the dehydration unit; optionally, washing impurity removal treatment is further included between the condensation treatment and the dehydration treatment to obtain a water phase of the washing tower;
s2: sending the impurity-removed and dehydrated alkyne-enriched C4, hydrogen and hydrogenation cycle C4 to the hydrogenation reactor together for hydrogenation reaction;
s3: sending the discharge of the hydrogenation reactor to the hydrogenation separation tank through a first inlet of the hydrogenation separation tank; sending the light components separated from the hydrogenation separation tank into the hydrogenation aftercooler, sending the liquid phase obtained by cooling through the hydrogenation aftercooler back into the hydrogenation separation tank through a second inlet of the hydrogenation separation tank, and sending the uncondensed purge gas obtained by cooling through the hydrogenation aftercooler out of the device;
s4: and cooling a part of the bottom liquid phase separated by the hydrogenation separation tank by the circulating cooler, sending the cooled part of the bottom liquid phase to the hydrogenation reactor as the fourth hydrogenation cycle carbon, sending the other part of the bottom liquid phase to the middle part of the stabilizing tower, and treating the cooled part of the bottom liquid phase by the stabilizing tower to obtain a gas phase product at the top of the stabilizing tower, a bottom product of the stabilizing tower and a hydrogenation product.
According to the invention, in step S1, the gas-phase impurity-containing alkyne-carbon-rich feedstock is preferably fed at a temperature of 20 to 80 ℃ and at a pressure of 2 to 20kPaG.
According to the invention, in step S1, the pressure of the gas-phase impurity-enriched alkyne-carbon-tetrad feedstock after the pressurization treatment is preferably 150 to 300kPaG.
According to the present invention, preferably, in step S1, the condensing and liquefying treatment scheme is a treatment scheme using a primary condenser or a treatment scheme using a primary condenser and a secondary condenser. And through the condensation liquefaction treatment, the temperature of the gas-phase impurity-containing alkyne-carbon-rich raw material is reduced to the temperature below the corresponding condensation point under the corresponding pressure of the pressurization equipment.
According to the present invention, preferably, in step S1, the condensing medium of the primary condenser of the treatment scheme employing the primary condenser is chilled water or propylene; the condensation medium of the first-stage condenser adopting the treatment scheme of the first-stage condenser and the second-stage condenser is cooling water or process materials, and the condensation medium of the second-stage condenser is chilled water or propylene.
According to the present invention, preferably, in step S1, a treatment of removing a part of heavy components by the alkyne knockout drum is further included between the condensation treatment and the water washing impurity removal treatment.
According to the present invention, preferably, in step S1, the operating conditions of the water washing column include: the washing water feeding temperature of the washing tower is 20-50 ℃, and the tower plate number of the washing tower is 20-80.
According to the present invention, preferably, in step S1, the aqueous phase of the water washing column and the aqueous phase of the dehydration unit are sent out of the apparatus through the water washing column bottom aqueous phase outlet line and the dehydration unit aqueous phase outlet line, respectively.
According to the present invention, preferably, in step S1, the vapor phase impurity-containing alkyne-rich carbon four-feedstock comprises the vapor phase impurity-containing alkyne-rich carbon four-feedstock from the butadiene extraction unit and vapor phase unsaturated carbon four produced by other units. The impurities comprise a water-soluble solvent and a water-soluble polar organic substance, wherein the water-soluble solvent is preferably at least one or more of acetonitrile, N-dimethylformamide, N-methylpyrrolidone and N-formylmorpholine, or a mixture containing water.
According to the present invention, preferably, in step S2, the hydrogenation reaction comprises three schemes:
scheme A, carrying out selective hydrogenation on unsaturated components in the hydrogenation reactor to prepare butene-1: most of vinyl acetylene is converted into butene-1, butyne-1 is converted into butene-1, and a side reaction for generating butane is also inevitable, namely a process for preparing butene-1; according to the invention, the selective hydrogenation butene-1 preparing reaction is preferably a reaction for converting the unsaturated component into a butene-1-rich component, and in the invention, particularly, vinyl acetylene, butadiene and butyne in the unsaturated component are converted into butene-1, a small amount of butene-2 and butane to obtain the butene-1-rich component.
Scheme two, the unsaturated components in the hydrogenation reactor are subjected to selective hydrogenation to prepare butadiene: most of vinyl acetylene is converted into 1, 3-butadiene, butyne-1 is converted into butene-1, and side reactions for generating butane and butene-1 can also be inevitably generated, namely the process for preparing 1, 3-butadiene; according to the invention, the selective hydrogenation reaction for preparing butadiene is preferably a reaction for converting the unsaturated component into a butadiene-rich component, and in the invention, particularly, vinyl acetylene in the unsaturated component is converted into butadiene and a small amount of butene-1, and butyne is converted into butene-1 to obtain the butadiene-rich component.
And in the third scheme, the unsaturated components in the hydrogenation reactor are subjected to full hydrogenation to prepare alkane: the process for preparing the alkane comprises the step of converting all or most of unsaturated olefin, including vinyl acetylene, butyne-1, butene-2 (comprising cis-trans structures), isobutene and the like into corresponding alkane, namely normal butane and isobutane. According to the present invention, preferably, the all-hydrogenation alkane production reaction is a reaction of converting the unsaturated component into a saturated alkane component.
According to the present invention, preferably, the unsaturated component is at least one of vinyl acetylene, butadiene, butyne, butene-1, butene-2, and isobutylene. In the present invention, the unsaturated component includes the unsaturated component in the deduplicated, dehydrated alkyne-rich carbocycle and hydrocycle carbocycle.
According to the invention, preferably, in the reaction for preparing butene-1 by selective hydrogenation, the inlet temperature of the hydrogenation reactor is 20-70 ℃, the reaction pressure is 0.5-3 MPaG, the reaction temperature is 5-50 ℃, the molar ratio of hydrogen to acetylene is 0.5-5, the circulation ratio is 10-1, the catalyst volume space velocity is 0.1-10 h -1 The catalyst is at least one of a platinum group of noble metal, a palladium group of noble metal, a nickel group of non-noble metal and a copper group of non-noble metal. Further preferably, the inlet temperature of the hydrogenation reactor is 30-60 ℃, the reaction pressure is 1.0-2.5 MPaG, the reaction temperature is 10-30 ℃, the molar ratio of hydrogen to acetylene is 1-3, the circulation ratio is 10 -1 。
In the present invention, the hydrogen alkyne molar ratio refers to the ratio of hydrogen to the "sum of alkyne and diene moles"; the recycle ratio refers to the flow ratio of the recycle material (hydrogenation recycle C4) to the fresh feed (impurity-removing and dehydration alkyne-rich C4); the catalyst volumetric space velocity refers to the ratio of fresh feed (deduplicated and dehydrated alkyne-rich C.sub.four) to catalyst volume.
According to the invention, preferably, in the reaction for preparing butadiene by selective hydrogenation, the inlet temperature of the hydrogenation reactor is 15-70 ℃, the reaction pressure is 0.4-3 MPaG, the reaction temperature is 5-50 ℃, the molar ratio of hydrogen to acetylene is 1-3, the circulation ratio is 5 -1 The catalyst is at least one of a platinum system of noble metal, a palladium system of noble metal, a nickel system of non-noble metal and a copper system of non-noble metal; further preferably, the inlet temperature of the hydrogenation reactor is 20-50 ℃, the reaction pressure is 0.5-2 MPaG, the reaction temperature is 10-20 ℃, the circulation ratio is 15-2 h -1 。
According to the invention, preferably, in the full hydrogenation reaction, the inlet temperature of the hydrogenation reactor is 30-70 ℃, the reaction pressure is 0.5-3 MPaG, the reaction temperature is 5-60 ℃, the molar ratio of hydrogen to acetylene is 1-5, the circulation ratio is 5-40 -1 The catalyst is at least one of a platinum system of noble metal, a palladium system of noble metal, a nickel system of non-noble metal and a copper system of non-noble metal; further preferably, the inlet temperature of the hydrogenation reactor is 30-50 ℃, the reaction pressure is 1.5-2.5 MPaG, the reaction temperature is 10-30 ℃, the molar ratio of the hydrogen to the alkyne is 1-3, the circulation ratio is 15 -1 . Preferably, the alkane component is a component such as an n-butane and/or isobutane component.
According to the present invention, preferably, in step S4, the operating conditions of the stabilizer tower include: the reaction pressure of the stabilizing tower is 0.5-1.0 MPaG, the operation temperature of the top of the stabilizing tower is 35-80 ℃, and the number of tower plates of the stabilizing tower is 20-80.
According to the invention, preferably, the bottom liquid phase separated from the hydro-separation tank sent to the middle part of the stabilizer is treated by the stabilizer to obtain a stabilizer top material and a stabilizer bottom material. Treating the material at the top of the stabilizer tower by the stabilizer condenser to obtain a gas-phase product at the top of the stabilizer tower and a liquid-phase material at the top of the stabilizer tower; and the gas-phase product at the top of the stabilizer tower and the uncondensed purge gas are sent out of the device together, and the liquid-phase material at the top of the stabilizer tower flows back to the stabilizer tower for rectification circulation. And the material at the bottom of the stabilizer tower is treated by the stabilizer reboiler, one part of the material flows back to the bottom of the stabilizer tower for rectification circulation, and the other part of the material is taken as the product at the bottom of the stabilizer tower and is sent out of the device.
According to the invention, preferably, the hydrogenated product is withdrawn from the upper side of the rectifying section of the stabilizer column.
According to the present invention, preferably, the stabilizer top gas phase product comprises at least one or more mixtures of hydrogen, methane and carbon four; the bottom product of the stabilizer tower is a heavy component; the hydrogenation product is a butene-1-rich product, a butadiene-rich product or an alkane-rich product; preferably, the stabilizer column bottoms is a mixture rich in C5 and C8.
The present invention is specifically described below by way of examples.
Example 1
The embodiment provides a four carbon alkyne hydrogenation apparatus, as shown in fig. 2, the apparatus includes a pressure boosting device 1, a liquefaction condensing unit 2, a water washing tower 3, a dehydration unit 4, a hydrogenation reactor 5, a hydrogenation separation tank 6, a hydrogenation aftercooler 7, a circulation cooler 9, and a stabilizer 10;
an alkyne-rich carbon four-feedstock feed line 14 containing solvent N, N-Dimethylformamide (DMF) in the gas phase is connected to the inlet of the pressurising means 1;
the liquefaction and condensation unit 2 comprises a primary condenser 2-1 and a secondary condenser 2-2 which are connected in sequence; the outlet of the supercharging equipment 1 is connected with the inlet of the primary condenser 2-1; the outlet of the secondary condenser 2-2 is connected with the inlet of the water washing tower 3; an alkyne separation tank 22 and a water washing pump 23 are sequentially arranged between the outlet of the secondary condenser 2-2 and the inlet of the water washing tower 3; in the present embodiment, the supercharging apparatus 1 is a blower.
The dehydration unit 4 comprises a decanter 4-1, a settler 4-2 and a coalescer 4-3 which are connected in sequence; the top outlet of the water washing tower 3 is connected with the inlet of a decanter 4-1 of the dehydration unit 4; the organic phase outlet of the coalescer 4-3 of the dehydration unit 4 is connected with a four alkyne-rich carbon feeding line 24 through a reaction feeding pump 13; the dehydration unit 4 is further provided with a dehydration unit aqueous phase outlet line 25, the dehydration unit aqueous phase outlet line 25 comprises a decanter aqueous phase outlet line 26, a settler aqueous phase outlet line 27 and a coalescer aqueous phase outlet line 28;
the top of the water washing tower 3 is also connected with a washing water feeding pipeline 16 of the water washing tower, and the bottom of the water washing tower is connected with a water phase outlet pipeline 29 at the bottom of the water washing tower; the decanter aqueous phase outlet line 26, the settler aqueous phase outlet line 27, the coalescer aqueous phase outlet line 28 and the water scrubber bottom aqueous phase outlet line 29 are merged together to the wastewater discharge line 17;
the four alkyne-rich feed line 24, the outlet connection line 30 of the recycle cooler and the hydrogen feed line 18 are all connected to the inlet line 34 of the hydrogenation reactor;
the hydrogenation reactor 5 is an up-flow reactor; the outlet of the hydrogenation reactor 5 is connected with the first inlet 31 of the hydrogenation separation tank;
an outlet at the top of the hydrogenation separation tank 6 is connected with an inlet of the hydrogenation aftercooler 7; the liquid phase outlet of the hydrogenation aftercooler 7 is connected with the second inlet 32 of the hydrogenation separation tank, and the gas phase outlet of the hydrogenation aftercooler 7 is connected with the purge gas output pipeline 19; an outlet pipeline at the bottom of the hydrogenation separation tank 6 is divided into two paths through a circulating pump 8, one path is connected with an inlet of the circulating cooler 9 through a four hydrogenation cycle carbon pipeline 33, and an outlet connecting pipeline 30 of the circulating cooler is connected with an inlet pipeline 34 of the hydrogenation reactor; the other is connected to the central inlet 35 of the stabilizer column.
The top of the stabilizer 10 is provided with a stabilizer condenser 11 and a stabilizer top gas-phase product discharge pipeline 36, and the stabilizer top gas-phase product discharge pipeline 36 is connected with the purge gas output pipeline 19 and is used for discharging the stabilizer top gas-phase product and the uncondensed purge gas together out of the device; the bottom of the stabilizer is provided with a stabilizer reboiler 12 and a stabilizer bottom product discharge pipeline 21, and the upper part of the rectifying section of the stabilizer is provided with a hydrogenated product discharge pipeline 20.
Example 2
The present embodiment provides a method for hydrogenating a carbon tetraalkyne, where the method employs the carbon tetraalkyne hydrogenation apparatus described in embodiment 1, and includes the following steps:
s1: feeding a gas-phase alkyne-rich carbon four raw material containing N, N-dimethylformamide as a solvent into the alkyne-carbon four hydrogenation device through a gas-phase impurity-containing alkyne-carbon four raw material feeding pipeline 14, sequentially passing through the supercharging equipment 1, the liquefaction condensation unit 2, the washing tower 3 and the dehydration unit 4, and sequentially performing supercharging, condensation liquefaction, washing impurity removal (removing water-soluble impurities such as solvent) and dehydration treatment to obtain an organic phase of the dehydration unit, namely impurity-removed dehydrated alkyne-carbon four, a water phase of the washing tower and a water phase of the dehydration unit; a part of heavy component removal treatment performed by the alkyne knockout drum 22 is also included between the condensation treatment and the water washing impurity removal treatment;
the feeding temperature of the gas-phase impurity-containing alkyne-rich carbon four raw material is 45 ℃, and the feeding pressure is 10kPaG; the pressure of the gas-phase impurity-containing alkyne-rich C-C four raw material subjected to pressurization treatment is 180kPaG;
the condensing and liquefying treatment scheme is a treatment scheme adopting a primary condenser 2-1 and a secondary condenser 2-2; the condensing medium 15 of the first-stage condenser 2-1 is cooling water 15-1, and the condensing medium 15 of the second-stage condenser 2-2 is propylene 15-2;
the operating conditions of the water scrubber 3 include: the feeding temperature of washing water of the washing tower is 30 ℃, and the number of tower plates of a washing tower 3 is 40;
the solvent content in the liquid-phase carbon four after being washed by the water washing tower 3 is 10ppm; the free water content in the carbon four after dehydration by the dehydration unit 4 was 100ppm. The water phase of the washing tower and the water phase of the dehydration unit are respectively converged to the wastewater discharge pipeline 17 through the water phase outlet pipeline 29 at the bottom of the washing tower and the water phase outlet pipeline 25 of the dehydration unit, and then sent out of the device.
S2: sending the impurity-removed and dehydrated alkyne-rich carbon IV, hydrogen and hydrogenation cycle carbon IV to the hydrogenation reactor, carrying out selective hydrogenation with a non-noble metal nickel catalyst to prepare butadiene, converting vinyl acetylene in the unsaturated component into butadiene and a small amount of butene-1, and converting butyne into butene-1 to obtain a butadiene-rich component;
in the selective hydrogenation butadiene production reaction, the hydrogenation reactor 5 is an ascending hydrogenation reactor, the inlet temperature of the hydrogenation reactor 5 is 30 ℃, the reaction pressure is 0.6MPaG, the reaction temperature is 15 ℃, the circulation ratio is 20 -1 ；
S3: sending the discharge of the hydrogenation reactor 5 to the hydro-separation tank 6 through a first inlet 31 of the hydro-separation tank; sending the light components separated from the hydrogenation separation tank 6 into the hydrogenation aftercooler 7, sending the liquid phase obtained by cooling the hydrogenation aftercooler 7 back to the hydrogenation separation tank 6 through a second inlet 32 of the hydrogenation separation tank, and sending the uncondensed purge gas obtained by cooling the hydrogenation aftercooler 7 out of the device through a purge gas output pipeline 19;
s4: and cooling a part of the bottom liquid phase separated by the hydrogenation separation tank 6 by the circulating cooler 9, sending the cooled part of the bottom liquid phase to the hydrogenation reactor 5 as the hydrogenation circulating carbon four, sending the other part of the bottom liquid phase to the middle part of the stabilizing tower 10, and treating the cooled part of the bottom liquid phase by the stabilizing tower 10 to obtain a stabilizing tower top material and a stabilizing tower bottom material.
The operating conditions of the stabilizer column 10 include: the reaction pressure of the stabilizer is 0.8MPaG, the operation temperature at the top of the stabilizer is 60 ℃, and the number of tower plates of the stabilizer is 50;
the material at the top of the stabilizer tower is treated by the stabilizer condenser 11 to obtain a gas-phase product at the top of the stabilizer tower and a liquid-phase material at the top of the stabilizer tower; the gas-phase product at the top of the stabilizer tower and the uncondensed purge gas are sent out of the device together, and the liquid-phase material at the top of the stabilizer tower flows back to the stabilizer tower 10 for rectification circulation;
the material at the top of the stabilizer tower is treated by the stabilizer reboiler 12, one part of the material flows back to the bottom of the stabilizer tower 10 for rectification circulation, and the other part of the material is taken as the product at the bottom of the stabilizer tower and sent out of the device;
the hydrogenated product is withdrawn through the upper side line (hydrogenated product discharge line 20) of the rectifying section of the stabilizer.
The stabilizer column overhead gas phase product comprises hydrogen and methane; the bottom product of the stabilizer tower is a mixture rich in C5 and C8; the hydrogenated product is a butadiene-rich product, and can be returned to a butadiene extraction device to increase the yield of butadiene.
TABLE 1
| Logistics | Alkyne-rich carbon four feedstock | Hydrogenated product | Purge gas | Heavy fraction |
| Phase state | Gaseous state | Liquid state | Gaseous state | Liquid state |
| Temperature, C | 45 | 40 | 20 | 70 |
| Pressure, MPaG | 0.005 | 1.2 | 0.7 | 0.8 |
| Mass fraction% | ||||
| Hydrogen gas | 0 | 0 | 7.2 | 0 |
| Methane | 0 | 0 | 0.24 | 0 |
| N-butane | 15.622 | 15.98 | 11.57 | 6.07 |
| Isobutane | 0.603 | 0.61 | 0.89 | 0.03 |
| 1-butene | 18.211 | 27.17 | 29.03 | 3.2 |
| Isobutene | 28.549 | 29.18 | 31.69 | 3.18 |
| 2-butene | 9.766 | 9.92 | 6.19 | 6.44 |
| 1, 3-butadiene | 4.291 | 10.18 | 9.86 | 1.53 |
| 1, 2-butadiene | 3.340 | 3.02 | 1.11 | 12.24 |
| Butyne | 2.230 | 0.67 | 0.33 | 0.88 |
| Vinyl acetylene | 16.083 | 3.24 | 1.82 | 3.84 |
| Heavy fraction | 0.505 | 0 | 0 | 62.57 |
| Water (W) | 0.3 | 0.04 | 0.07 | 0.02 |
| N, N-dimethylformamide | 0.5 | 0 | 0 | 0 |
| Is totaled | 100.00 | 100.00 | 100 | 100 |
As shown in Table 1, the acetylene-rich carbon four-feed containing solvent N, N-dimethylformamide in vapor phase from the butadiene extraction unit was treated by the method of this example to obtain the hydrogenated product, the uncondensed purge gas and the composition of the heavy components and the operating conditions. Through economic measurement and calculation, by means of the device and the method, 20 ten thousand tons of butadiene per year are extracted to obtain the byproduct carbon tetraalkyne 2t/h, butadiene is prepared through selective hydrogenation, the device investment is 2000-3000 ten thousand yuan, the annual benefit is 2500-3000 ten thousand yuan, the cost can be recovered more than one year, and the benefit is remarkable.
Example 3
The present embodiment provides a method for hydrogenating a carbon tetraalkyne, where the method employs the carbon tetraalkyne hydrogenation apparatus described in embodiment 1, and includes the following steps:
s1: feeding a gas-phase alkyne-rich carbon four raw material containing N, N-dimethylformamide as a solvent into the alkyne-four-carbon hydrogenation device through a gas-phase alkyne-rich carbon four raw material feeding pipeline 14, sequentially passing through the supercharging equipment 1, the liquefaction condensation unit 2, the water washing tower 3 and the dehydration unit 4, and sequentially performing supercharging, condensation liquefaction, dehydration impurity removal (removing water-soluble impurities such as solvents) and dehydration treatment to obtain an organic phase of the dehydration unit, namely impurity-removed dehydrated alkyne-rich carbon four, a water phase of the water washing tower and a water phase of the dehydration unit; a partial heavy component removal treatment by the alkyne knockout drum 22 is further included between the condensation treatment and the impurity removal treatment;
the feeding temperature of the gas-phase impurity-containing alkyne-rich carbon four raw material is 45 ℃, and the feeding pressure is 10kPaG; the pressure of the gas-phase impurity-containing alkyne-rich carbon four raw material subjected to pressurization treatment is 180kPaG;
the condensing and liquefying treatment scheme is a treatment scheme adopting a primary condenser 2-1 and a secondary condenser 2-2; the condensing medium 15 of the first-stage condenser 2-1 is cooling water 15-1, and the condensing medium 15 of the second-stage condenser 2-2 is propylene 15-2;
the operating conditions of the water washing column 3 include: the feeding temperature of washing water of the washing tower is 30 ℃, and the number of tower plates of a washing tower 3 is 40;
the solvent content in the liquid-phase carbon four after being washed by the water washing tower 3 is 10ppm; the free water content in the carbon four after dehydration by the dehydration unit 4 was 100ppm. The water phase of the washing tower and the water phase of the dehydration unit are respectively converged to the wastewater discharge pipeline 17 through the water phase outlet pipeline 29 at the bottom of the washing tower and the water phase outlet pipeline 25 of the dehydration unit, and then sent out of the device.
S2: the impurity-removed and dehydrated alkyne-enriched C4, hydrogen and hydrogenation cycle C4 are sent to the hydrogenation reactor together, and are subjected to selective hydrogenation with a non-noble metal nickel catalyst to prepare butene-1, and vinyl acetylene, butadiene and butyne in the unsaturated component are converted into butene-1 and a small amount of butene-2, so that a butene-1-enriched component is obtained;
in the reaction for preparing butene-1 by selective hydrogenation, the hydrogenation reactor 5 is an ascending hydrogenation reactor, the inlet temperature of the hydrogenation reactor 5 is 45 ℃, the reaction pressure is 2.5MPaG, the reaction temperature is 30 ℃, the circulation ratio is 15 -1 ；
S3: the discharge of the hydrogenation reactor 5 is sent to the hydrogenation separation tank 6 through a first inlet 31 of the hydrogenation separation tank; sending the light components separated from the hydrogenation separation tank 6 into the hydrogenation aftercooler 7, sending the liquid phase obtained by cooling the hydrogenation aftercooler 7 back to the hydrogenation separation tank 6 through a second inlet 32 of the hydrogenation separation tank, and sending the uncondensed purge gas obtained by cooling the hydrogenation aftercooler 7 out of the device through a purge gas output pipeline 19;
s4: and (3) cooling a part of the bottom liquid phase separated by the hydrogenation separation tank 6 by the circulating cooler 9, sending the cooled part of the bottom liquid phase to the hydrogenation reactor 5 as the hydrogenation circulating carbon four, sending the other part of the bottom liquid phase to the middle part of the stabilizing tower 10, and treating the part of the bottom liquid phase by the stabilizing tower 10 to obtain a stabilizing tower top material and a stabilizing tower bottom material.
The operating conditions of the stabilizer column 10 include: the reaction pressure of the stabilizer is 0.8MPaG, the operation temperature of the top of the stabilizer is 60 ℃, and the number of tower plates of the stabilizer is 50;
the material at the top of the stabilizer tower is processed by the stabilizer tower condenser 11 to obtain a gas-phase product at the top of the stabilizer tower and a liquid-phase material at the top of the stabilizer tower; the gas-phase product at the top of the stabilizer tower and the uncondensed purge gas are sent out of the device together, and the liquid-phase material at the top of the stabilizer tower flows back to the stabilizer tower 10 for rectification circulation;
the material at the top of the stabilizer tower is treated by the stabilizer reboiler 12, one part of the material flows back to the bottom of the stabilizer tower 10 for rectification circulation, and the other part of the material is taken as the product at the bottom of the stabilizer tower and sent out of the device;
the hydrogenated product is withdrawn through the upper side line (hydrogenated product discharge line 20) of the rectifying section of the stabilizer.
The gas phase product at the top of the stabilizer column comprises hydrogen and methane; the bottom product of the stabilizer tower is a mixture rich in C5 and C8; the hydrogenation product is a butene-1-rich product and can be sent to a downstream chemical device for further treatment.
TABLE 2
As shown in Table 2, the acetylene-rich carbon four-feed containing solvent N, N-dimethylformamide in vapor phase from the butadiene extraction unit was treated by the method of this example to obtain the hydrogenated product, the uncondensed purge gas and the composition of the heavy components and the operating conditions. Through economic measurement and calculation, by using the device and the method of the embodiment, 20 ten thousand tons per year of butadiene extraction byproduct carbon tetraalkyne 2t/h is prepared by selective hydrogenation, the device investment is 2000-3000 ten thousand yuan, the annual benefit is about 1500 ten thousand yuan, the cost can be recovered after more than two years, and the benefit is remarkable.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments.
Claims (10)
1. The carbon-tetra-alkyne hydrogenation device is characterized by comprising a pressurizing device, a liquefaction condensing unit, a dehydration unit, a hydrogenation reactor, a hydrogenation separation tank, a hydrogenation aftercooler, a circulating cooler, a stabilizing tower and an optional water washing tower;
a gas-phase impurity-containing alkyne-carbon-rich four-raw material feeding pipeline is connected with the inlet of the pressurizing device;
the outlet of the pressure boosting device is connected with the inlet of the liquefaction condensation unit;
the outlet of the liquefaction condensation unit is connected with the inlet of the dehydration unit; optionally, the outlet of the liquefaction condensation unit is connected with the inlet of the water washing tower, and the top outlet of the water washing tower is connected with the inlet of the dehydration unit;
the outlet of the organic phase of the dehydration unit is connected with a four-feed pipeline for removing impurities, dehydrating and enriching alkyne carbon;
the four alkyne-enriched carbon feeding pipeline for impurity removal and dehydration, the outlet connecting pipeline of the circulating cooler and the hydrogen feeding pipeline are connected to the inlet pipeline of the hydrogenation reactor;
the outlet of the hydrogenation reactor is connected with the first inlet of the hydrogenation separation tank;
the outlet at the top of the hydrogenation separation tank is connected with the inlet of the hydrogenation aftercooler; the liquid phase outlet of the hydrogenation aftercooler is connected with the second inlet of the hydrogenation separation tank, and the gas phase outlet of the hydrogenation aftercooler is connected with a purge gas output pipeline; an outlet pipeline at the bottom of the hydrogenation separation tank is respectively connected with a four hydrogenation cycle carbon pipeline and a middle inlet of the stabilizing tower; the four hydrogenation circulating carbon pipelines are connected with the inlet of the circulating cooler.
2. The carbon-tetraalkyne hydrogenation apparatus according to claim 1, wherein,
the supercharging equipment is a blower or a compressor;
the liquefaction and condensation unit comprises a primary condenser and/or a secondary condenser;
the top of the water washing tower is connected with a washing water feeding pipeline of the water washing tower, and the bottom of the water washing tower is connected with a water phase outlet pipeline at the bottom of the water washing tower;
an alkyne separation tank and a water washing pump are sequentially arranged between the outlet of the liquefaction condensation unit and the inlet of the water washing tower;
the organic phase outlet of the dehydration unit is connected with a four-feeding pipeline for impurity removal and dehydration of alkyne-rich carbon through a reaction feeding pump; the dewatering unit comprises at least one of a decanter, a settler, and a coalescer; the dehydration unit is also provided with a dehydration unit aqueous phase outlet pipeline which comprises at least one of a decanter aqueous phase outlet pipeline, a settler aqueous phase outlet pipeline and a coalescer aqueous phase outlet pipeline;
the hydrogenation reactor is a descending trickle bed reactor or an ascending reactor;
an outlet pipeline at the bottom of the hydrogenation separation tank is respectively connected with a four hydrogenation cycle carbon pipeline and a middle inlet of the stabilizing tower through a circulating pump;
the top of stabilizer is equipped with stabilizer condenser and stabilizer top gas phase product discharge line, the bottom of stabilizer is equipped with stabilizer reboiler and stabilizer bottom product discharge line, the rectifying section upper portion of stabilizer is equipped with hydrogenation product discharge line.
3. A method for hydrogenating carbon-four alkyne, which is characterized by using the apparatus for hydrogenating carbon-four alkyne of claim 1 or 2, comprising the steps of:
s1: sequentially passing the gas-phase impurity-containing alkyne-rich carbon four raw material through the supercharging equipment, the liquefaction condensation unit and the dehydration unit, and sequentially performing supercharging, condensation liquefaction and dehydration treatment to obtain impurity-removed dehydrated alkyne-rich carbon four and a water phase of the dehydration unit; optionally, washing impurity removal treatment is further included between the condensation treatment and the dehydration treatment to obtain a water phase of the washing tower;
s2: sending the impurity-removed and dehydrated alkyne-enriched C4, hydrogen and hydrogenation cycle C4 to the hydrogenation reactor together for hydrogenation reaction;
s3: sending the discharge of the hydrogenation reactor to the hydrogenation separation tank through a first inlet of the hydrogenation separation tank; sending the light components separated from the hydrogenation separation tank into the hydrogenation aftercooler, sending the liquid phase obtained by cooling through the hydrogenation aftercooler back into the hydrogenation separation tank through a second inlet of the hydrogenation separation tank, and sending the uncondensed purge gas obtained by cooling through the hydrogenation aftercooler out of the device;
s4: and cooling a part of the bottom liquid phase separated by the hydrogenation separation tank by the circulating cooler, sending the cooled part of the bottom liquid phase to the hydrogenation reactor as the fourth hydrogenation cycle carbon, sending the other part of the bottom liquid phase to the middle part of the stabilizing tower, and treating the cooled part of the bottom liquid phase by the stabilizing tower to obtain a gas phase product at the top of the stabilizing tower, a bottom product of the stabilizing tower and a hydrogenation product.
4. The carbon-tetraalkyne hydrogenation method according to claim 3, wherein, in step S1,
the feeding temperature of the gas-phase impurity-containing alkyne-rich carbon four raw material is 20-80 ℃, and the feeding pressure is 2-20 kPaG;
the pressure of the gas-phase impurity-containing alkyne-carbon-rich four-raw material subjected to pressurization treatment is 150-300 kPaG;
the condensing and liquefying treatment scheme is a treatment scheme adopting a primary condenser or a treatment scheme adopting a primary condenser and a secondary condenser;
the condensing medium of the first-stage condenser adopting the treatment scheme of the first-stage condenser is chilled water or propylene; the condensation medium of the first-stage condenser adopting the treatment scheme of the first-stage condenser and the second-stage condenser is cooling water or a process material, and the condensation medium of the second-stage condenser is chilled water or propylene;
the operating conditions of the water washing tower comprise: the feeding temperature of the washing water of the washing tower is 20-50 ℃, and the number of tower plates of the washing tower is 20-80.
5. The carbon-tetraalkyne hydrogenation method according to claim 3, wherein, in step S1,
a part of heavy component removal treatment is carried out through the alkyne knockout drum between the condensation treatment and the water washing impurity removal treatment;
and the water phase of the water washing tower and the water phase of the dehydration unit are respectively sent out of the device through the water phase outlet pipeline at the bottom of the water washing tower and the water phase outlet pipeline of the dehydration unit.
6. A process for the hydrogenation of carbonine according to claim 3, wherein, in step S1, the gaseous impurity-enriched alkyne-carbon-tetrafeedstock comprises a gaseous impurity-enriched alkyne-carbon-tetrafeedstock from a butadiene extraction plant, wherein the impurities comprise a water-soluble solvent and a water-soluble polar organic substance, and the water-soluble solvent is preferably at least one or more of acetonitrile, N-dimethylformamide, N-methylpyrrolidone and N-formylmorpholine, or an aqueous mixture.
7. The carbon-tetraalkyne hydrogenation method according to claim 3, wherein, in step S2, the hydrogenation reaction is one or more of a selective hydrogenation to butene-1 reaction, a selective hydrogenation to butadiene reaction or a full hydrogenation to alkanes reaction on unsaturated components in the hydrogenation reactor;
the unsaturated component is at least one of vinyl acetylene, butadiene, butyne, butene-1, butene-2, and isobutylene.
8. The carbon-four alkyne hydrogenation process of claim 7, wherein the selective hydrogenation to butene-1 reaction is a reaction that converts the unsaturated component to a butene-1-rich component; in the reaction for preparing the butene-1 by the selective hydrogenation, the inlet temperature of the hydrogenation reactor is 20-70 ℃, the reaction pressure is 0.5-3 MPaG, the reaction temperature is 5-50 ℃, the molar ratio of the hydrogen to the alkyne is 0.5-5, the circulation ratio is 10 -1 The catalyst is at least one of a platinum system of noble metal, a palladium system of noble metal, a nickel system of non-noble metal and a copper system of non-noble metal;
the selective hydrogenation butadiene preparation reaction is a reaction for converting the unsaturated component into a butadiene-rich component; in the reaction for preparing butadiene by selective hydrogenation, the inlet temperature of the hydrogenation reactor is 15-70 ℃, the reaction pressure is 0.4-3 MPaG, the reaction temperature is 5-50 ℃, the molar ratio of hydrogen to acetylene is 1-3, the circulation ratio is 5-40 -1 The catalyst is at least one of a platinum system of noble metal, a palladium system of noble metal, a nickel system of non-noble metal and a copper system of non-noble metal;
the full hydrogenation reaction is a reaction for converting the unsaturated component into a saturated alkane component; in the full hydrogenation reaction, the inlet temperature of the hydrogenation reactor is 30-70 ℃, the reaction pressure is 0.5-3 MPaG, the reaction temperature is 5-60 ℃, the molar ratio of hydrogen to acetylene is 1-5, the circulation ratio is 5-40 -1 The catalyst is at least one of a platinum group of noble metal, a palladium group of noble metal, a nickel group of non-noble metal and a copper group of non-noble metal.
9. The carbon-four alkyne hydrogenation process of claim 3, wherein in step S4, the operating conditions of the stabilizer column comprise: the reaction pressure of the stabilizer is 0.5-1.0 MPaG, the operation temperature of the top of the stabilizer is 35-80 ℃, and the number of tower plates of the stabilizer is 20-80;
treating the bottom liquid phase separated by the hydrogenation separation tank sent to the middle part of the stabilizing tower by the stabilizing tower to obtain a material at the top of the stabilizing tower and a material at the bottom of the stabilizing tower;
treating the material at the top of the stabilizer tower by the stabilizer condenser to obtain a gas-phase product at the top of the stabilizer tower and a liquid-phase material at the top of the stabilizer tower; the gas-phase product at the top of the stabilizer tower and the uncondensed purge gas are sent out of the device together, and the liquid-phase material at the top of the stabilizer tower flows back to the stabilizer tower for rectification circulation;
the material at the bottom of the stabilizer tower is treated by the reboiler of the stabilizer tower, one part of the material flows back to the bottom of the stabilizer tower for rectification circulation, and the other part of the material is taken as the product at the bottom of the stabilizer tower and sent out of the device;
and the hydrogenated product is extracted from the upper side line of the rectifying section of the stabilizing tower.
10. A carbon tetraalkyne hydrogenation process according to claim 9, wherein the stabilizer column overhead gas phase product comprises at least one or more mixtures of hydrogen, methane, and carbon tetraalkyne; the bottom product of the stabilizer tower is a heavy component; the hydrogenation product is a butene-1-rich product, a butadiene-rich product or an alkane-rich product;
preferably, the stabilizer column bottoms is a mixture rich in C5 and C8.
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