A method and device for hydrogenating carbon tetraacetylene

Abstract

The present invention belongs to the field of alkyne-rich C4 recovery and discloses a C4 alkyne hydrogenation method and apparatus. The apparatus comprises: a pressurizing device, a condenser, a water scrubber, a dehydration device, a hydrogenation reactor, a hydrogenation separation tank, a hydrogenation aftercooler, a circulating cooler, a stabilization tower, a stabilization tower condenser, and a stabilization tower reboiler. Through pressurization, liquefaction, water scrubbing and impurity removal, dehydration, hydrogenation, and separation processes, three alkyne-rich C4 hydrogenation reaction processes are implemented. This process can process all tail gases containing alkynes and impurities from a butadiene plant, solving the C4 alkyne processing challenge and increasing the economic benefits of the apparatus.

Description

Technical Field

[0001] The present invention belongs to the field of alkyne-rich C4 recovery, and more specifically, relates to a C4 alkyne hydrogenation method and device. Background Art

[0002] In the past, due to the lack of a suitable recovery method, the acetylene-rich C4 tail gas from the butadiene extraction unit usually needed to be diluted with a large amount of C4 residual liquid and then used as fuel gas or directly discharged into the flare, resulting in great waste. At present, the acetylene tail gas hydrogenation process has been successfully developed at home and abroad. It can selectively hydrogenate the acetylene-rich C4 tail gas into butene-1 or butadiene to achieve the purpose of turning waste into treasure, thereby reducing acetylene emissions and preventing environmental pollution. The liquid phase hydrogenation technology route has the advantages of a small hydrogen-to-hydrocarbon ratio, low reaction temperature, low energy consumption, and good economic benefits and is gradually being widely used. However, the C4 alkyne tail gas from the butadiene unit, especially the DMF method, is sent out of the boundary area in the form of a low-pressure gas phase. Therefore, the docking process with the liquid phase hydrogenation requires a pressurized liquefaction process, and the catalyst in the liquid phase hydrogenation reactor has extremely stringent requirements on water content and solvent content, so a water washing and dehydration process is required. Liquid phase hydrogenation is divided into full hydrogenation process, selective hydrogenation process for producing butene-1 and selective hydrogenation process for producing butadiene. The prior art does not mention using one-stage liquid phase hydrogenation to realize the above three processes.

[0003] CN102294203A discloses a two-stage hydrogenation apparatus and process for C4 in catalytic pyrolysis to produce ethylene. By employing two-stage selective hydrogenation, this process avoids the problems of reactor coking, reduced catalyst life, and reduced operating cycle associated with deep hydrogenation of 1,3-butadiene. Mixed C4 can be directly hydrogenated, improving raw material utilization. However, the process is relatively lengthy, and the two-stage hydrogenation requires a circulating hydrogen compressor, among other factors, resulting in high investment costs.

[0004] CN105566032 discloses a selective hydrogenation process for alkyne-rich C4, that is, the C4 alkynes produced as by-products of a butadiene extraction unit are first separated through a distillation tower, and the overhead material is extracted after being selectively hydrogenated to remove the alkynes. This invention mainly focuses on separation first, that is, the alkyne-rich C4 is first separated, and then hydrogenated after removing the heavy components. However, the heavy oil produced by the reaction may not be completely removed, and only the butadiene production is increased, without increasing the production of butene-1.

[0005] CN1590513A discloses a selective hydrogenation process for alkyne-rich hydrocarbon streams. This patent involves passing the alkyne-rich residual material from the butadiene extraction unit through a fixed-bed hydrogenation reactor equipped with a circulation system. The material undergoes selective hydrogenation in a liquid state, returning hydrogen and alkynes to remove the alkynes before returning the material to the butadiene extraction unit. This technology is characterized by a single route, specifically the hydrogenation of alkynes to butadiene, not butene-1. Secondly, the lack of a stabilization tower to remove light and heavy components can easily lead to excessive light and heavy component levels entering the butadiene unit, resulting in increased equipment and pipeline loads or blockages. Finally, the hydrogenation circulating material is not cooled, making the reaction inlet temperature uncontrollable and prone to temperature fluctuations. The lack of an aftercooler at the top of the vapor-liquid separator tank also easily leads to loss of C4 entrained by the light component. The process is therefore difficult to operate.

[0006] CN110963878A discloses a method for recovering C4 alkyne tail gas. This patent recovers C4 through liquefaction, impurity removal, and hydrogenation. This technology removes heavy components solely in a buffer tank, failing to meet the impurity requirements of the reactor catalyst. Furthermore, the use of a two-stage hydrogenation reactor requires high equipment investment. The product from the bottom of the light removal tower is susceptible to containing polymers produced during the reaction, making product purity uncertain. Furthermore, direct flaring from the tower top can carry over C4 components, resulting in material loss.

[0007] Therefore, in order to address the defects of the current liquid phase hydrogenation process and to solve the problem of utilizing the alkyne-rich C4 tail gas from the existing butadiene plant, it is urgent to propose a new C4 alkyne hydrogenation device and method. Summary of the Invention

[0008] The present invention addresses the shortcomings of the prior art by providing a method and apparatus for hydrogenating C4 alkynes. The present invention utilizes pressurization, liquefaction, water washing and impurity removal, dehydration, hydrogenation, and separation processes to achieve three alkyne-rich C4 hydrogenation reaction processes. This method can treat all tail gases containing alkynes and impurities from butadiene plants, resolving the challenges of C4 alkyne treatment and increasing the economic benefits of the plant.

[0009] To achieve the above-mentioned object, the present invention provides a C4 alkyne hydrogenation device, which includes a pressurizing device, a liquefaction and condensation unit, a dehydration unit, a hydrogenation reactor, a hydrogenation separation tank, a hydrogenation aftercooler, a circulating cooler and a stabilization tower, and optionally includes a water scrubber;

[0010] A gaseous impurity-containing alkyne-rich C4 raw material feed pipeline is connected to the inlet of the boosting device;

[0011] The outlet of the boosting device is connected to the inlet of the liquefaction condensation unit;

[0012] The outlet of the liquefaction and condensation unit is connected to the inlet of the dehydration unit; optionally, the outlet of the liquefaction and condensation unit is connected to the inlet of the water scrubber, and the top outlet of the water scrubber is connected to the inlet of the dehydration unit;

[0013] The organic phase outlet of the dehydration unit is connected to the de-doping, dehydration, and alkyne-enriched C4 feed pipeline;

[0014] The de-doped, dehydrated, and alkyne-enriched C4 feed pipeline, the outlet connecting pipeline of the circulating cooler, and the hydrogen feed pipeline are all connected to the inlet pipeline of the hydrogenation reactor;

[0015] The outlet of the hydrogenation reactor is connected to the first inlet of the hydrogenation separation tank;

[0016] The top outlet of the hydrogenation separation tank is connected to the inlet of the hydrogenation aftercooler; the liquid phase outlet of the hydrogenation aftercooler is connected to the second inlet of the hydrogenation separation tank, and the gas phase outlet of the hydrogenation aftercooler is connected to the purge gas output pipeline; the bottom outlet pipeline of the hydrogenation separation tank is respectively connected to the hydrogenation circulation C4 pipeline and the middle inlet of the stabilization tower; the hydrogenation circulation C4 pipeline is connected to the inlet of the circulation cooler.

[0017] Another aspect of the present invention provides a method for hydrogenating C4 alkynes, which uses the C4 alkyne hydrogenation device and comprises the following steps:

[0018] S1: The gaseous impurity-containing alkyne-rich C4 feedstock is sequentially passed through the boosting equipment, the liquefaction and condensation unit, and the dehydration unit, and is sequentially subjected to boosting, condensation, liquefaction, and dehydration treatment to obtain impurity-free and dehydrated alkyne-rich C4 and the aqueous phase of the dehydration unit; optionally, a water washing and impurity removal treatment is further included between the condensation treatment and the dehydration treatment to obtain the aqueous phase of the water washing tower;

[0019] S2: sending the de-doped, dehydrated, and alkyne-rich C4, hydrogen, and hydrogenation recycled C4 to the hydrogenation reactor for hydrogenation reaction;

[0020] S3: sending the discharge of the hydrogenation reactor to the hydrogenation separation tank through the first inlet of the hydrogenation separation tank; sending the light components separated in the hydrogenation separation tank to the hydrogenation aftercooler, sending the liquid phase obtained by cooling the hydrogenation aftercooler back to the hydrogenation separation tank through the second inlet of the hydrogenation separation tank, and sending the uncondensed purge gas obtained by cooling the hydrogenation aftercooler out of the device;

[0021] S4: A portion of the bottom liquid phase separated from the hydrogenation separation tank is cooled in the circulating cooler and sent to the hydrogenation reactor as the hydrogenation circulating C4, and the other portion is sent to the middle of the stabilization tower. After being processed in the stabilization tower, a gas phase product at the top of the stabilization tower, a bottom product of the stabilization tower and a hydrogenation product are obtained.

[0022] The technical solution of the present invention has the following beneficial effects:

[0023] 1) The present invention reduces the energy consumption of the liquefaction process of the liquefaction condensation unit through the acetylene-rich C4 tail gas pressurization process;

[0024] 2) The present invention removes water-soluble impurities such as solvents from the acetylene-rich C4 tail gas through a water washing process in a water washing tower, thereby avoiding the impact on the hydrogenation catalyst;

[0025] 3) The present invention reduces system energy consumption and improves the economic benefits of the device by rationally setting the heat exchange sequence and utilizing the energy of the primary condenser and the secondary condenser in a graded manner;

[0026] 4) The present invention minimizes the water content by arranging decanters, settlers, and coalescers in stages in the dehydration unit, thereby avoiding the impact on the catalyst of the hydrogenation reactor;

[0027] 5) The present invention can treat all acetylene-rich tail gases produced as by-products of butadiene plants through pressurization, liquefaction, water washing, dehydration, and hydrogenation processes. Furthermore, all gas-phase unsaturated C4s can be hydrogenated. If the raw materials do not contain water-soluble impurities, the water washing step can be eliminated.

[0028] 6) The present invention can realize three acetylene-rich C4 hydrogenation reaction processes, namely, full hydrogenation to butane process, selective hydrogenation to butene-1 process and selective hydrogenation to butadiene process, through a one-stage liquid phase hydrogenation device.

[0029] 7) The device of the present invention obtains the hydrogenation product through the side line of the distillation tower, which ensures the purity of the product and saves equipment investment.

[0030] Other features and advantages of the present invention will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0031] The above and other objects, features and advantages of the present invention will become more apparent through a more detailed description of exemplary embodiments of the present invention with reference to the accompanying drawings, wherein like reference numerals generally represent like components throughout the exemplary embodiments of the present invention.

[0032] Figure 1 A schematic diagram of a C4-alkyne hydrogenation device provided by the present invention is shown.

[0033] Figure 2 A schematic diagram of a C4-alkyne hydrogenation device provided in Example 1 of the present invention is shown.

[0034] Description of reference numerals:

[0035] 1. Booster; 2. Liquefaction and condensation unit; 2-1. Primary condenser; 2-2. Secondary condenser; 3. Water scrubber; 4. Dehydration unit; 4-1. Decanter; 4-2. Settler; 4-3. Coalescer; 5. Hydrogenation reactor; 6. Hydrogenation separation tank; 7. Hydrogenation aftercooler; 8. Circulation pump; 9. Circulation cooler; 10. Stabilizer; 11. Stabilizer condenser; 12. Stabilizer reboiler; 13. Reaction feed pump; 14. Gas-phase impurity-containing acetylene-rich C4 feed pipeline; 15. Condensing medium; 15-1. Cooling water; 15-2. Propylene; 16. Water scrubber wash water feed pipeline; 17. Wastewater discharge pipeline; 18. Hydrogen feed pipeline; 19. Purge gas Output pipeline; 20. Hydrogenation product discharge pipeline; 21. Stabilization tower bottom product discharge pipeline; 22. Alkyne separation tank; 23. Water washing pump; 24. De-impurity, dehydration, and alkyne-enriched C4 feed pipeline; 25. Dehydration unit aqueous phase outlet pipeline; 26. Decanter aqueous phase outlet pipeline; 27. Settler aqueous phase outlet pipeline; 28. Coalescer aqueous phase outlet pipeline; 29. ​​Water washing tower bottom aqueous phase outlet pipeline; 30. Circulating cooler outlet connecting pipeline; 31. First inlet of hydrogenation separation tank; 32. Second inlet of hydrogenation separation tank; 33. Hydrogenation circulation C4 pipeline; 34. Inlet pipeline of hydrogenation reactor; 35. Middle inlet of stabilization tower; 36. Gas phase product discharge pipeline at the top of stabilization tower. DETAILED DESCRIPTION

[0036] The preferred embodiments of the present invention will be described in more detail below. Although the preferred embodiments of the present invention are described below, it should be understood that the present invention can be implemented in various forms and should not be limited by the embodiments set forth herein. Instead, these embodiments are provided to make the present invention more thorough and complete and to fully convey the scope of the present invention to those skilled in the art.

[0037] In one aspect, the present invention provides a C4 alkyne hydrogenation device, which includes a pressurizing device, a liquefaction and condensation unit, a dehydration unit, a hydrogenation reactor, a hydrogenation separation tank, a hydrogenation aftercooler, a circulating cooler and a stabilization tower, and optionally includes a water scrubber;

[0038] A gaseous impurity-containing alkyne-rich C4 raw material feed pipeline is connected to the inlet of the boosting device;

[0039] The outlet of the boosting device is connected to the inlet of the liquefaction condensation unit;

[0040] The outlet of the liquefaction and condensation unit is connected to the inlet of the dehydration unit; optionally, the outlet of the liquefaction and condensation unit is connected to the inlet of the water scrubber, and the top outlet of the water scrubber is connected to the inlet of the dehydration unit;

[0041] The organic phase outlet of the dehydration unit is connected to the de-doping, dehydration, and alkyne-enriched C4 feed pipeline;

[0042] The de-doped, dehydrated, and alkyne-enriched C4 feed pipeline, the outlet connecting pipeline of the circulating cooler, and the hydrogen feed pipeline are all connected to the inlet pipeline of the hydrogenation reactor;

[0043] The outlet of the hydrogenation reactor is connected to the first inlet of the hydrogenation separation tank;

[0044] The top outlet of the hydrogenation separation tank is connected to the inlet of the hydrogenation aftercooler; the liquid phase outlet of the hydrogenation aftercooler is connected to the second inlet of the hydrogenation separation tank, and the gas phase outlet of the hydrogenation aftercooler is connected to the purge gas output pipeline; the bottom outlet pipeline of the hydrogenation separation tank is respectively connected to the hydrogenation circulation C4 pipeline and the middle inlet of the stabilization tower; the hydrogenation circulation C4 pipeline is connected to the inlet of the circulation cooler.

[0045] In the present invention, the bottom outlet pipeline of the hydrogenation separation tank is divided into two routes after passing through the circulation pump. One route is connected to the inlet of the circulation cooler through the hydrogenation circulation C4 pipeline, and the outlet connecting pipeline of the circulation cooler is connected to the inlet pipeline of the hydrogenation reactor; the other route is connected to the middle inlet of the stabilization tower.

[0046] According to the present invention, preferably, the boosting device is a blower or a compressor.

[0047] According to the present invention, preferably, the liquefaction condensation unit includes a primary condenser and / or a secondary condenser.

[0048] According to the present invention, preferably, the top of the water washing tower is connected to a water washing tower washing water feed pipeline, and the bottom is connected to a water washing tower bottom water phase outlet pipeline.

[0049] According to the present invention, preferably, an acetylene separation tank and a water washing pump are sequentially provided between the outlet of the liquefaction condensation unit and the inlet of the water washing tower.

[0050] According to the present invention, preferably, the organic phase outlet of the dehydration unit is connected to the de-doping, dehydration, and alkyne-enriched C4 feed pipeline via a reaction feed pump.

[0051] According to the present invention, preferably, the dehydration unit comprises at least one of a decanter, a settler and a coalescer.

[0052] According to the present invention, preferably, the dehydration unit is further provided with a dehydration unit water phase outlet pipeline, and the dehydration unit water phase outlet pipeline includes at least one of a decanter water phase outlet pipeline, a settler water phase outlet pipeline and a coalescer water phase outlet pipeline.

[0053] According to the present invention, preferably, the hydrogenation reactor is a descending trickle bed reactor or an ascending reactor.

[0054] According to the present invention, preferably, the bottom outlet pipeline of the hydrogenation separation tank is connected to the hydrogenation circulation C4 pipeline and the middle inlet of the stabilization tower respectively through a circulation pump.

[0055] According to the present invention, preferably, a stabilization tower condenser and a stabilization tower top gas phase product discharge pipeline are provided at the top of the stabilization tower, a stabilization tower reboiler and a stabilization tower bottom product discharge pipeline are provided at the bottom of the stabilization tower, and a hydrogenation product discharge pipeline is provided at the upper part of the distillation section of the stabilization tower.

[0056] Another aspect of the present invention provides a method for hydrogenating C4 alkynes, which uses the C4 alkyne hydrogenation device and comprises the following steps:

[0057] S1: The gaseous impurity-containing alkyne-rich C4 feedstock is sequentially passed through the boosting equipment, the liquefaction and condensation unit, and the dehydration unit, and is sequentially subjected to boosting, condensation, liquefaction, and dehydration treatment to obtain impurity-free and dehydrated alkyne-rich C4 and the aqueous phase of the dehydration unit; optionally, a water washing and impurity removal treatment is further included between the condensation treatment and the dehydration treatment to obtain the aqueous phase of the water washing tower;

[0058] S2: sending the de-doped, dehydrated, and alkyne-rich C4, hydrogen, and hydrogenation recycled C4 to the hydrogenation reactor for hydrogenation reaction;

[0059] S3: sending the discharge of the hydrogenation reactor to the hydrogenation separation tank through the first inlet of the hydrogenation separation tank; sending the light components separated in the hydrogenation separation tank to the hydrogenation aftercooler, sending the liquid phase obtained by cooling the hydrogenation aftercooler back to the hydrogenation separation tank through the second inlet of the hydrogenation separation tank, and sending the uncondensed purge gas obtained by cooling the hydrogenation aftercooler out of the device;

[0060] S4: A portion of the bottom liquid phase separated from the hydrogenation separation tank is cooled in the circulating cooler and sent to the hydrogenation reactor as the hydrogenation circulating C4, and the other portion is sent to the middle of the stabilization tower. After being processed in the stabilization tower, a gas phase product at the top of the stabilization tower, a bottom product of the stabilization tower and a hydrogenation product are obtained.

[0061] According to the present invention, preferably, in step S1, the feed temperature of the gas-phase impurity-containing alkyne-rich C4 raw material is 20-80° C., and the feed pressure is 2-20 kPaG.

[0062] According to the present invention, preferably, in step S1, the pressure of the gaseous impurity-containing acetylene-rich C4 raw material after the pressurization treatment is 150-300 kPaG.

[0063] According to the present invention, preferably, in step S1, the condensation and liquefaction treatment scheme is a treatment scheme using a primary condenser or a treatment scheme using a primary condenser and a secondary condenser. Through the condensation and liquefaction treatment, the temperature of the gaseous impurity-containing, acetylene-rich C4 feedstock is reduced to a temperature below the corresponding freezing point at the corresponding pressure of the boosting equipment.

[0064] According to the present invention, preferably, in step S1, the condensing medium of the primary condenser of the treatment scheme using a primary condenser is chilled water or propylene; the condensing medium of the primary condenser of the treatment scheme using a primary condenser and a secondary condenser is cooling water or process material, and the condensing medium of the secondary condenser is chilled water or propylene.

[0065] According to the present invention, preferably, in step S1, a process of removing some heavy components by using the alkyne separation tank is further included between the condensation process and the water washing and impurity removal process.

[0066] According to the present invention, preferably, in step S1, the operating conditions of the water scrubber include: the feed temperature of the washing water of the water scrubber is 20-50° C., and the number of plates of the water scrubber is 20-80.

[0067] According to the present invention, preferably, in step S1, 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.

[0068] According to the present invention, preferably, in step S1, the gaseous impure, alkyne-rich C4 feedstock includes a gaseous impure, alkyne-rich C4 feedstock from a butadiene extraction unit, and a gaseous unsaturated C4 feedstock produced by other units. The impurities include a water-soluble solvent and a water-soluble polar organic compound. The water-soluble solvent is preferably a mixture or aqueous mixture of at least one or more of acetonitrile, N,N-dimethylformamide, N-methylpyrrolidone, and N-formylmorpholine.

[0069] According to the present invention, preferably, in step S2, the hydrogenation reaction comprises three schemes:

[0070] Scheme 1 is to selectively hydrogenate the unsaturated components in the hydrogenation reactor to produce butene-1: most of the vinyl acetylene is converted into butene-1, and butyne-1 is converted into butene-1. A side reaction of producing butane will inevitably occur, that is, a process for preparing butene-1; according to the present invention, preferably, the selective hydrogenation to butene-1 reaction is a reaction of converting the unsaturated components into a butene-1-rich component. In the present invention, specifically, the vinyl acetylene, butadiene, and butyne in the unsaturated components are converted into butene-1, a small amount of butene-2 ​​and butane to obtain a butene-1-rich component.

[0071] Scheme 2 is to selectively hydrogenate the unsaturated components in the hydrogenation reactor to produce butadiene: most of the vinyl acetylene is converted into 1,3-butadiene, and butyne-1 is converted into butene-1. Side reactions of producing butane and butene-1 will inevitably occur, i.e., a process for preparing 1,3-butadiene. According to the present invention, preferably, the selective hydrogenation reaction to produce butadiene is a reaction to convert the unsaturated components into butadiene-rich components. In the present invention, specifically, the vinyl acetylene in the unsaturated components is converted into butadiene and a small amount of butene-1, and butyne is converted into butene-1 to obtain a butadiene-rich component.

[0072] Scheme 3: The unsaturated components in the hydrogenation reactor are subjected to a full hydrogenation reaction to produce alkanes: all or most of the unsaturated olefins, including vinyl acetylene, butyne-1, butene-1, butene-2 ​​(including cis and trans structures), isobutene, etc., are converted into corresponding alkanes, namely n-butane and isobutane, i.e., a process for producing alkanes. According to the present invention, preferably, the full hydrogenation reaction to produce alkanes is a reaction that converts the unsaturated components into saturated alkanes.

[0073] 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 components in the dehybridized dehydrated alkyne-enriched C4 and the hydrogenated recycled C4.

[0074] According to the present invention, preferably, in the selective hydrogenation reaction to produce butene-1, the inlet temperature of the hydrogenation reactor is 20-70°C, the reaction pressure is 0.5-3 MPaG, the reaction temperature rise is 5-50°C, the hydrogen-alkyne molar ratio is 0.5-5, the circulation ratio is 10:1-40:1, and the catalyst volume space velocity is 0.1-10h -1 The catalyst is at least one of a precious metal platinum system, a precious metal palladium system, a non-precious metal nickel system, and a non-precious metal copper system. Further preferably, the inlet temperature of the hydrogenation reactor is 30-60°C, the reaction pressure is 1.0-2.5 MPaG, the reaction temperature rise is 10-30°C, the hydrogen-alkyne molar ratio is 1-3, the circulation ratio is 10:1-30:1, and the catalyst volume space velocity is 0.3-5h -1 .

[0075] In the present invention, the hydrogen-to-alkyne molar ratio refers to the ratio of hydrogen to the "sum of the moles of alkynes and dienes"; the circulation ratio refers to the flow ratio of the circulating material (hydrogenated recycled C4) to the fresh feed (de-doped, dehydrated, and alkyne-enriched C4); and the catalyst volumetric space velocity refers to the ratio of the fresh feed (de-doped, dehydrated, and alkyne-enriched C4) to the catalyst volume.

[0076] According to the present invention, preferably, in the selective hydrogenation reaction to butadiene, the inlet temperature of the hydrogenation reactor is 15-70°C, the reaction pressure is 0.4-3 MPaG, the reaction temperature rise is 5-50°C, the hydrogen-alkyne molar ratio is 1-3, the circulation ratio is 5:1-40:1, and the catalyst volume space velocity is 0.1-10h -1 The catalyst is at least one of a precious metal platinum system, a precious metal palladium system, a non-precious metal nickel system, and a non-precious metal copper system; further preferably, the inlet temperature of the hydrogenation reactor is 20-50°C, the reaction pressure is 0.5-2 MPaG, the reaction temperature rise is 10-20°C, the circulation ratio is 15:1-25:1, and the catalyst volume space velocity is 0.3-2h -1 .

[0077] According to the present invention, preferably, in the full hydrogenation reaction, the inlet temperature of the hydrogenation reactor is 30-70°C, the reaction pressure is 0.5-3 MPaG, the reaction temperature rise is 5-60°C, the hydrogen-alkyne molar ratio is 1-5, the circulation ratio is 5:1-40:1, and the catalyst volume space velocity is 0.1-10h -1 The catalyst is at least one of a platinum-based precious metal, a palladium-based precious metal, a nickel-based non-precious metal, and a copper-based non-precious metal; further preferably, the inlet temperature of the hydrogenation reactor is 30-50°C, the reaction pressure is 1.5-2.5 MPaG, the reaction temperature rise is 10-30°C, the hydrogen-alkyne molar ratio is 1-3, the circulation ratio is 15:1-25:1, and the catalyst volume space velocity is 0.5-2h -1 Preferably, the alkane component is a component such as n-butane and / or isobutane.

[0078] According to the present invention, preferably, in step S4, the operating conditions of the stabilization tower include: a stabilization tower reaction pressure of 0.5-1.0 MPaG, a stabilization tower top operating temperature of 35-80° C., and a stabilization tower plate number of 20-80.

[0079] According to the present invention, preferably, the bottom liquid phase separated from the hydrogenation separation tank and sent to the middle of the stabilization tower is processed in the stabilization tower to obtain a stabilization tower overhead material and a stabilization tower bottom material. The stabilization tower overhead material is processed in the stabilization tower condenser to obtain the stabilization tower overhead gas phase product and the stabilization tower overhead liquid phase material; the stabilization tower overhead gas phase product and the uncondensed purge gas are sent out of the device together, and the stabilization tower overhead liquid phase material is refluxed to the stabilization tower for distillation cycle. The stabilization tower bottom material is processed in the stabilization tower reboiler, with a portion refluxed to the stabilization tower bottom for distillation cycle, and the remaining portion is sent out of the device as the stabilization tower bottom product.

[0080] According to the present invention, preferably, the hydrogenated product is taken out from the upper side of the distillation section of the stabilizer tower.

[0081] According to the present invention, preferably, the gaseous product at the top of the stabilization tower includes at least one or more mixtures of hydrogen, methane and C4; the bottom product of the stabilization tower is a heavy component; the hydrogenated product is a butene-1-rich product, a butadiene-rich product or an alkane-rich product; preferably, the bottom product of the stabilization tower is a mixture rich in C5 and C8.

[0082] The present invention is specifically described below through examples.

[0083] Example 1

[0084] This embodiment provides a C4 alkyne hydrogenation device, such as Figure 2 As shown, the device includes a booster 1, a liquefaction condensation unit 2, a water scrubber 3, a dehydration unit 4, a hydrogenation reactor 5, a hydrogenation separation tank 6, a hydrogenation aftercooler 7, a circulating cooler 9, and a stabilization tower 10;

[0085] A gas phase alkyne-rich C4 raw material feed line 14 containing solvent N,N-dimethylformamide (DMF) is connected to the inlet of the booster device 1;

[0086] The liquefaction and condensation unit 2 includes a primary condenser 2-1 and a secondary condenser 2-2 connected in sequence; the outlet of the boosting device 1 is connected to the inlet of the primary condenser 2-1; the outlet of the secondary condenser 2-2 is connected to the inlet of the water washing tower 3; an acetylene 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 this embodiment, the boosting device 1 is a blower.

[0087] The dehydration unit 4 includes a decanter 4-1, a settler 4-2 and a coalescer 4-3 connected in sequence; the top outlet of the water scrubber 3 is connected to the inlet of the decanter 4-1 of the dehydration unit 4; the organic phase outlet of the coalescer 4-3 of the dehydration unit 4 is connected to the de-impurity, dehydration and alkyne-enriched carbon four feed pipeline 24 through a reaction feed pump 13; the dehydration unit 4 is also provided with a dehydration unit water phase outlet pipeline 25, and the dehydration unit water phase outlet pipeline 25 includes a decanter water phase outlet pipeline 26, a settler water phase outlet pipeline 27 and a coalescer water phase outlet pipeline 28;

[0088] The top of the water washing tower 3 is also connected to a water washing tower washing water feed pipeline 16, and the bottom is connected to a water washing tower bottom water phase outlet pipeline 29; the decanter water phase outlet pipeline 26, the settler water phase outlet pipeline 27, the coalescer water phase outlet pipeline 28 and the water washing tower bottom water phase outlet pipeline 29 are all merged into the wastewater discharge pipeline 17;

[0089] The de-doped, dehydrated, and alkyne-enriched C4 feed pipeline 24, the outlet connecting pipeline 30 of the circulating cooler, and the hydrogen feed pipeline 18 are all connected to the inlet pipeline 34 of the hydrogenation reactor;

[0090] The hydrogenation reactor 5 is an upward reactor; the outlet of the hydrogenation reactor 5 is connected to the first inlet 31 of the hydrogenation separation tank;

[0091] The top outlet of the hydrogenation separation tank 6 is connected to the inlet of the hydrogenation aftercooler 7; the liquid phase outlet of the hydrogenation aftercooler 7 is connected to the second inlet 32 ​​of the hydrogenation separation tank, and the gas phase outlet of the hydrogenation aftercooler 7 is connected to the purge gas output pipeline 19; the bottom outlet pipeline of the hydrogenation separation tank 6 is divided into two paths after passing through the circulation pump 8, one path is connected to the inlet of the circulation cooler 9 through the hydrogenation circulation C4 pipeline 33, and the outlet connecting pipeline 30 of the circulation cooler is connected to the inlet pipeline 34 of the hydrogenation reactor; the other path is connected to the middle inlet 35 of the stabilization tower.

[0092] The top of the stabilization tower 10 is provided with a stabilization tower condenser 11 and a stabilization tower top gas-phase product discharge pipeline 36, and the stabilization tower top gas-phase product discharge pipeline 36 is connected to the purge gas output pipeline 19, and is used to discharge the stabilization tower top gas-phase product and uncondensed purge gas together from the device; the bottom of the stabilization tower is provided with a stabilization tower reboiler 12 and a stabilization tower bottom product discharge pipeline 21, and the upper part of the distillation section of the stabilization tower is provided with a hydrogenation product discharge pipeline 20.

[0093] Example 2

[0094] This embodiment provides a method for hydrogenating C4 alkynes, which uses the C4 alkyne hydrogenation apparatus described in Example 1 and includes the following steps:

[0095] S1: feeding the gas phase alkyne-rich C4 feedstock containing the solvent N,N-dimethylformamide into the C4 alkyne hydrogenation unit through the gas phase impurity-containing alkyne-rich C4 feedstock feed pipeline 14, and sequentially passing through the pressurizing device 1, the liquefaction and condensation unit 2, the water scrubber 3 and the dehydration unit 4, and sequentially undergoing pressurization, condensation and liquefaction, water washing and impurity removal (removal of water-soluble impurities such as the solvent) and dehydration treatment to obtain the dehydration unit organic phase, i.e., the impurity-removed and dehydrated alkyne-rich C4, the water phase of the water scrubber and the water phase of the dehydration unit; and between the condensation treatment and the water washing and impurity removal treatment, a treatment of removing some heavy components is also included in the alkyne separation tank 22;

[0096] The feed temperature of the gas phase impurity-containing alkyne-rich C4 raw material is 45° C., and the feed pressure is 10 kPaG; the pressure of the gas phase impurity-containing alkyne-rich C4 raw material after the pressurization treatment is 180 kPaG;

[0097] The condensation and liquefaction treatment scheme is a treatment scheme using a primary condenser 2-1 and a secondary condenser 2-2; the condensation medium 15 of the primary condenser 2-1 is cooling water 15-1, and the condensation medium 15 of the secondary condenser 2-2 is propylene 15-2;

[0098] The operating conditions of the water scrubber 3 include: the feed temperature of the water scrubber is 30°C, the number of plates of the water scrubber 3 is 40;

[0099] The solvent content of the liquid C4 after washing in the water scrubber 3 is 10 ppm; the free water content of the C4 after dehydration in the dehydration unit 4 is 100 ppm. The aqueous phase of the water scrubber and the aqueous phase of the dehydration unit are respectively combined through the aqueous phase outlet pipeline 29 at the bottom of the water scrubber and the aqueous phase outlet pipeline 25 of the dehydration unit to the wastewater discharge pipeline 17, and then discharged out of the device.

[0100] S2: sending the de-doped, dehydrated, acetylene-rich C4, hydrogen and hydrogenated recycled C4 together to the hydrogenation reactor for selective hydrogenation to butadiene over a non-precious metal nickel-based catalyst, 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;

[0101] In the selective hydrogenation reaction to butadiene, the hydrogenation reactor 5 is an upward hydrogenation reactor, the inlet temperature of the hydrogenation reactor 5 is 30°C, the reaction pressure is 0.6 MPaG, the reaction temperature rise is 15°C, the circulation ratio is 20:1, and the catalyst volume space velocity is 0.5h -1 ;

[0102] S3: The discharge of the hydrogenation reactor 5 is sent to the hydrogenation separation tank 6 through the first inlet 31 of the hydrogenation separation tank; the light components separated in the hydrogenation separation tank 6 are sent to the hydrogenation aftercooler 7, the liquid phase obtained by cooling the hydrogenation aftercooler 7 is returned to the hydrogenation separation tank 6 through the second inlet 32 ​​of the hydrogenation separation tank, and the uncondensed purge gas obtained by cooling the hydrogenation aftercooler 7 is sent out of the device through the purge gas output pipeline 19;

[0103] S4: A portion of the bottom liquid phase separated from the hydrogenation separation tank 6 is cooled in the circulating cooler 9 and sent to the hydrogenation reactor 5 as the hydrogenation circulating C4, and the other portion is sent to the middle of the stabilization tower 10. After being processed in the stabilization tower 10, the top material of the stabilization tower and the bottom material of the stabilization tower are obtained.

[0104] The operating conditions of the stabilization tower 10 include: a stabilization tower reaction pressure of 0.8 MPaG, a stabilization tower top operating temperature of 60° C., and a stabilization tower plate number of 50;

[0105] The stabilization tower top material is processed by the stabilization tower condenser 11 to obtain a stabilization tower top gas phase product and a stabilization tower top liquid phase material; the stabilization tower top gas phase product and the uncondensed purge gas are sent out of the device together, and the stabilization tower top liquid phase material is refluxed to the stabilization tower 10 for distillation cycle;

[0106] The top material of the stabilization tower is processed by the stabilization tower reboiler 12, a portion of which is refluxed to the bottom of the stabilization tower 10 for distillation circulation, and the other portion is sent out of the device as the bottom product of the stabilization tower;

[0107] The hydrogenated product is taken out through the upper side line (hydrogenated product discharge line 20) of the distillation section of the stabilizer tower.

[0108] The gaseous product at the top of the stabilization tower includes hydrogen and methane; the bottom product of the stabilization tower is a mixture rich in C5 and C8; the hydrogenated product is a butadiene-rich product, which can be returned to the butadiene extraction unit to increase butadiene production.

[0109] Table 1

[0110] logistics Alkyne-rich C4 raw materials Hydrogenation products Release the air heavy components Phase gaseous liquid gaseous liquid Temperature, °C 45 40 20 70 Pressure, MPaG 0.005 1.2 0.7 0.8 Mass fraction, % hydrogen 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 Isobutylene 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 components 0.505 0 0 62.57 water 0.3 0.04 0.07 0.02 N,N-Dimethylformamide 0.5 0 0 0 total 100.00 100.00 100 100

[0111] Table 1 shows the composition and operating conditions of the hydrogenated product, uncondensed purge gas, and heavy components obtained from a butadiene extraction unit using the method of this embodiment, after treating a vapor-phase, alkyne-rich C4 feedstock containing the solvent N,N-dimethylformamide. Economic calculations show that using the apparatus and method of this embodiment, a 200,000 tons / year butadiene extraction system can produce 2 tons / hour of C4 alkynes as a by-product, and then selectively hydrogenate butadiene for an investment of 20 to 30 million yuan, generating an annual profit of 25 to 30 million yuan. This represents a significant payback period of just over a year.

[0112] Example 3

[0113] This embodiment provides a method for hydrogenating C4 alkynes, which uses the C4 alkyne hydrogenation apparatus described in Example 1 and includes the following steps:

[0114] S1: feeding the gas phase alkyne-rich C4 feedstock containing the solvent N,N-dimethylformamide into the C4 alkyne hydrogenation unit through the gas phase impurity-containing alkyne-rich C4 feedstock feed pipeline 14, and sequentially passing through the pressurizing device 1, the liquefaction and condensation unit 2, the water scrubber 3 and the dehydration unit 4, and sequentially undergoing pressurization, condensation and liquefaction, dehydration and impurity removal (removal of water-soluble impurities such as the solvent) and dehydration treatment to obtain the dehydration unit organic phase, i.e., the impurity-removed and dehydrated alkyne-rich C4, the aqueous phase of the water scrubber and the aqueous phase of the dehydration unit; and between the condensation treatment and the impurity removal treatment, a treatment of removing some heavy components by the alkyne separation tank 22 is also included;

[0115] The feed temperature of the gas phase impurity-containing alkyne-rich C4 raw material is 45° C., and the feed pressure is 10 kPaG; the pressure of the gas phase impurity-containing alkyne-rich C4 raw material after the pressurization treatment is 180 kPaG;

[0116] The condensation and liquefaction treatment scheme is a treatment scheme using a primary condenser 2-1 and a secondary condenser 2-2; the condensation medium 15 of the primary condenser 2-1 is cooling water 15-1, and the condensation medium 15 of the secondary condenser 2-2 is propylene 15-2;

[0117] The operating conditions of the water scrubber 3 include: the feed temperature of the water scrubber is 30°C, the number of plates of the water scrubber 3 is 40;

[0118] The solvent content of the liquid C4 after washing in the water scrubber 3 is 10 ppm; the free water content of the C4 after dehydration in the dehydration unit 4 is 100 ppm. The aqueous phase of the water scrubber and the aqueous phase of the dehydration unit are respectively combined through the aqueous phase outlet pipeline 29 at the bottom of the water scrubber and the aqueous phase outlet pipeline 25 of the dehydration unit to the wastewater discharge pipeline 17, and then discharged out of the device.

[0119] S2: sending the de-doped, dehydrated, acetylene-rich C4, hydrogen and hydrogenated recycled C4 together to the hydrogenation reactor, and performing a selective hydrogenation reaction with a non-precious metal nickel-based catalyst to produce butene-1, converting vinyl acetylene, butadiene and butyne in the unsaturated components into butene-1 and a small amount of butene-2 ​​to obtain a butene-1-rich component;

[0120] In the selective hydrogenation reaction to produce butene-1, the hydrogenation reactor 5 is an upward hydrogenation reactor, the inlet temperature of the hydrogenation reactor 5 is 45°C, the reaction pressure is 2.5 MPaG, the reaction temperature rise is 30°C, the circulation ratio is 15:1, and the catalyst volume space velocity is 1h -1 ;

[0121] S3: The discharge of the hydrogenation reactor 5 is sent to the hydrogenation separation tank 6 through the first inlet 31 of the hydrogenation separation tank; the light components separated in the hydrogenation separation tank 6 are sent to the hydrogenation aftercooler 7, the liquid phase obtained by cooling the hydrogenation aftercooler 7 is returned to the hydrogenation separation tank 6 through the second inlet 32 ​​of the hydrogenation separation tank, and the uncondensed purge gas obtained by cooling the hydrogenation aftercooler 7 is sent out of the device through the purge gas output pipeline 19;

[0122] S4: A portion of the bottom liquid phase separated from the hydrogenation separation tank 6 is cooled in the circulating cooler 9 and sent to the hydrogenation reactor 5 as the hydrogenation circulating C4, and the other portion is sent to the middle of the stabilization tower 10. After being processed in the stabilization tower 10, the top material of the stabilization tower and the bottom material of the stabilization tower are obtained.

[0123] The operating conditions of the stabilization tower 10 include: a stabilization tower reaction pressure of 0.8 MPaG, a stabilization tower top operating temperature of 60° C., and a stabilization tower plate number of 50;

[0124] The stabilization tower top material is processed by the stabilization tower condenser 11 to obtain a stabilization tower top gas phase product and a stabilization tower top liquid phase material; the stabilization tower top gas phase product and the uncondensed purge gas are sent out of the device together, and the stabilization tower top liquid phase material is refluxed to the stabilization tower 10 for distillation cycle;

[0125] The top material of the stabilization tower is processed by the stabilization tower reboiler 12, a portion of which is refluxed to the bottom of the stabilization tower 10 for distillation circulation, and the other portion is sent out of the device as the bottom product of the stabilization tower;

[0126] The hydrogenated product is taken out through the upper side line (hydrogenated product discharge line 20) of the distillation section of the stabilizer tower.

[0127] The gaseous products at the top of the stabilization tower include hydrogen and methane; the bottom product of the stabilization tower is a mixture rich in C5 and C8; the hydrogenation product is a butene-1-rich product, which can be sent to downstream chemical plants for further processing.

[0128] Table 2

[0129]

[0130]

[0131] Table 2 shows the composition and operating conditions of the hydrogenated product, uncondensed purge gas, and heavy components obtained from a butadiene extraction unit using the method of this embodiment, after treating a vapor-phase, N,N-dimethylformamide-containing solvent-rich C4 feedstock. Economic calculations show that using the apparatus and method of this embodiment, a 200,000 ton / year butadiene extraction system can produce 2 tons / hour of C4 alkynes as a byproduct, and selectively hydrogenate butene-1 for an investment of 20 to 30 million yuan, with an annual return of approximately 15 million yuan. This represents a significant payback period of just over two years.

[0132] While various embodiments of the present invention have been described above, the above description is intended to be illustrative, not exhaustive, and not limited to the disclosed embodiments. Many modifications and variations will be apparent to those skilled in the art without departing from the scope and spirit of the described embodiments.

Claims

1. A C4 alkyne hydrogenation device, characterized in that: The device includes a pressurizing device, a liquefaction condensation unit, a dehydration unit, a hydrogenation reactor, a hydrogenation separation tank, a hydrogenation aftercooler, a circulating cooler and a stabilizing tower, and optionally includes a water washing tower; A gaseous impurity-containing alkyne-rich C4 raw material feed pipeline is connected to the inlet of the boosting device; The outlet of the boosting device is connected to the inlet of the liquefaction condensation unit; The outlet of the liquefaction and condensation unit is connected to the inlet of the dehydration unit; optionally, the outlet of the liquefaction and condensation unit is connected to the inlet of the water scrubber, and the top outlet of the water scrubber is connected to the inlet of the dehydration unit; The organic phase outlet of the dehydration unit is connected to the de-doping, dehydration, and alkyne-enriched C4 feed pipeline; The de-doped, dehydrated, and alkyne-enriched C4 feed pipeline, the outlet connecting pipeline of the circulating cooler, and the hydrogen feed pipeline are all connected to the inlet pipeline of the hydrogenation reactor; The outlet of the hydrogenation reactor is connected to the first inlet of the hydrogenation separation tank; The top outlet of the hydrogenation separation tank is connected to the inlet of the hydrogenation aftercooler; the liquid phase outlet of the hydrogenation aftercooler is connected to the second inlet of the hydrogenation separation tank, and the gas phase outlet of the hydrogenation aftercooler is connected to the purge gas output pipeline; the bottom outlet pipeline of the hydrogenation separation tank is respectively connected to the hydrogenation circulation C4 pipeline and the middle inlet of the stabilization tower; the hydrogenation circulation C4 pipeline is connected to the inlet of the circulation cooler.

2. The C4 alkyne hydrogenation device according to claim 1, wherein: The boosting device is a blower or a compressor; The liquefaction condensation unit includes a primary condenser and / or a secondary condenser; The top of the water washing tower is connected to a water washing tower washing water feed pipeline, and the bottom is connected to 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 to the de-doped, dehydrated, alkyne-rich C4 feed pipeline through a reaction feed pump; the dehydration unit includes at least one of a decanter, a settler and a coalescer; the dehydration unit is further provided with a dehydration unit aqueous phase outlet pipeline, and the dehydration unit aqueous phase outlet pipeline includes 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; The bottom outlet pipeline of the hydrogenation separation tank is connected to the hydrogenation circulation C4 pipeline and the middle inlet of the stabilization tower respectively through a circulation pump; The top of the stabilization tower is provided with a stabilization tower condenser and a stabilization tower top gas phase product discharge pipeline, the bottom of the stabilization tower is provided with a stabilization tower reboiler and a stabilization tower bottom product discharge pipeline, and the upper part of the distillation section of the stabilization tower is provided with a hydrogenation product discharge pipeline.

3. A method for hydrogenating carbon tetraalkynes, characterized in that: The method adopts the C4 alkyne hydrogenation device according to claim 1 or 2, comprising the following steps: S1: The gaseous impurity-containing alkyne-rich C4 feedstock is sequentially passed through the boosting equipment, the liquefaction and condensation unit, and the dehydration unit, and is sequentially subjected to boosting, condensation and liquefaction, and dehydration treatment to obtain impurity-free and dehydrated alkyne-rich C4 and the aqueous phase of the dehydration unit; optionally, a water washing and impurity removal treatment is further included between the condensation treatment and the dehydration treatment to obtain the aqueous phase of the water washing tower; S2: sending the de-doped, dehydrated, and alkyne-rich C4, hydrogen, and hydrogenation recycled C4 to the hydrogenation reactor for hydrogenation reaction; S3: sending the discharge of the hydrogenation reactor to the hydrogenation separation tank through the first inlet of the hydrogenation separation tank; sending the light components separated in the hydrogenation separation tank to the hydrogenation aftercooler, sending the liquid phase obtained by cooling the hydrogenation aftercooler back to the hydrogenation separation tank through the second inlet of the hydrogenation separation tank, and sending the uncondensed purge gas obtained by cooling the hydrogenation aftercooler out of the device; S4: A portion of the bottom liquid phase separated from the hydrogenation separation tank is cooled in the circulating cooler and sent to the hydrogenation reactor as the hydrogenation circulating C4, and the other portion is sent to the middle of the stabilization tower. After being processed in the stabilization tower, a gas phase product at the top of the stabilization tower, a bottom product of the stabilization tower and a hydrogenation product are obtained.

4. The method for hydrogenating carbon tetraalkynes according to claim 3, wherein In step S1, The feed temperature of the gaseous impurity-containing alkyne-rich C4 raw material is 20-80° C., and the feed pressure is 2-20 kPaG; The pressure of the gaseous impurity-containing alkyne-rich C4 raw material after the pressurization treatment is 150-300 kPaG; The condensation and liquefaction treatment scheme is a treatment scheme using a primary condenser or a treatment scheme using a primary condenser and a secondary condenser; The condensing medium of the primary condenser of the treatment scheme using a primary condenser is chilled water or propylene; the condensing medium of the primary condenser of the treatment scheme using a primary condenser and a secondary condenser is cooling water or process material, and the condensing medium of the secondary condenser is chilled water or propylene; The operating conditions of the water washing tower include: the feed temperature of the washing water of the water washing tower is 20-50° C., and the number of plates of the water washing tower is 20-80.

5. The method for hydrogenating carbon tetraalkynes according to claim 3, wherein In step S1, Between the condensation process and the water washing and impurity removal process, a process of removing part of the heavy components by the alkyne separation tank is also included; 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. The method for hydrogenating carbon tetraalkynes according to claim 3, wherein In step S1, the gas-phase impurity-containing alkyne-rich C4 raw material includes the gas-phase impurity-containing alkyne-rich C4 raw material from a butadiene extraction unit, wherein the impurities include water-soluble solvents and water-soluble polar organic matter.

7. The method for hydrogenating carbon tetraalkynes according to claim 6, wherein The water-soluble solvent is at least one or more mixtures or aqueous mixtures of acetonitrile, N,N-dimethylformamide, N-methylpyrrolidone and N-formylmorpholine.

8. The method for hydrogenating carbon tetraalkynes according to claim 3, wherein In step S2, the hydrogenation reaction is to perform one or more of a selective hydrogenation reaction to produce butene-1, a selective hydrogenation reaction to produce butadiene, or a full hydrogenation reaction to produce alkanes on the unsaturated components in the hydrogenation reactor; The unsaturated component is at least one of vinyl acetylene, butadiene, butyne, butene-1, butene-2 ​​and isobutylene.

9. The method for hydrogenating carbon tetraalkynes according to claim 8, wherein The selective hydrogenation reaction to produce butene-1 is a reaction that converts the unsaturated component into a butene-1-rich component. In the selective hydrogenation reaction to produce butene-1, the inlet temperature of the hydrogenation reactor is 20-70°C, the reaction pressure is 0.5-3 MPaG, the reaction temperature rise is 5-50°C, the hydrogen-acetylene molar ratio is 0.5-5, the circulation ratio is 10:1-40:1, and the catalyst volume space velocity is 0.1-10h -1 The catalyst is at least one of a noble metal platinum series, a noble metal palladium series, a non-noble metal nickel series, and a non-noble metal copper series; The selective hydrogenation reaction to butadiene is a reaction for converting the unsaturated component into a butadiene-rich component. In the selective hydrogenation reaction to butadiene, the inlet temperature of the hydrogenation reactor is 15-70°C, the reaction pressure is 0.4-3 MPaG, the reaction temperature rise is 5-50°C, the hydrogen-acetylene molar ratio is 1-3, the circulation ratio is 5:1-40:1, and the catalyst volume space velocity is 0.1-10h -1 The catalyst is at least one of a noble metal platinum series, a noble metal palladium series, a non-noble metal nickel series, and a non-noble metal copper series; 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°C, the reaction pressure is 0.5-3 MPaG, the reaction temperature rise is 5-60°C, the hydrogen-alkyne molar ratio is 1-5, the circulation ratio is 5:1-40:1, and the catalyst volume space velocity is 0.1-10h -1 The catalyst is at least one of a precious metal platinum system, a precious metal palladium system, a non-precious metal nickel system, and a non-precious metal copper system.

10. The method for hydrogenating carbon tetraacetylene according to claim 3, wherein: In step S4, the operating conditions of the stabilization tower include: a reaction pressure of the stabilization tower of 0.5 to 1.0 MPaG, an operating temperature of the top of the stabilization tower of 35 to 80° C., and a plate number of the stabilization tower of 20 to 80; The bottom liquid phase separated from the hydrogenation separation tank sent to the middle of the stabilization tower is processed by the stabilization tower to obtain a stabilization tower top material and a stabilization tower bottom material; The stabilization tower top material is processed by the stabilization tower condenser to obtain the stabilization tower top gas phase product and the stabilization tower top liquid phase material; the stabilization tower top gas phase product and the uncondensed purge gas are sent out of the device together, and the stabilization tower top liquid phase material is refluxed to the stabilization tower for distillation cycle; The bottom material of the stabilization tower is processed by the stabilization tower reboiler, a portion of which is refluxed to the bottom of the stabilization tower for distillation circulation, and the other portion is sent out of the device as the bottom product of the stabilization tower; The hydrogenation product is taken out from the side line at the upper part of the distillation section of the stabilization tower.

11. The method for hydrogenating carbon tetraacetylene according to claim 10, wherein: The gaseous product at the top of the stabilization tower includes at least one or more mixtures of hydrogen, methane and C4; the bottom product of the stabilization tower is a heavy component; and the hydrogenated product is a butene-1-rich product, a butadiene-rich product or an alkane-rich product.

12. The method for hydrogenating carbon tetraacetylene according to claim 11, wherein: The bottom product of the stabilizing tower is a mixture rich in C5 and C8.

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