METHOD FOR PRODUCING BUTADIENE
The present invention refers to the production of manufacturing method relates to, saving energy and material ratio is provided, productivity can be secured to the diameter of number decided process performance high purity butadiene butadiene manufacturing method are disclosed. Butadiene (Butadiene) petrochemical number is used as an intermediate in the presence of a petroleum chemical market large aspect ratios, petrochemical based on current market demand value as one of the most important oil etc. near the walls. Extracting method from the hydrocarbon cracking C4 through a leaden company number bath method include butadiene, butene (butene) direct dehydrogenation, oxidative dehydrogenation of butene (butene) etc. through reaction (oxidative dehydrogenation) method. The chemical oxidation of one of the method for the manufacture of oxygen number bath via reaction butadiene reaction with number 2 to butadiene is a stand-alone two hydrogen generating reaction, the production of which is very advantageous since thermodynamically stable product, exothermic reaction unlike direct dehydrogenation because the higher temperature than the yield of butadiene is lower than direct dehydrogenation reaction can be achieved. The chemical reaction is oxidation of butadiene can meet the demand extend through process for manufacturing method is effective method can be. On the other hand, such as the chemical oxidation of the method, oxygen and reduced risk due to explosion, the exothermic heat number for every other purposes in addition to raw material mainly nitrogen, water vapor (steam) or the like and can be used as dilution gas, dilution gas and light gas flow (COx, O2 Or the like), hydrocarbons and the like a reaction product from the reaction product of hydrocarbons when separated solvent hydrocarbons in absorbing and cooling the reaction product and method being mainly hydrocarbons for liquefying method are provided which during absorption method. The reaction product is present dilution method to separate the reaction product liquefied gas and light gas flow required off cryogenic refrigerant which can be non-capillary device, such as linearly by the process in order to ensure non-operation is difficult to increase the diameter of number's oldest. In this regard Figure 1 shows a device of the existing method to explain method number bath surface on butadiene also are disclosed. The reference also 1, butene, oxygen (O2 ), Water vapor (steam) and dilution gas containing nitrogen oxide and gaseous reaction products including butadiene dehydrogenation reaction material from oxidation dehydrogenation reactor (110); said cooling section for separating water from the reaction product derived from a dehydrogenation oxide (120); said water from oxidation dehydrogenation in the products of butadiene or butadiene C4 hydrocarbons mixture and separating a absorbent separating portion (130); and said absorbent separating portion (130) isolated from butadiene are included in separating flow (stream) butadiene positive number portion (140); without using a tool. Said oxidation dehydrogenation reactor (110) and is butene, oxygen (O2 ) On, water vapor (steam) on, dilution gas (N2 ), Said recovered unreacted butene for increasing positive number in ferritic catalyst or bismuth grade molybdenite concentrates comprising reaction raw material using a catalyst be a driven isothermal or under adiabatic conditions. Cooling said separating portion (120) includes a quench direct cooler method (quencher) or indirect cooling driven may be disclosed. Figure 1 said absorbent separating portion (130) can absorb selectively only butadiene in separating said example or absorbent separating portion (130) is butadiene dehydrogenation in the products of the oxidation for reparing over water number can absorb selectively only or C4 hydrocarbons comprising a mixture using a solvent that is capable of absorbing the entire absorbent manner be a driven. Example selective absorbent solvent ACN (Acetonitrile), NMP (N n-methylpyrrolidone), DMF (Dimethyl formamide) (toluene) and the full absorbent solvent like toluene, xylene (xylene) can be is used as the alkali. Said absorbent separating portion (130) on isolated from COx O2 , Dilution gas used N2 The entire incineration treating the recovered portion along like some of which are the time when reused by reaction section. Said positive number portion (140) is in one positive number device Acetonitrile to conventional butadiene) process, (N non-methylpyrrolidone) process on NMP, DMF or the like (Dimethyl formamide) process modifications of said device is in the form of a driven butadiene can be positive number. However, absorbent separation processes (130) excess solvent is used in most absorbent solvent recovery process number part of base station controller (140) are used in the process of large quantities of energy recovery and butadiene in positive number. In addition replaced cryogenic refrigerant condensation separation process energy absorbent separation processes even if required, material ratio, such as diameter of number process production costs cannot be secured it to data in a database related technology can improve the development gulp are disclosed. Said prior art door such as if the point number, the present invention refers to oxidation of butane gas through dehydrogenation reaction using nitrogen instead of morning fair number butadiene dilution, use conventional nitrogen oxide from the reaction product of butadiene dehydrogenation is divided by the low temperature refrigerant or absorbent separation method using water instead mounted to separate a condensation separation method number liquefying butadiene substrate. In particular condensation separation COx divided on O2 , N - butane and the like between flow discharged with the efficacy (butadiene defines all the hydrocarbons) in order to minimize loss of condensed stream of recovering method number bath method applied to the entire effective ingredient from the butadiene intended number. The present invention of the present invention said purposes and other purposes are described for all can be achieved. In order to achieve said purposes of, the present invention refers to Butene, oxygen (O2 ), Water vapor (steam) and dilution gas oxidation reaction material including dehydrogenation reaction including butadiene oxide obtained passing to obtain a dehydrogenation reaction product, Said butadiene dehydrogenation reaction product including oxide while passing the separated water cooling section, Said dehydrogenation reaction product water from oxidation and condensed hydrocarbons passed through a condensation separation unit, Said condensation separation unit not condense hydrocarbons including oxide dehydrogenation reaction product gas dilution in the presence of absorbent separation while passing incombustible hydrocarbons not condense and recovering the entire condensation separation unit, Said condensation separation in the condensed n - butane, butene and butadiene hydrocarbons included in the deformation part passed through a number comprising the step of separating the butadiene, Said condensation separation unit not condense hydrocarbons including oxide dehydrogenation reaction product, which can be non-combustible dilution gas flow transfers during absorbent separation, positive number n - butane gas separated in said butadiene number into said mixed oxide included in the dehydrogenation reaction, the butene butadiene has been separated in said remaining positive number, said kiln and mixed with the raw material butene oxide dehydrogenation unit, characterized in that the modulus of said dilution gas is butane squalane manufacturing method characterized a number substrate. In addition the present invention refers to butene, oxygen (O2 ), Water vapor (steam) and dilution gas oxidation reaction material including dehydrogenation reaction oxidation reaction section; said dehydrogenation oxide obtained from butadiene dehydrogenation reaction product including oxide for separating water from cooling section; Said hydrocarbons condensed water from oxidation dehydrogenation in the products of the condensation separation unit; Said condensation separation unit not condense hydrocarbons including oxide dehydrogenation in the products of the incombustible gas dilution on the presence O COx2 , Separation of gas dilution incombustible absorbent separating portion; and Said condensation separation in the condensed n - butane, butene and butadiene and the like for acquiring crude hydrocarbon, absorption modulation section recovered n - butane, butene and butadiene and the like for acquiring crude hydrocarbon in, butadiene positive number separating part; and, Positive number n - butane gas separated in said butadiene number included in the mixed into said oxidation dehydrogenation reaction, the butene butadiene has been separated in said remaining positive number, said dehydrogenation unit is installed and mixed with the raw material butene oxide characterized by a modulus of number bath device number substrate. According to the present invention through oxidation of isobutane dehydrogenation morning fair number dilution using nitrogen gas instead of butadiene, conventional nitrogen in use from the reaction product of butadiene is divided by the low temperature refrigerant or absorbent separation method using water instead mounted to separate condensation separation method after liquefying butadiene hydrocarbons absorbent separation method and the condensing stream to the display through the entire recovery of hydrocarbon loss energy consumption in the material ratio by minimizing the diameter of number can be secured safely removing performance high purity butadiene intended for a number modulus of the manufacturing method. Figure 1 shows a device of the existing method to explain method number bath surface on butadiene also are disclosed. The present invention according to the device manufacturing method number 2 to 6 also for drawing to explain on crude butadiene are disclosed. Also the present invention according to in the embodiment 1 and comparison example 1, 2 Figure 7 shows a main flow absorption modulation section seat surface oxygen concentration indicating an area are disclosed. Hereinafter of the present invention detail device manufacturing method of the SFC butadiene and number tank 2000. Manufacturing method and device of the present invention is butadiene as water condensation separation process and condensation separation process number bath butane gas dilution holes in order flow in recovering the entire upper part of active ingredient characterized by applying absorbent separation processes are disclosed. The use of low-temperature refrigerant or cooling in an isobutane dehydrogenation oxidation as dilution gas condensation separation can be separating hydrocarbons from the reaction product, total hydrocarbons recovered in absorbent separating portion being interposed between the external active principle by minimizing the diameter number number being interposed between the external-butadiene can be high pressure liquid coolant. Drawing number on the device manufacturing method of the present invention under using crude butadiene and transmissions take other. The present invention according to the method number 2 to 6 also for drawing to explain on butadiene bath device are disclosed. The reference 2 also, first butene, oxygen (O2 ), Water vapor (steam) and dilution gas (butane) oxidation reaction material including a dehydrogenation reaction section (210) passing a butadiene obtain oxidation dehydrogenation reaction product. The, positive number in said reaction material has a positive number (B7, B8) and discharge flow generated after being treated with factor obtained oxide dehydrogenation unit (210) can be entering, said flow processes (B1) is butadiene, n - butane, butene, O2 , COx, H2 O can be like. (B1) cooling said dehydrogenation oxide discharged from flow separation unit (220) enters the water separated therefrom. (B2) cooling said discharge flow generated after separation is butadiene, n - butane, butene, O2 , Which can be like COx, condensation separation unit (230) introduced into the substrate. Said condensation separation condensing separation step (B3) generated after discharge flow provided from cooling water that is not condensed hydrocarbons compression/cooling and condensing through then the dehydrogenation reaction product comprising hydrocarbons including oxide can be, absorbent separating portion (250) hydrocarbons enters recovery substrate. Said condensation separation before discharge flow (B4) to another condensing section (230) condensed in the n - butane, butene and butadiene and the like for acquiring crude hydrocarbon can be included and, positive number portion (240) butadiene can in positive number. Said condensation separation unit (230) not condense said dehydrogenation reaction product hydrocarbons including oxide absorbent separating portion (250) and transferring the substrate into the incombustible particles during dilution gas flow, in this case absorption separation processes occurring in vapor compositions can be ensure stability by not entering the explosion area. Said absorbent separation step (B5) previously generated discharge flow is divided O condensation separation2 , Like COx incombustible gas and dilution may be included, in the absorbing section discharge flow (B6) generated in another absorbent after separation (250) on isolated from COx O2 a number n - butane, butene and butadiene and the like for acquiring crude hydrocarbon can be included and, said positive number portion (240) passing a butadiene can be separated. Positive number is generated after said discharge flow (B7) comprises n - butane-rich remaining can be, oxidation dehydrogenation unit (210) to be coated to form a recirculation flow kiln. Said positive number portion (240) including reduction of remaining in butadiene has been separated during the discharge flow (B8), butene oxide raw material by mixing said dehydrogenation reaction section (210) is installed can be recycled to form, in this case reactor and an excellent effect is transferred spacer flow tides. Said "crude (Crude) hydrocarbon" in the art no crude (crude) hydrocarbons and conventional means, not with specific hydrocarbons including positive number obtained from the reaction product of butadiene dehydrogenation oxide like refer to as negative material. Said terms are otherwise unspecified "COx" without the, CO, CO2 Lapse of each other. Said 1 - butene is butene, 2 - butene or a combination of be a. Said bath including reduction of raw materials can be used including a number generally butadiene raw material is not particularly when a butene number one. In one embodiment said butene very high purity butene, naphtha C4 raffinate (raffinate) for the recovery of the two imide -2, raffinate (raffinate) such as butene stream -3 including hydrocarbon mixture can be obtained. Said water vapor (steam) is oxide in the reaction, adverse affects during the reactants, catalyst (coking) prevention and the exothermic heat number into which horizontally to at volatile gas are disclosed. On the other hand, said oxygen (O2 ) Is allowed to react with butene as dehydrogenation reaction oxidation number deformable cladding layer. Said oxidation catalyst filled within the reactor can be the high pressure liquid coolant reacting butadiene butene number if not one specifically number, e.g. grade molybdenite concentrates can be ferritic catalyst or bismuth catalyst. In one embodiment of the present invention search, said catalyst may be ferritic catalyst, among zinc ferrite, magnesium ferrite, manganese ferrite can be used butadiene selectivity height. The amount of odd pixels of said reaction catalyst reaction can be depending on specific conditions. Be said dilution gas is butane. Example incombustible said dilution gas is nitrogen gas (N2 ), Argon, helium or carbon dioxide (CO2 ) May be, preferably nitrogen gas and, in this case oxygen (O2 ) And n - butane mole fraction of hydrocarbon resultant explosion ranges need to be disclosed. Said oxidation dehydrogenation unit (210) is in one embodiment, butene and, oxygen (O2 ) On, water vapor (steam) on, said positive number portion (240) in a texture unit n - butane as residue separating butadiene and reduction of said oxidation dehydrogenation catalyst isothermal or adiabatic conditions ferritic which resolves the be a driven. In one embodiment said reaction material included in oxygen (O2 ) Is 90% or more purity, 95% greater than or 98% or more gaseous form can be input. Said 90% or more purity gaseous oxygen (O2 ) Introduced air from without, which means that the kiln can be in the form of basic oxygen, through, such as by measuring the amount of active ingredient between reactor embodiment amount of the ingredients contained in reaction material into which can be set individually. In one embodiment said oxidation dehydrogenation unit (210) in reaction conditions process comprises the steps of: oxygen: water vapor: dilution gas (n - butane)=1:0. 5 - 3:0. 1 - 20:0. 1 - 20 May be molar ratio, saving in energy and material ratio within this range, such as improving the productivity of excellent mirror number can be lead-free. In specific embodiments, oxide dehydrogenation unit (210) is oxygen: butene molar ratio of 0. 5 - 3:1, Steam: butene molar ratio of 1 - 20:1, n - butane: butene molar ratio of 0. 1 - 20:1, The reaction pressure atmospheric - 10atm, preferably an isothermal reaction temperature 150 provided 650 °C or driven under adiabatic conditions, saving in energy and material ratio within this range, such as improving the productivity of excellent mirror number can be lead-free. Cooling said separating portion (220) is in one direct cooler method (quencher) quench or indirect cooling can be driven, the implementation being 0 - 100 °C quench temperature. Said condensation separation unit (230) is in one embodiment, non single stage 1, stage 2 to stage compression structure 10, or 1 end-stage compression structure -2 stage may have. Said first reduced to a pressure at a time of multi-compression reason for wanting to target during the compression, many power are spaced by compression gas as well as heat is generated, thereby expands the gas compression efficiency is deteriorated, the door number multiple compression embodiment to prevent all, said compressing process using a cooler heat can be cool. Said condensation separation unit (230) condensation conditions in consideration of unreacted oxygen explosion range (upper limit greater than or limiting oxygen concentration hereinafter explosion) corresponding flow range can be determined to have. In one embodiment of the present invention search, said condensation separation unit (230) used in the coolant flowing cooling water, ethylene glycol, concentration 20 - 100% by weight aqueous solution of ethylene glycol, propylene glycol, propylene glycol concentration 30 - 100 weight % aqueous solution and at least one selected from the group consisting 1 be a propylene-based solvent. For example propylene or propylene compound including said propylene solvent, -10 °C hereinafter, or -10 -50 °C to materials having boiling point can be. Said refrigerant preferably cooling water, cooling water 0 to 40 °C, or cooling water may be 5 to 30 °C, in this case said extrusion units 250 °C hereinafter, or may be 50 to 200 °C, flow of cooling temperature 120 °C hereinafter compression, or 20 to 80 °C implementation being. Dilution is by using nitrogen gas, dilution gas and light gas flow separating the condensation method where attached to a cryogenic refrigerant, butane gas time to prevent dilution in the present invention, in accordance with the even lower than refrigerant grade. Said positive number portion (240) is butadiene applying positive number can be a conventional device, in one embodiment ACN (Acetonitrile) process, NMP (N n-methylpyrrolidone) process, or DMF (Dimethyl formamide) can be second direction. Said absorbent separating portion (250) for absorbing the entire example toluene as a solvent includes hydrocarbons, such as xylene using absorption can be driven. Said condensation separation unit (230) not condense said dehydrogenation reaction product hydrocarbons including oxide absorbent separating portion (250) can be transferred during exhaust flow incombustible dilution gas is put. Said absorbent separating portion (250) of hydrocarbon concentration by dilution is incombustible gas present upper explosion limit oxygen concentration such that the limiting oxygen concentration hereinafter hereinafter more or explosion either possibility can be a stand-alone number explosion in absorbent separating portion characterized by stability to. Separation via a number obtained by the butadiene via said sealer is coated in the solvent, so that the number of special high-boiling and low-boiling components, high purity butadiene can be recovered. In one embodiment of the present invention search, said through the resulting in a series of steps can be butadiene purity of 95. 0 - 99. Implementation being 9%. The cooling section also 3 to 9 said in Figure 2 (220) through water from oxidation dehydrogenation product (230) on absorbent separating portion (250) through pulsator number portion (240) is installed process of subdividing including feed de base (discharge flow B4, B6) are disclosed. The conventional example using stripping column feed de said base, or can be driven into the de. The reference also 3, first butene, oxygen (O2 ), Water vapor (steam) and dilution gas (butane) oxidation reaction material including a dehydrogenation reaction section (310) including passing a butadiene dehydrogenation oxidation to obtain reaction product. The, oxidation dehydrogenation reaction product number process (B7, B8) and discharge flow generated after being treated with sealer is coated in the positive number obtained oxide dehydrogenation reactor (310) can be entering. Said flow processes (B1) is butadiene, n - butane, butene, O2 , COx, H2 O can be like, cooling separating portion (320) enters the water separated therefrom. (B2) cooling said discharge flow generated after separation is butadiene, n - butane, butene, O2 , Which can be like COx, condensation separation unit (330) introduced into the substrate. Said condensation separation condensing separation step (B3) generated after discharge flow provided from cooling water that is not condensed hydrocarbons compression/cooling and condensing through then the dehydrogenation reaction product comprising hydrocarbons including oxide can be, absorbent separating portion (350) introduced into the substrate. Said condensation separation generated after discharge flow (B4 ') is condensed in said condensation separation unit to another n - butane, butene and butadiene included in the dehydrogenation reaction product comprising hydrocarbons including oxide can be, de base (360) on O enters COx2 Is separated therefrom. Said absorbent separation step (B5) previously generated discharge flow is divided O condensation separation2 , And the like may be included COx incombustible gas dilution, said discharge flow (B6 ') generated in the absorbing section absorbent after separation (350) on O COx in2 a number n - butane, butene and butadiene included in the total solvent comprising hydrocarbons can be absorbed, solvent recovering section (370) to recover solvent passing, said exhaust flow (B9) recovered solvent through said absorbent separating portion (350) texture to can. (B10) can be solvent number generated in said another feed discharge flow for reparing over n - butane, butene and butadiene and the like including hydrocarbons can be included, de base (360) COx while passing on O2 Can be further separated. Degassing said generated after discharge flow (B4 ") type and includes a base (360) on which an additional separate COx O2 a number n - butane, butene and butadiene and the like for acquiring crude hydrocarbon can be included and, positive number portion (340) passing a butadiene can be separated. Positive number is generated after said discharge flow (B7) comprises n - butane-rich remaining can be, oxidation dehydrogenation unit (310) to be coated to form a recirculation flow kiln. Said positive number portion (340) remaining in the scrubber flow (B8) butene butadiene has been separated, and butene raw material obtained oxide dehydrogenation unit (210) to form recirculation is installed to be coated. Example incombustible said dilution gas is nitrogen gas (N2 ), Argon, helium or carbon dioxide (CO2 ) May be, preferably nitrogen gas and, in this case oxygen (O2 ) And n - butane mole fraction of hydrocarbon resultant explosion ranges need to be disclosed. Figure 4 shows a discharge flow generated after degassing in also said 3 (another ") B4 (B4" discharge flow ') that further, said discharge flow (B4 ") reactor is base (460) on which an additional separate COx O2 a number n - butane, butene butadiene, and the like high-boiling hydrocarbons can be included, high-boiling-point number rejection (480) which in separating high-boiling, high-boiling process would discharge flow is generated after said number (B4 " ') high-boiling material number for reparing over n - butane, butene and butadiene and the like for acquiring crude hydrocarbons can be comprising, said positive number portion (440) are introduced into the pulsator number. Distillation can be operated high-boiling said number rejection is one example. Said high-boiling-point material is in one embodiment furan current, aldehydes, acetic acid, benzene, or the aromatic hydrocarbon, or be a polystyrene. The reference also 4, first butene, oxygen (O2 ), Water vapor (steam) and dilution gas (butane) oxidation reaction material including a dehydrogenation reaction section (410) obtain oxidation dehydrogenation reaction product including passing a butadiene. At this time, reaction material has a positive number process (B7, B8) and discharge flow generated after being treated with factor positive number obtained oxide dehydrogenation unit (410) can be entering. Said flow processes (B1) is butadiene, n - butane, butene, O2 , COx, H2 O can be like, cooling separating portion (420) enters the water separated therefrom. On in the same manner as in Figure 3, cooling said discharge flow generated after separation (B2) is butadiene, n - butane, butene, O2 , Which can be like COx, condensation separator (430) introduced into the substrate. A condensing separation step (B3) generated after said condensation separation discharge flow provided from cooling water that is not condensed is then through cooling and condensing the compressed hydrocarbon/hydrocarbons including oxide dehydrogenation reaction product may be included and, absorbent separating portion (450) introduced into the substrate. Said condensation separation discharge flow (B3) is generated after said absorbent separating portion (450) is fed incombustible during dilution gas is turned on with each other. Example incombustible said dilution gas is nitrogen gas (N2 ), Argon, helium or carbon dioxide (CO2 ) May be, preferably nitrogen gas and, in this case oxygen (O2 ) And n - butane mole fraction of hydrocarbon resultant explosion ranges need to be disclosed. Said absorbent separation step (B5) previously generated discharge flow is divided on O COx condensation separation2 In an incombustible dilution gas and the like, said absorbent separation step (B6 ') on discharge flow generated in the absorbing modulation section COx O2 a number n - butane, butene and butadiene performance as a whole can be absorbed hydrocarbons solvent comprising, solvent recovering section (470) to recover solvent passing, said exhaust flow (B9) recovered solvent through said absorbent separating portion (450) to be . (B10) and solvent recovery generated after said discharge flow, said diverter including a hydrocarbons condensed in the condensation separation unit (B4 '), de base (460) while passing on O COx2 Can be further separated. Said discharge flow (B11) in said degassing process is de base (460) on which an additional separate COx O2 And said absorbent section (460) can be separated from the absorbent is installed and, to another (B4 ") type and includes a discharge flow generated after degassing said base (460) on which an additional separate COx O2 a number n - butane, butene and butadiene, and the like for acquiring crude hydrocarbon can be included high-boiling, high-boiling-point number rejection (480) can be enters separating high-boiling. Discharge flow is generated after said high-boiling-point number (B4 " ') number for reparing over high-boiling material process volatile n - butane, butene and butadiene and the like for acquiring crude hydrocarbon deformation part number (440) can be kiln. Said high-boiling-point material is for example benzene, styrene, or the aromatic hydrocarbons, butadiene dimer, protected morphinones acetoacetoxy-functional, benzo-protected morphinones or be. Said positive number portion (440) passing a butadiene can be separating, positive number is generated after said discharge flow (B7) n - butane-rich remaining can be included, said oxidation dehydrogenation unit (410) can be kiln to form a recirculation flow. Said positive number portion (340) remaining in the scrubber flow (B8) butene butadiene has been separated, said oxidation dehydrogenation unit (410) is installed can be recycled to form. Figure 5 shows a degassing of discharge flow (B11) generated after another discharge flow also said 3 (B11 ') that replaced, de base (560) on isolated from COx O2 Condensing the gas into the separation efficiency can be improved. Said condensation system are otherwise not specific, compressor (531), heat exchange (532) and condensation separation unit (530) has a system including age. The reference also 5, first butene, oxygen (O2 ), Water vapor (steam) and dilution gas (butane) oxidation reaction material including a dehydrogenation reaction (510) to obtain butadiene dehydrogenation reaction product obtained passing including oxide. The, positive number in said reaction material has a positive number (B7, B8) and discharge flow generated after being treated with factor obtained oxide dehydrogenation unit (510) can be entering, in the reaction process said discharged flow (B1) is butadiene, n - butane, butene, O2 , COx, H2 O can be like cooling separating portion (520) enters the water separated therefrom. (B2) cooling said discharge flow generated after separation is butadiene, n - butane, butene, O2 , Which can be like COx, condensation separation unit (530) introduced into the substrate. Said condensation separation condensing separation step (B3) generated after discharge flow installed in cooling and condensing the hydrocarbons through compression/cooling water that is not condensed hydrocarbons including oxide dehydrogenation reaction product then can be included and, said discharge flow (B3) includes an absorbent separating portion (550) introduced into the substrate. Said condensation separation unit (530) not condense hydrocarbons including oxide dehydrogenation product the scrubber flow (B3), absorbent separating portion (550) is turned on during entering the incombustible gas dilution are disclosed. Said condensation separation before discharge flow to another (B4 ') is condensed n - butane, butene and butadiene included in the dehydrogenation reaction product can be hydrocarbons including oxide, said base de (560) on O enters COx2 Are isolated each other. Said absorbent separation step (B5) previously generated discharge flow is divided on O COx condensation separation2 In an incombustible dilution gas and the like, said separating portion is such discharge flow generated in another absorbent separation step (B6 ') (550) COx in on O2 a number n - butane, butene and butadiene and the like a solvent recovering section being entirely absorbed hydrocarbons solvent (570) passing to recover a solvent, said solvent recovered (B9) discharge flow through said absorbent separating portion (550) texture to can. (B10) and said discharge flow generated in another solvent recovery process, condensed in said condensation separation unit (B4 ') hydrocarbons including a diverter, de base (560) COx while passing on O2 Can be further separated. Degassing said generated after discharge flow (B11 ') type and includes a base (560) on which an additional separate COx O2 And, said condensation system condensation system with a diameter in said condensation separation unit (530) can be re-condensation separation, to another (B4 ") type and includes a discharge flow generated after degassing said base (560) on which an additional separate COx O2 a number n - butane, butene and butadiene and the like for acquiring crude hydrocarbon can be included and, positive number portion (540) and separately passing butadiene. Said condensation system are otherwise not specific, compressor (531), heat exchanger (532) and condensation separation unit (530) has a system including age. Positive number is generated after said discharge flow (B7) remaining n - butane-rich can be included, said oxidation dehydrogenation reaction (510) to be coated to form a recirculation flow kiln. Said discharge flow (B8) is generated after said positive number to another positive number portion (540) may include butene and remaining in butadiene has been separated, said dehydrogenation reaction by mixing a raw material butene oxide (510) is installed can be recycled to form. Figure 6 shows a degassing of discharge flow (B11) also said 4 generated after another discharge flow (B11 ') that replaced, de base (660) on isolated from COx O2 Condensed into the condensed stream separator (630) by gas separation can be re-circulated to efficiency is improved. Said condensation system are otherwise not specific, compressor (631), heat exchanger (632) and condensation separation unit (630) has a system including age. 6 Also reference surface, first butene, oxygen (O2 ), Water vapor (steam) and dilution gas (butane) oxidation reaction material including a dehydrogenation reactor (610) obtain butadiene oxide including passing a dehydrogenation reaction product. The, positive number in said reaction material has a positive number (B7, B8) and discharge flow generated after being treated with factor obtained oxide dehydrogenation reactor (610) can be entering. In the reaction process said discharged flow (B1) is butadiene, n - butane, butene, O2 , COx, H2 O can be like, discharge flow (B1) cooling said separating portion (620) enters the water separated therefrom. Also in the same manner as 5 on, cooling said discharge flow generated after separation (B2) is butadiene, n - butane, butene, O2 , Which can be like COx, condensation separator (630) enters the water separated therefrom. Said condensation separation condensing separation step (B3) generated after discharge flow provided from cooling water that is not condensed hydrocarbons compression/cooling and condensing the hydrocarbons including oxide through the dehydrogenation reaction product then can be included. (B3) said diverter and absorbent separating portion (650) open at, said absorbent separating portion (650) can be incombustible during entering the dilution gas is turned on. Example incombustible said dilution gas is nitrogen gas (N2 ), Argon, helium or carbon dioxide (CO2 ) May be, preferably nitrogen gas and, in this case oxygen (O2 ) And n - butane mole fraction of hydrocarbon resultant explosion ranges need to be disclosed. Said absorbent separation step (B5) discharge flow is generated on an isolation COx O previous condensation separation2 , Incombustible gas dilution can be like, said absorbent separation step (B6 ') discharge flow generated in another absorbent separating portion (650) on O COx in2 a number n - butane, butene and butadiene performance as a whole can be absorbed hydrocarbons solvent comprising, solvent recovering section (670) to recover solvent passing, said exhaust flow (B9) recovered solvent through said absorbent separating portion (650) to be . (B10) and solvent recovery generated after said discharge flow to another, said condensation separation generated after a discharge flow (B4 '), said base de (660) COx while passing on O2 Can be separate. Degassing said discharge flow (B11 ') generated after the reactor is base (660) on which an additional separate COx O2 And, condensation system into a condensation separation unit (630) can be re-condensation separation, said degassing before discharge flow (B4 ") to another reactor is base (660) on which an additional separate COx O2 a number n - butane, butene and butadiene, and the like for acquiring crude hydrocarbon can be included high-boiling, high-boiling-point number rejection (680) high-boiling material enters the isolated each other. Said high-boiling-point number (B4 " ') number for reparing over high-boiling material discharge flow is generated after volatile n - butane, butene and butadiene are included for acquiring crude hydrocarbon can be included and, positive number portion (640) passing a butadiene can be separated. Positive number is generated after said discharge flow (B7) remaining n - butane-rich can be included, said oxidation dehydrogenation reactor (610) to be coated to form a recirculation flow kiln. Said discharge flow (B8) is generated after said positive number to another positive number portion (640) may include butene and remaining in butadiene has been separated, said dehydrogenation reactor and mixed with the raw material butene oxide (610) is installed can be recycled to form. Said manufacturing method used in bath device also as an example of the reference number 2, butene, oxygen (O2 ), Water vapor (steam) and a dilution gas (butane) reacting butadiene dehydrogenation reaction material including oxide including oxide dehydrogenation oxidation dehydrogenation reaction product (210); butadiene dehydrogenation reaction product including oxide for separating water from said cooling section (220); said water from condensing the hydrocarbons in the products of the oxidation dehydrogenation condensation separation unit (230); said condensation separation unit (230) not condense hydrocarbons including hydrocarbons in the presence of oxidation dehydrogenation in the products of the entire absorbent recovering incombustible dilution gas separation unit (250); said condensation separation unit (230) condensed in the n - butane, butene and butadiene are included for acquiring crude hydrocarbon in butadiene positive number separating portion (240); and, said positive number portion (240) n - butane number scrubber flow (B7) is isolated from butadiene, said oxidation dehydrogenation unit (210) into chamber construction. Said absorbent separating portion (250) in the presence of incombustible dilution gas recovered n - butane, butene and butadiene crude hydrocarbons including said discharge flow (B6) is included in the positive number portion (240) consists of than the first. Said positive number portion (240) n - butane gas isolated from butadiene number included in the oxidation dehydrogenation unit (210) consists of at least one exhaust valve (B7) with texture to flow. Said positive number portion (240) remaining in the scrubber flow (B8) butene butadiene has been separated, said raw material by mixing a butene oxide dehydrogenation unit (210) to texture to consists of. Example incombustible said dilution gas is nitrogen gas (N2 ), Argon, helium or carbon dioxide (CO2 ) May be, preferably nitrogen gas are disclosed. Another number as an example of the tank device reference also 3, butene, oxygen (O2 ), Water vapor (steam) and a dilution gas (butane) reacting butadiene dehydrogenation reaction material including oxide including oxide dehydrogenation oxidation dehydrogenation reaction product (310); butadiene dehydrogenation reaction product including oxide for separating water from said cooling section (320); said water from condensing the hydrocarbons in the products of the oxidation dehydrogenation condensation separation unit (330); said condensation separation unit (330) is not condense hydrocarbons including hydrocarbons in the presence of oxidation dehydrogenation in the products of the entire absorbent recovering incombustible dilution gas separation unit (350); said absorbent separating portion (350) recovered in n - butane, butene and butadiene and the like a solvent recovering section for recovering hydrocarbons including solvents and discharge flow (B6 ') (370) constructed to supply, said solvent recovering section (370) (B9) said diverter and a recovered solvent including the absorbent separating portion (350) to consists of recycled. Said condensation separation unit (330) condensed in the n - butane, butene and butadiene hydrocarbons including a discharge flow (B4 ') and the like, said solvent recovering section (370) number for reparing over solvent is n - butane, butene and butadiene in discharge flow (B10) including like hydrocarbons including, COx, O2 On, n - butane, butene and butadiene and the like a de hydrocarbons separating base (360); including a preferably. De said base (360) on isolated from COx O2 the scrubber flow (B11) is absorbent separating portion (350) to consists of cooling fluid. De said base (360) on isolated from COx O2 a number n - butane, butene and butadiene like discharge flow (B4 ") is comprised of said resistance comprising a positive number portion (340) consists of than the first. Positive number portion separating said butadiene (340) and, said positive number portion (340) number n - butane scrubber flow (B7) is isolated from butadiene, said oxidation dehydrogenation unit (310) to texture to consists of. Said positive number portion (340) remaining in the scrubber flow (B8) butene butadiene has been separated, said oxidation dehydrogenation unit (310) to texture to consists of. Example incombustible said dilution gas is nitrogen gas (N2 ), Argon, helium or carbon dioxide (CO2 ) May be, preferably nitrogen gas are disclosed. Another number tank device also as an example of the reference 4, butene, oxygen (O2 ), Water vapor (steam) and a dilution gas (butane) reacting butadiene dehydrogenation reaction material including oxide including oxide dehydrogenation products oxidation dehydrogenation unit (410); butadiene dehydrogenation reaction product including oxide for separating water from said cooling section (420); said water from condensing the hydrocarbons in the products of the oxidation dehydrogenation condensation separation unit (430); said condensation separation unit (430) not condense hydrocarbons including hydrocarbons in the presence of oxidation dehydrogenation in the products of the entire absorbent recovering incombustible dilution gas separation unit (450); said absorbent separating portion (450) recovered in n - butane, butene and butadiene hydrocarbons including solvents and the like solvent recovering section for recovering a discharge flow (B6 ') (470) constructed to supply, said solvent recovering section (470) (B9) said diverter and a recovered solvent including the absorbent separating portion (450) to consists of recycled. Said condensation separation unit (430) condensed in the n - butane, butene and butadiene such as hydrocarbons including discharge flow (B4 ') and composed, said solvent recovering section (470) number for reparing over solvent is n - butane, butene and butadiene hydrocarbons including discharge flow (B10) such as consisting in, COx, O2 On, n - butane, butene and butadiene such as hydrocarbons including separating base de (460); including a preferably. De said base (460) on isolated from COx O2 the scrubber flow (B11) is absorbent separating portion (450) to consists of cooling fluid. De said base (460) on isolated from COx O2 a number n - butane, butene and butadiene, high-boiling hydrocarbons and the like for acquiring crude scrubber flow (B4 ") high-boiling material to decouple a high-boiling-point number rejection (480) inserted into and, said high-boiling-point number rejection (480) isolated from n - butane, butene and butadiene and the like for acquiring crude comprising the hydrocarbons emissions flow (B4" ') consists of the positive number than the first portion. Positive number portion separating said butadiene (440); and, said positive number portion (440) number n - butane scrubber flow (B7) is isolated from butadiene, said oxidation dehydrogenation unit (410) to texture to consists of. Said positive number portion (440) (B8) remaining butene butadiene has been separated in the scrubber flow, said oxidation dehydrogenation unit (410) to texture to consists of. Example incombustible said dilution gas is nitrogen gas (N2 ), Argon, helium or carbon dioxide (CO2 ) May be, preferably nitrogen gas are disclosed. Said high-boiling-point material is in one embodiment furan current, aldehydes, acetic acid, benzene, or the aromatic hydrocarbon, or styrene are disclosed. Another number as an example of the tank device also 5 reference, butene, oxygen (O2 ), Water vapor (steam) and a dilution gas (butane) reacting butadiene dehydrogenation reaction material including oxide including oxide dehydrogenation oxidation dehydrogenation reaction product (510); butadiene dehydrogenation reaction product including oxide for separating water from said cooling section (520); condensing the water from said hydrocarbons in the products of the oxidation dehydrogenation condensation separation unit (530); said condensation separation unit (530) not condense hydrocarbons including oxide dehydrogenation in the products of the hydrocarbons in the presence of the entire absorbent separation recovering incombustible gas dilution (550); said absorbent separating portion (550) recovered in n - butane, butene and butadiene and the like a solvent recovering section for recovering hydrocarbons including solvents and discharge flow (B6 ') (570) constructed to supply, said solvent recovering section (570) (B9) said diverter and a recovered solvent including the absorbent separating portion (550) to consists of recycled. Said condensation separation unit (530) condensed in the n - butane, butene and butadiene hydrocarbons including discharge flow (B4 ') and the like, said additional solvent times (570) number for reparing over solvent is n - butane, butene and butadiene and the like hydrocarbons including in a discharge flow (B10), COx, O2 On, n - butane, butene and butadiene and the like a de hydrocarbons separating base (560); including a preferably. De said base (560) on isolated from COx O2 a number n - butane, butene and butadiene like discharge flow (B4 ") is comprised of said resistance comprising a positive number portion (340) constructed to supplied, said de base (560) on isolated from COx O2 The discharge flow (B11 ') into a condensation system comprising said condensation separation unit (530) to consists of recycled. Said condensation system are otherwise not specific, compressor (531), heat exchanger (532) and condensation separation unit (530) has a system including age. Positive number portion separating said butadiene (540); and, said positive number portion (540) the number n - butane scrubber flow (B7) isolated from butadiene, said oxidation dehydrogenation reaction (510) to texture to consists of. Said positive number portion (540) butadiene has been separated in the scrubber flow remaining butene (B8), butene and raw material obtained oxide dehydrogenation unit (210) to texture to consists of. Example incombustible said dilution gas is nitrogen gas (N2 ), Argon, helium or carbon dioxide (CO2 ) May be, preferably nitrogen gas are disclosed. As an example of a reference device also 6 the tank another number, butene, oxygen (O2 ), Water vapor (steam) and a dilution gas (butane) reacting butadiene dehydrogenation reaction material including oxide including oxide dehydrogenation oxidation dehydrogenation reaction product (610); butadiene dehydrogenation reaction product for separating water from said cooling section including oxide (620); condensing the water from said hydrocarbons in the products of the oxidation dehydrogenation condensation separation unit (630); said condensation separation unit (630) not condense hydrocarbons including hydrocarbons in the presence of oxidation dehydrogenation in the products of the entire absorbent recovering incombustible dilution gas separation unit (650); said absorbent separating portion (650) recovered in n - butane, butene and butadiene hydrocarbons including solvents and the like solvent recovering section for recovering a discharge flow (B6 ') (670) constructed to supply, said solvent recovering section (670) (B9) said diverter and a recovered solvent including the absorbent separating portion (650) to consists of recycled. Said condensation separation unit (630) condensed in the n - butane, butene and butadiene such as hydrocarbons including discharge flow (B4 ') and composed, said solvent recovering section (670) number for reparing over solvent is n - butane, butene and butadiene hydrocarbons including discharge flow (B10) such as consisting in, COx, O2 On, n - butane, butene and butadiene such as hydrocarbons including separating base de (660); including a preferably. De said base (660) on isolated from COx O2 The scrubber is flow (B11 ') into a condensation system, said condensation separation unit (630) to the original consists of. Said condensation system are otherwise not specific, compressor (631), heat exchanger (632) and condensation separation unit (630) has a system including age. De said base (660) on isolated from COx O2 a number n - butane, butene and butadiene, high-boiling hydrocarbons and the like for acquiring crude scrubber flow (B4 ") high-boiling material to decouple a high-boiling-point number rejection (680) is installed and, said high-boiling-point number rejection (680) isolated from n - butane, butene and butadiene and the like for acquiring crude comprising the hydrocarbons emissions flow (B4" ') consists of the positive number than the first portion. Positive number portion separating said butadiene (640); and, said positive number portion (640) the number n - butane scrubber flow (B7) isolated from butadiene, said oxidation dehydrogenation reactor (610) to texture to consists of. Said positive number portion (640) remaining in the scrubber flow (B8) butene butadiene has been separated, said oxidation dehydrogenation reactor (610) to texture to consists of. Example incombustible said dilution gas is nitrogen gas (N2 ), Argon, helium or carbon dioxide (CO2 ) May be, preferably nitrogen gas are disclosed. Said high-boiling-point material is in one embodiment furan current, aldehydes, acetic acid, benzene, or the aromatic hydrocarbon, or styrene are disclosed. Said absorbent separating portion (250, 350, 450, 550, 650) dilution in incombustible gas present on separate COx O2 , Incombustible dilution gas raw material heat up (heat up) heat generated by incineration, solvent recovering section (370, 470, 570, 670), or positive number portion (240, 340, 440, 540, 640) livestock in said absorbent separating portion (250, 350, 450, 550, 650) dehydrogenation reaction on said oxide (210, 310, 410, 510, 610) between, or said absorbent separating portion (250, 350, 450, 550, 650) on said condensation separation unit (240, 340, 440, 540, 640) between, or said absorbent separating portion (250, 350, 450, 550, 650) dehydrogenation reaction on said oxide (210, 310, 410, 510, 610) on said condensation separation unit (240, 340, 440, 540, 640) can be exchanging means. Manufacturing method and device of the present invention heretofore described butadiene used is such that the conventional butadiene number number bath sample dilution xylamine processing advantages of manufacturing method using pore-size effect, process can minimize energy consumption and maximize energy efficiency. In addition of the present invention (the aforementioned ACN, NMP, DMF or the like) in a variety of applications material manufacturing method butadiene positive number/number direct outer periphery of the bath, various applications disclosed. Hereinafter, a preferred embodiment of the present invention to aid in the understanding at one number, in the embodiment of the present invention is to in various angular positions in the present invention is exemplified ephemeral feature category and vertical range in which it is apparent that changes and modification of a skilled, of relay and modifying these modified of course also belonging to claim are disclosed. [In the embodiment] In the embodiment 1 Reaction raw material composition of table 1 below to of Figure 2 device having oxidized by using using raffinate -3 ferritic by catalytically butene: oxygen=1:09, Butene: water vapor=1:5, butene: butane=1:4 by reacting reactants having the molar ratio of the oxidation dehydrogenation, stand-alone water after cooling modulation section number, condensation separation and absorption separation step is negative raw material crude hydrocarbons obtained through pulsator number. In dehydrogenation reaction product followed by oxidation for reparing over water cooling number condensation separation unit 2 stage compressor of hydrocarbons using condensing and the coolant pressure was 40 °C. Condensation conditions condensation separation when the convex portions vapor compositions not entering the explosion area after condensation separation in order to minimize the loss of hydrocarbon vapor present effective absorption modulation section his entire absorbing hydrocarbons using toluene. The vapor generated in the non-absorbent composition diagram explosion region absorbent separation nitrogen is charged up. Toluene in the presence of hydrocarbons using nitrogen absorption modulation section by overall absorbent main vapor flow number to have the possibility to guarantee safety stand-alone process such that explosion of 99% positive to negative number butadiene recovery for acquiring crude hydrocarbon raw material are obtained. At this time, oxidation dehydrogenation of discharge flow measuring gas chromatography, cooling separating portion, absorbent condensation separation (B1, B2, B3, B3 provided 1, B5, B4 + B6) composition in each discharge flow section (AspenPlus) wool process are described to which code table 2 calculation is performed. In addition, the absorbent separating portion in solvent and usage and listed in tables 5, 6 to oxygen concentration table are described. Comparison example 1 In condensation separation unit in the embodiment 1 and the coolant pressure with compressed vent temperature by using 2 stage compressor having communication holes 80 °C condensing hydrocarbon was 40 °C. Condensation separation of vapor present effective for minimizing loss of hydrocarbon absorption modulation section incombustible gas dilution N a2 Except that the total absorbed hydrocarbons using toluene without easy and have in the embodiment embodiment, 99% positive to negative number butadiene recovery for acquiring crude hydrocarbon raw material are obtained. However process such that main vapor flow entering the explosion area by didn't guarantee safety. At this time, oxidation dehydrogenation of discharge flow measuring gas chromatography, cooling separating portion, (B1, B2, B3, B5, B4 + B6) absorbent separating portion each diverter and a condensation separation process are described to which code table 3 composition in wool (AspenPlus) calculation is performed. Comparison example 2 Using the lung light orgin of Figure 1 device using nitrogen gas for dilution by catalytically butene: oxygen=1:0. 96, Butene: steam=1:5, butene: molar ratio=1:4 by butadiene reaction material having nitrogen oxide are obtained. After cooling is modulation section in a stand-alone water absorbent separation reaction product number, positive number portion through a final article number are obtained. By using nitrogen dilution gas main vapor flow which ensures security for the possibility of a stand-alone process such that explosion of 99% positive to negative number number butadiene recovery for acquiring crude hydrocarbon raw material are obtained. Each process of Figure 1 absorbent separating portion (130) comprising the main flow (AspenPlus) wool which code table 4 was shown a calculation process, the energy needed for the recovery of solvent used amount solvent absorbent separating portion in tables 5 shown to usage. In the embodiment 1 and comparison example 1, 2 the energy needed for the recovery of solvent absorption modulation section solvent used amount amount was shown and listed in tables 5, 6 have shown the tables to seat within the main flow region absorbent separating oxygen concentration. A light gas flow *: COx, O2 C4 number than a higher boiling point than the current ** High-boiling products: benzene, styrene, or the aromatic hydrocarbons, butadiene dimer, protected morphinones acetoacetoxy-functional, benzo-protected morphinones or As shown in table 2 to 6, instead of using butane gas absorb nitrogen dilution in the presence of nitrogen gas dilution gas COx incombustible modulation section, O2 , N2 On n - butane, butene and butadiene in the beneficiation of many hydrocarbons including, secure a safety process such that may be confirmed. In addition, the present invention according to dilution using nitrogen gas instead of the comparison example 2 compared to the butane using nitrogen in the embodiment 1, the amount of solvent absorption modulation section by the reduced diameter number number are considerably reduced energy consumption high purity high pressure liquid coolant capable of butadiene. 110, 210, 310, 410, 510, 610: Oxidation dehydrogenation reaction 130, 250, 350, 450, 550, 650: Absorbent separating portion 120, 220, 320, 420, 520, 620: Cooling separation 230, 330, 430, 530, 630: Condensation separation unit 140, 240, 340, 440, 540, 640: Positive number unit 360, 460, 560, 660: De base 370, 470, 570, 670: Solvent recovering section 480, 680: High-boiling-point number rejection 531, 631: Compressor 532, 632: Heat exchanger The present invention relates to a method and an apparatus for producing butadiene. According to the present invention, butane is used instead of nitrogen as diluent gas for the production of butadiene through oxidative dehydrogenation of butane so as to easily separate butadiene from a reaction product composed of hydrocarbon including a C4 mixture and a gas stream. Therefore, economical efficiency of the process such as energy and raw material cost reduction, productivity improvement, etc. and high purity of butadiene can be safely secured. COPYRIGHT KIPO 2018 Butene, oxygen (O2 ), Water vapor (steam) and dilution gas oxidation reaction material including dehydrogenation reaction including butadiene dehydrogenation oxidation and passing a gaseous reaction products, said cooling section including butadiene dehydrogenation reaction product while passing the separated water oxidation, oxidation dehydrogenation reaction product water from said condensation separation unit and condensed hydrocarbons passed through, said condensation separation unit including oxide dehydrogenation reaction product hydrocarbons not condense while passing hydrocarbons in the presence of absorbent separation and recovering the entire incombustible dilution gas, condensed in said condensation separation unit n - butane, butene and butadiene included in the dehydrogenation reaction product hydrocarbons including oxide comprising the step of separating the butadiene part passed through a positive number, said positive number n - butane gas and an analog butadiene and butene included in said oxidation dehydrogenation unit number , modulus of manufacturing method characterized in that said dilution gas is butane. According to Claim 1, said reaction material included in oxygen (O2 ) Is 90% or more purity gaseous modulus of manufacturing method characterized is installed. According to Claim 1, in the dehydrogenation reaction conditions said oxidation process comprises the steps of: oxygen: water vapor: dilution gas=1:0. 5 - 3:0. 1 - 20:0. 1 - 20 Molar to predict the modulus of manufacturing method characterized. According to Claim 1, said condensation separation a non single stage 1, stage 2 to stage compression structure 10, the stage 1 or stage 2 to stage compression, compression modulus of 50 to 250 units characterized in manufacturing method. According to Claim 1, said condensation separation coolant used in cooling water, ethylene glycol, concentration 20 - 100% by weight aqueous solution of ethylene glycol, propylene glycol, propylene glycol concentration 30 - 100% by weight aqueous solution and propylene solvent selected from the group consisting of not more than 1 species characterized by a modulus of manufacturing method. According to Claim 1, said absorption modulation section on separated COx O2 a number n - butane, butene and butadiene are included for acquiring crude hydrocarbon solvent recovering section number portion passing butadiene or separating a deformation absorbing kiln characterized so as to further including modulus of manufacturing method. According to Claim 1, condensed in said condensation separation unit including oxide dehydrogenation reaction product hydrocarbons not absorbent separation while passing on O COx2 A separated, condensed in said condensation separation unit n - butane, butene and butadiene hydrocarbons including positive number is passed through a scrubber flow includes the step of separating said dilution gas absorption modulation section to the butadiene present separate COx O on the incombustible2 , Incombustible gas dilution number n - butane, butene and butadiene comprising hydrocarbons including discharge flow is, passing solvent recovering section to recover a solvent, said solvent recovered absorbent separating portion into mass insertion, said solvent recovering section on isolated from COx O2 On, hydrocarbons condensed in said condensation separation unit, on O de COx passed through onto the bottom surface2 The separated further, said O COx de in its base on a further be divided into2 Said absorption section and a kiln, said O COx de in its base on a further be divided into2 a number n - butane, butene and butadiene hydrocarbons included in said positive number part made of butadiene manufacturing method characterized in vitro. According to Claim 1, condensed in said condensation separation unit including oxide dehydrogenation reaction product hydrocarbons not absorbent separation while passing on O COx2 A separated, condensed in said condensation separation unit n - butane, butene and butadiene hydrocarbons including positive number is passed through a scrubber flow includes the step of separating said dilution gas absorption modulation section to the butadiene present separate COx O on the incombustible2 , Incombustible gas dilution number n - butane, butene and butadiene hydrocarbons including, passing the solvent mixture to recover a solvent recovering section, said absorption section and texture to recovered solvent, said solvent recovering section on isolated from COx O2 On hydrocarbons condensed in said condensation separation unit, on O de COx passed through onto the bottom surface2 The separated further, said O COx de in its base on a further be divided into2 a number n - butane, butene and butadiene rejection passed through high-boiling hydrocarbons included in the number crude hydrocarbons separated, said crude hydrocarbons are isolated from said high-boiling number rejection in vitro positive number part, made of a manufacturing method characterized butadiene. According to Claim 1, condensed in said condensation separation unit including oxide dehydrogenation reaction product hydrocarbons not absorbent separation while passing on O COx2 A separated, condensed in said condensation separation unit n - butane, butene and butadiene hydrocarbons including a deformation part passed through the absorbent modulation section includes the step of separating said number butadiene present separate COx incombustible gas dilution, O2 On, incombustible gas dilution number n - butane, butene and butadiene hydrocarbons including the, solvent recovering section passing to recover a solvent, said solvent into said absorption section and recovered in vitro, isolated from said solvent recovering section on O COx2 On, hydrocarbons condensed in said condensation separation unit, on O de COx passed through onto the bottom surface2 The separated further, said O COx de in its base on a further be divided into2 Said inserted into a condensation system and, at the base on a further be divided into O said COx de2 a number n - butane, butene and butadiene are included for acquiring crude hydrocarbons into said positive number made of butadiene manufacturing method characterized in vitro. According to Claim 1, condensed in said condensation separation unit including oxide dehydrogenation reaction product hydrocarbons not absorbent separation while passing on O COx2 A separated, condensed in said condensation separation unit n - butane, butene and butadiene number including a deformation part passed through the crude hydrocarbon includes the step of separating said dilution gas absorption modulation section incombustible butadiene present separate COx, O2 On, incombustible gas dilution number n - butane, butene and butadiene comprising hydrocarbons including discharge flow is, passing solvent recovering section to recover a solvent, said solvent recovered absorbent separating portion into mass insertion, said solvent recovering section on isolated from COx O2 On, said condensation separation unit comprising hydrocarbons condensed in the discharge flow, O COx passed through onto the bottom surface on de2 The separated further, said O COx de in its base on a further be divided into2 Said inserted into a condensation system and, at the base on a further be divided into O said COx de2 a number n - butane, butene and butadiene rejection passed through high-boiling hydrocarbons included in the number crude hydrocarbons separated, said crude hydrocarbons are isolated from said high-boiling number rejection in vitro positive number part, made of a manufacturing method characterized butadiene. According to Claim 1, said incombustible dilution gas is nitrogen gas (N2 ), Argon, helium or carbon dioxide (CO2 ) Characterized in modulus of manufacturing method. According to Claim 1, butene and said oxidation dehydrogenation reactor, oxygen (O2 ) On, water vapor (steam) on, said separating said positive number as residue in the texture unit n - butadiene dehydrogenation oxidation reaction using a catalyst that is butane comprise ferritic starting or under adiabatic conditions driven isothermal reaction temperature 150 provided 650 °C characterized process for manufacturing method. According to Claim 1, said direct cooler method (quencher) which can be driven in indirect cooling or quench cooling separating parts separate characterized modulus of manufacturing method. According to Claim 1, in the presence of absorbent separating parts separate COx O on said incombustible dilution gas2 Using absorption driven separating solvent characterized process for manufacturing method. According to Claim 1, said dilution gas condensation separation unit including incombustible hydrocarbons not condense during oxidation dehydrogenation reaction product group mounted on the absorbent separating characterized modulus of manufacturing method. According to Claim 1, said base or solvent recovering section de general column using stripping, or controller driven de characterized process for manufacturing method. Butene, oxygen (O2 ), Water vapor (steam) and dilution gas reacting butadiene dehydrogenation reaction material including oxide oxidation dehydrogenation products including oxidation dehydrogenation reaction; butadiene dehydrogenation reaction product including oxide for separating water from said cooling section; said water from condensing the hydrocarbons in the products of the oxidation dehydrogenation condensation separation unit; said condensation separation unit not condense hydrocarbons including oxide dehydrogenation reaction product, incombustible gas dilution in the presence COx, O2 Incombustible gas on dilution, n - butane, butene and butadiene into hydrocarbons including absorbent separating portion; and said condensation separation unit for separating condensed in the crude hydrocarbon in butadiene positive number portion; and, said positive number number n - butane gas and butene included in said signal and an analog butadiene oxidation dehydrogenation unit mounted texture, characterized in that the modulus of said dilution gas is butane tank device number. According to Claim 17, said absorption modulation section incombustible dilution gas present separate COx, O2 On, incombustible gas dilution number n - butane, butene and butadiene are included for acquiring crude hydrocarbon flow including at least one exhaust valve for supplying coolant to a number modulus of deformation characterized bath device number. According to Claim 17, said absorption modulation section incombustible dilution gas present separate COx, O2 On, incombustible gas dilution number n - butane, butene and butadiene hydrocarbons including scrubber solvent recovering section is recovering a solvent flow; and said solvent to said recovered solvent recovering section absorbent separation texture exhaust flow; characterized in including a modulus of bath device number. According to Claim 19, said solvent recovered solvent recovering section number n - butane, butene and butadiene hydrocarbons including scrubber flow COx is on O2 Separating hydrocarbons on de base; characterized in further including modulus of bath device number. According to Claim 20, said separated COx de in its base on O2 The absorbent separating portion is installed discharge flow; characterized in further including modulus of bath device number. According to Claim 20, said separated COx de in its base on O2 Condensation system is inserted into the exhaust flow; characterized in further including modulus of bath device number. According to Claim 20, de said separated at the base n - butane, butene and butadiene hydrocarbons including scrubber flow separating crude hydrocarbons is high-boiling number rejection; and said high-boiling-point number rejection isolated from crude hydrocarbon discharge is installed mechanical number part flow; characterized in further including modulus of bath device number. Tank- Mole % Wt % 1 - Butene 0. 00 0. 00 Trans - 2 - butene 43. 20 42. 77 Cis - 2 - butene 28. 80 28. 51 N - butane 28. 00 28. 72 In the embodiment Oxidation dehydrogenation unit (210) and cooling section (220) Condensation separation unit (230) and absorptive separating portion (250) Pressure (kg/cm2 G) 1. 0 0. 5 0. 1 5. 0 5. 0 4. 4 3. 0 Temperature (°C) 350 350 35 40 35 57 40 Mass flow (kg/hr) Reactant B1 B2 B3 B3 provided 1 B5 B4 + B6 Oxygen 12,203 1,945 1,945 1,915 1,915 1,945 - Nitrogen - - - - 10,000 10,000 - COx - 4,080 4,079 3,687 3,687 4,078 - water 38,167 46,375 1,250 124 124 132 - * - 3 3 3 3 3 - Carbonyl and aldehydes - 73 68 13 13 8 59 1 - Butene - 210 210 40 40 4 206 1, 3 - Butadiene - 18,755 18,755 3,672 3,672 188 18,567 N - butane 98,512 98,512 98,512 16,371 16,371 1,626 96,886 Acetylene flow - 23 23 5 5 0 23 Trans - 2 - butene 14,264 1,787 1,787 294 294 8 1,779 Cis - 2 - butene 9,510 610 610 95 95 2 608 ** High-boiling - 283 147 3 3 107 29 Toluene - - - - - 1,392 0 DMF - - - - - - - Sum-based 172,656 172,656 127,388 26,220 36,220 19,492 118,158 Oxidation dehydrogenation unit (210) and cooling section (220) Condensation separation unit (230) and absorptive separating portion (250) Pressure (kg/cm2 G) 1. 0 0. 5 0. 1 9. 7 7. 0 3. 0 Temperature (°C) 350 350 35 40 78 40 Mass flow (kg/hr) Reactant B1 B2 B3 B5 B4 + B6 Oxygen 12,203 1,945 1,945 1,828 1,945 - Nitrogen - - - - - - COx - 4,080 4,079 2,929 4,077 - water 38,167 46,375 1,250 32 47 - A light gas flow * - 3 3 2 3 - Carbonyl and aldehydes - 73 68 4 7 59 1 - Butene - 210 210 11 3 207 1, 3 - Butadiene - 18,755 18,755 981 188 18,567 N - butane 98,512 98,512 98,512 4,302 1,232 97,280 Acetylene flow - 23 23 2 0 23 Trans - 2 - butene 14,264 1,787 1,787 77 10 1,777 Cis - 2 - butene 9,510 610 610 25 2 608 ** High-boiling - 283 147 1 92 38 Toluene - - - - 628 0 DMF - - - - - - Sum-based 172,656 172,656 127,388 10,193 8,233 118,558 Oxidation dehydrogenation reactor (110) and cooling section (120) Absorbent separating portion (130) Pressure (kg/cm2 G) 1. 0 1. 0 0. 7 3. 4 3. 0 Temperature (°C) 350 350 35 44 33 Mass flow (kg/hr) Reactant B1 B2 B3 B4 Oxygen 13,013 2,757 2,757 2,757 - Nitrogen 42,855 42,855 42,855 42,855 - COx - 4,078 4,078 4,078 - water 38,156 46,363 1,250 350 306 A light gas flow (COx, O2 Such as) - 3 3 3 - Carbonyl and aldehydes - 73 68 7 60 1 - Butene - 209 209 5 205 1, 3 - Butadiene - 18,750 18,750 188 18,562 N - butane 9,575 9,575 9,575 253 9,321 Acetylene flow - 23 23 0 23 Trans - 2 - butene 14,260 1,786 1,786 10 1,776 Cis - 2 - butene 9,507 610 610 2 607 High-boiling - 283 147 91 42 Toluene - - - 3,582 0 DMF - - - - - Sum-based 127,366 127,366 82,111 54,182 30,903 In the embodiment 1 Comparison example 1 Comparison example 2 Absorption modulation section solvent usage (ton/hr) 154 51 358 Solvent recovery section absorbing energy when usage (Gcal/hr) 21. 7 14. 7 27. 6 Absorption modulation section (Mol %) oxygen concentration In the embodiment 1 Comparison example 1 Comparison example 2 B2 - - 3. 7 B3 11. 7 25. 6 4. 8 B3 provided 1 6. 9 - - B5 10. 7 31. 6 -
