Abstract:
A hybrid process comprising an adsorption process and a distillation process for the separation of butene-1 from a C4 hydrocarbon mixture gas including butene-1, trans-2-butene, cis-2-butene, normal butane, isobutane, etc. is provided. The hybrid process comprises introducing a gaseous C4 mixture into the adsorption tower loaded with adsorbents which adsorb olefins selectively to discharge C4 paraffins to the outlet of the tower, desorbing C4 olefins selectively adsorbed in the adsortion tower to produce high purity C4 olefins mixture gas in which isobutane and normal butane was removed, and separating the high C4 olefins mixture gas (a mixture of butene-1, trans-2-butene, cis-2-butene, and a trace amount of C4 paraffins) via distinction to obtain high purity butene-1 including a trace amount of isobutane in the top of the distillation tower and obtain a mixture gas including trans-2-butene, cis-2-butene and a trace amount of normal butane in the bottom of the tower.

Description:
CROSS REFERENCE TO RELATED APPLICATION 
       [0001]    This application is a division of U.S. patent application Ser. No. 12/593,252, filed on Sep. 25, 2009, the disclosure of which is incorporated by reference in its entirety for all purposes. 
     
    
     BACKGROUND 
       [0002]    1. Field 
         [0003]    The present invention relates to a method and its apparatus for the separation of butene-1 from a C4 hydrocarbon mixed gas including butene-1, trans-2-butene, cis-2-butene, normal butane, isobutane, etc. by using a hybrid process composed of an adsorption process and a distillation process. 
         [0004]    2. Description of the Related Art 
         [0005]    The known method for the separation of butene-1 from a C4 hydrocarbon mixed gas including C4 olefins (butene-1, trans-2-butene, cis-2-butene, ct.) and C4 paraffins (normal butane, isobutane, etc) involves mainly a distillation process. However, the known method requires the use of distillation towers with a large number of fractionation plates due to the small boiling-point difference of the products to be separated and thus leads to high consumption of energy and to high investment costs. 
         [0000]    
       
         
               
             
               
               
               
               
             
               
               
               
               
             
           
               
                 TABLE 1 
               
             
             
               
                   
               
               
                 Boiling point of the C4 hydrocarbon mixture 
               
             
          
           
               
                   
                 Components 
                 Molecular weight 
                 Boiling point (° C.) 
               
               
                   
                   
               
             
          
           
               
                   
                 Isobutane 
                 58.124 
                 −11.7 
               
               
                   
                 Isobutene 
                 56.108 
                 −6.9 
               
               
                   
                 Butene-1 
                 56.108 
                 −6.3 
               
               
                   
                 1,3-Butadiene 
                 54.092 
                 −4.4 
               
               
                   
                 Normal-butane 
                 58.124 
                 −0.5 
               
               
                   
                 Trans-2-butene 
                 56.108 
                 0.3 
               
               
                   
                 Cis-2-butene 
                 56.108 
                 3.7 
               
               
                   
                   
               
             
          
         
       
     
         [0006]    U.S. Pat. No. 4,718,986 (1988) discloses a process for producing butene-1 of more than 99 wt % from the C4 hydrocarbon mixture of butene-1/isobutane/normal butane/butene-2 by using two distillation towers. According to the above patent invention, the C4 mixture is introduced into the first distillation tower to remove isobutane from the top of the tower. The lower stream from the first distillation tower is introduced into the second distillation tower, obtaining butene-1 with a purity of 99 wt % from the top of the second tower and discharging a mixture of normal butane, butene-2 and butene-1 from the bottom of the second tower. However, since a considerable amount, of butene-1 is discharged with the isobutane stream from the top of the first tower and also with the mixture of normal butane, butene-2 and butene-1 from the bottom of the second tower, the above process results in much loss of butene-1. 
         [0007]    There are a number of known techniques relating to the adsorption-separation processes for a C4 hydrocarbon mixture, for example, a technique for separating butene-1 from a mixture including butene-1/butene-2/isobutylene by using type X or Y zeolite containing potassium ion or barium ion (U.S. Pat. No. 3,723,561, Mar. 27, 1973), a technique for separating butene-1 from a liquid C4 hydrocarbon mixture by using type K—X zeolite (U.S. Pat. No. 4,119,678, Oct. 10, 1978), a technique for separating normal C4 hydrocarbon mixture and isobutylene by using a molecular sieve selective to normal C4 hydrocarbon mixture (U.S. Pat. No. 4,455,445, Jun. 19, 1984), a technique for selectively separating alfa olefin alone from olefins having more than 4 carbon atoms by a liquid adsorption process using a zeolite molecular sieve (U.S. Pat. No. 5,132,485, 1992), a pressure-swing adsorption process for the separation of olefins/paraffins having 2-6 carbon atoms in vapor phase by using type 4A zeolite (U.S. Pat. No. 5,365,011, 1994), and a technique for separating paraffins from a mixture of olefins/paraffins having 2-6 carbon atoms in vapor phase using type X or Y zeolite and reproducing the adsorbents used in the adsorption process by using desorbents (BP 0708070 81, 1999). The U.S. Pat. No. 5,955,640 (1999) discloses a process of improving the yield of butene-1 by converting butene-2 components into butene-1 while removing a portion of paraffin components by using an adsorption process in order to prevent the accumulation of unreacted paraffin components in the process. 
         [0008]    However, distillation using two towers connected in series as shown in the above U.S. Pat. No. 4,718,986 (1998) is the only process used for obtaining butene-1 with high purity from the C4 ole fins/paraffins mixture gas. Till now, there is no adsorptive-separation techniques that can separate butene-1 with high purity from a mixture of C4 olefins/paraffins by selectively separating C4 olefin mixture gas from C4 olefins/paraffins mixture by an adsorption process and then obtaining high purity butene-1 from C4 olefin mixture gas selectively separated from the adsorption process by a distillation process, as can be achieved by the present invention. 
       SUMMARY 
       [0009]    The existing distillation processes for separating betene-1 from a mixture of olefins/paraffins use two sequential distillation towers to remove isobutane from the first distillation and obtain high purity butene-1 from the second distillation tower. However, a significant amount of butene-1 is discharged together with a isobutane stream to the top of the first tower and also discharged to the bottom of the second distillation tower and thus butene-1 loss is large, in addition, since the difference in relative volatilities among C4 components is small, the above distillation processes require high consumption of energy and high investment costs. 
         [0010]    In the above circumstance, the inventors of the present invention have designed a hybrid process of removing paraffins by the C4 olefins/paraffins adsorption separation process and thereafter separating the C4 olefins via distillation to obtain high purity butene-1. 
         [0011]    If olefins are selectively separated from the C4 olefins/paraffins mixture gas by using the adsorption separation process, the paraffin components are selectively removed, butene-1 loss which is accompanied at the time of removing isobutane can be reduced, also the concentration of the normal butane in the gas introduced into the distillation process for the production of high purity butene-1 is lowered, and thus the production of butene-1 is easy and the yield of butene-1 in the whole process increases. 
         [0012]    The present invention provides a method of performing a adsorption process for the adsorption of C4 olefins from a C4 olefins/paraffins mixture gas to obtain high purity C4 olefins mixture gas (a mixture gas including betene-1, trans-2-butene, cis-2-butene and a trace amount of C4 paraffins) and then performing a distillation process for the distillation separation of the obtained high purity C4 olefins mixture gas to obtain high purity butene-1 including a trace amount of isobutane in the top of the distillation tower and obtain a mixture gas including trans-2-butene, cis-2-butene and a trace amount of normal butane in the bottom of the tower, and an apparatus for practicing said method. 
         [0013]    Preferably, the present invention provides a method for production of butene-1 by separating C4 olefins from a mixture gas composed of C4 olefins/paraffins via displacement desorption with desorbents (desorption agents) and then distilling the separated C4 olefins, in an apparatus including an adsorption facility composed of three adsorption towers loaded with adsorbents which adsorb olefins selectively and two distillation towers (one distillation tower for the separation of olefins/desorbents and another distillation tower for the separation of paraffins/desorbents), and a distillation tower for obtaining butene-1 by distilling C4 olefins produced from the adsorption facility, which comprises an adsorption process including an adsorption step for introducing the mixture gas of C4 olefins/paraffins into the adsorption towers loaded with olefin selective adsorbent to adsorb olefins on the adsorbents, discharge non-adsorbed paraffins and the desorbents retained in the adsorption tower to the distillation column for separation of paraffins and the desorbents through the outlet of the adsorption tower; a C4 olefin rinse step to remove a small amount of paraffins adsorbed together with olefins on the adsorbents by introducing a portion of high purity C4 olefins resulting from the distillation process of olefins/desorbents into the adsorption tower after the completion of the adsorption step and thus increasing the purity of olefins; and a desorption step of obtaining high purity olefins by introducing desorbents into the adsorption towers after the completion of the rinse step to desorb the C4 olefins and introduce the olefins/desorbents mixture to the distillation tower for the separation of the olefins and the desorbents; and a distillation process for production of butene-1 by distilling the C4 olefins obtained in the adsorption process, wherein said sequential adsorption, olefin rinse and desorption steps are repeatedly performed in each of the adsorption towers, and wherein each adsorption towers are operated to perform the different steps with each other at the same time point. 
         [0014]    In the above method, C4 olefins/paraffins mixture gas can be firstly distilled to separate isobutane and butene-1 and discharge normal butane and butene-2 and then the resulting isobutane and butene-1 mixture can be fed into the adsorption process to obtain high purity butene-1, in place of obtaining high purity butene-1 by first processing the C4 olefins/paraffins mixture gas via the adsorption process to separate C4 olefins and then separating butene-1 from the resulting C4 olefins via the distillation process. In this ease, isobutane and butene-1 are separated as paraffins and olefins respectively by the same process as said adsorption process. 
         [0015]    The adsorption process used in the method of the present invention is a process for separating C4 olefins from a mixture gas composed of C4 olefins/paraffins by displacement desorption with desorbents (desorption agents), in a facility composed of three adsorption towers loaded with adsorbents which adsorb olefins selectively and two distillation towers (one distillation tower for the separation of olefins/desorbents and another distillation tower for the separation of paraffins/desorbents), which comprises an adsorption step for introducing the mixture gas of C4 olefins/paraffins into the adsorption towers loaded with olefin selective adsorbent to adsorb olefins on the adsorbents, discharge non-adsorbed paraffins and the desorbents retained in the adsorption tower to the distillation column for separation of paraffins and the desorbents through the outlet of the adsorption tower; a C4 olefin rinse step of cleaning a small amount of paraffins adsorbed together with olefins on the adsorbents by introducing a portion of high purity C4 olefins resulting from the distillation process of olefins/desorbents into the adsorption tower after the completion of the adsorption step and thus increasing the purity of olefins; and a desorption step of obtaining high purity olefins by introducing desorbents into the adsorption towers after the completion of the rinse step to desorb the C4 olefins and introduce the olefins/desorbents mixture to the distillation tower for the separation of the olefins and the desorbents, wherein said sequential adsorption, olefin rinse and desorption steps are repeatedly performed in each of the adsorption towers, and wherein each adsorption towers are operated to perform the different steps with each other at the same time point. 
         [0016]    The adsorption process used in the method of the present invention may carry out a sequence of adsorption step, rinse step and desorption step in a predetermined time period in more than three adsorption towers respectively in such a way that a part of the same step overlaps to each other among the towers. 
         [0017]    Preferably, the adsorption process used in the method of the present invention further includes a concurrent depressurization step of discharging the paraffin component residue present in the adsorption towers before the olefin rinse step. 
         [0018]    Also preferably, the method of the present Invention further includes a pressure equalization step at which the paraffin components present in the interior of the adsorption tower after the completion of the adsorption step is transferred to the another adsorption tower which just completed the desorption step by connecting the two adsorption towers so that the pressure of the adsorption towers becomes equalized. 
         [0019]    Also preferably, the method of the present invention further includes a concurrent de-pressurization step of discharging the paraffin components present in the adsorption towers after the pressure reduction through the pressure equalization step, and a pressurization step which pressurize the adsorption tower to the adsorption pressure by introducing the mixture gas of C4 olefins/paraffins into the adsorption tower partially pressurized through the pressure equalization step. 
         [0020]    Also preferably, olefin selective adsorbents for use in the adsorption process of the method of the present invention is π-complex adsorbent forming π-complex selectively with olefins, type X zeolite or type V zeolite, and preferably type 13X zeolite. 
         [0021]    Also preferably, the adsorbent for use in the adsorption process of the method of the present invention is C5 hydrocarbon or C6 hydrocarbon. 
         [0022]    Also preferably, in the adsorption process of the method of the present invention, the desorbent separated from the olefin/desorbent distillation tower and the paraffin/desorbent distillation tower is recirculated into adsorption tower. 
         [0023]    Also preferably, in the adsorption process of the method of the present invention, the operating pressure of the adsorption tower in the C4 olefin/paraffin separation process is 1 to 10 atm (absolute pressure) and the temperature is 20 to 150° C. 
         [0024]    The present invention also provides an adsorption facility and a distillation tower for separating butene-1 from C4 olefins discharged from the distillation tower D 2  in the adsorption facility. 
         [0025]    Preferably, the present invention provides an apparatus for the separation of butene-1 from a mixture gas of C4 olefins/paraffins by carrying out repeated sequential adsorption, olefin rinse and desorption steps to separate C4 olefins from the mixture gas of C4 olefins/paraffins in such a way of performing displacement desorption with desorbents, in an adsorption facility including three adsorption towers AD- 1 , AD- 2  and AD- 3  loaded with adsorbents which adsorb olefins selectively and two distillation towers (one distillation tower D 2  for the separation of olefins/desorbents and another distillation tower D 1  for the separation of paraffins/desorbents), and by distilling the separated C4 olefins in the distillation tower B to separate butene-1 from the C4 olefins, said apparatus comprising the adsorption tower AD- 1  in which the bottom of the tower is connected with the feeding conduit  1  for the mixture gas of C4 olefins/paraffins through the valve  1   a , with the C4 olefin/desorbent discharging conduit  2  through the valve  2   a  which is connected to the distillation tower D 2 , and with the conduit  3  through the valve  3   a  which feeds an amount of C4 olefins produced by the distillation tower D 2 , and in which the top of the tower is connected with the conduit  4  through the valve  4   a  which introduces paraffins and desorbents from the olefin rinse step into the distillation tower D 1 , with the conduit  5  through the valve  5   a  which feeds paraffins and desorbents discharged from the adsorption step into the distillation tower D 1 , and with the conduit  6  through the valve  6   a  which feeds the desorbents into the adsorption tower; the adsorption tower AD- 2  in which the bottom of the tower is connected with the feeding conduit  1  for the mixture gas of C4 olefins/paraffins through the valve  1   b , with the C4 olefin/desorbent discharging conduit  2  through the valve  2   b  which is connected to the distillation tower D 2 , and with the conduit  3  through the valve  3   b  which feeds an amount of C4 olefins produced by the distillation tower D 2 , and in which the top of the tower is connected with the conduit  4  through the valve  4   b  which introduces paraffins and desorbents from the olefin rinse step into the distillation tower D 1 , with the conduit  5  through the valve  5   b  which feeds paraffins and desorbents discharged from the adsorption step into the distillation tower D 1 , and with the conduit  6  through the valve  6   b  which feeds the desorbents into the adsorption tower; the adsorption tower AD- 3  in which the bottom of the tower is connected with the feeding conduit  1  for the mixture gas of C4 olefins/paraffins through the valve  1   c , with the C4 olefin/desorbent discharging conduit  2  through the valve  2   c  which is connected to the distillation tower D 2 , and with the conduit  3  through the valve  3   c  which feeds an amount of C4 olefins produced by the distillation tower D 2 , and in which the top of the tower is connected with the conduit  4  through the valve  4   c  which introduces paraffins and desorbents from the cleaning step into the distillation tower D 1 , with the conduit  5  through the valve  5   c  which feeds paraffins and desorbents discharged from the adsorption step into the distillation tower D 1 , and with the conduit  6  through the valve  6   c  which feeds the desorbents into the adsorption tower; the distillation tower D 1  which separates C4 paraffins and desorbents introduced from the adsorption towers AD- 1 , AD- 2  and AD- 3 ; the distillation tower D 2  which separates C4 olefins and desorbents introduced from the adsorption towers AD- 1 , AD- 2  and AD- 3 ; and the distillation tower B which separates butene-1 by distillation of the C4 olefins from the distillation tower D 2 . 
         [0026]    Preferably, the adsorption facility of the apparatus of the present invention further includes the valve  7  in the conduit  4  connected to the distillation tower D 1 . 
         [0027]    In addition, the apparatus of the present invention may include more than three adsorption towers which are adapted to carry out a sequence of adsorption step, cleaning step and desorption step in a predetermined time period in three adsorption towers respectively in such a way that a part of the same step overlaps to each other among the towers. 
     
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS  
         [0028]      FIG. 1  is a schematic view of the process of obtaining high purity butene-1 from a mixture gas of C4 olefins/paraffins according to the method of the present invention. The method of the present invention comprises a adsorption process A for separating the C4 olefins via selective adsorption and a distillation process B for producing butene-3 from the olefin components. 
           [0029]      FIG. 2  is a schematic view of the apparatus for the production of high purity butene-1 by separating the olefins from C4 olefins/paraggins mixture gas and then distilling the C4 olefins separated according to the method of the invention. 
           [0030]      FIG. 3  is a table showing a cycle sequence of the adsorption process A for selectively separating the olefins according to the method of the present invention. 
           [0031]      FIG. 4  is a schematic view of another method of the present invention comprising the hybrid process of a adsorption process A and a distillation process B. 
       
    
    
     DETAILED DESCRIPTION  
       [0032]    The detailed description of the invention with reference to the drawings is as follows. 
         [0033]      FIG. 1  is a schematic view of the process constitution for separating C4 olefins from a mixture gas of C4 olefins/paraffins according to the present invention. The process of the present invention comprises an adsorption process for separating the mixture of C4 olefins/paraffins and a distillation process for separating high purity butene-1 from the C4 olefins mixture gas separated from the adsorption process. The mixture of C4 olefins/paraffins is introduced into the adsorption process through the conduit  1 . The paraffin components which were not adsorbed on the adsorbents from the mixture of C4 olefins/paraffins is discharged through conduit  2 , and the adsorbed olefin components is desorbed by the desorbents and introduced into the distillation process B through conduit  3 . If the olefin mixture gas containing butene-1 and butene-2 together with small amount of isobutane and normal butane is introduced into the distillation process, butene-1 and isobutane having lower boiling points is discharged to the top (conduit  4 ) of the distillation tower and normal butane and butene-2 components having relatively higher boiling points is discharged to the bottom (conduit  5 ) of the distillation tower. The olefin rich mixture gas produced from the adsorption process has about 0 to 0.5 wt % level of isobutane and 0 to 5 wt % of normal butane as a much amount of isobutane and normal butane is removed. If necessary, isobutane and normal butane may be completely removed. 
         [0034]    The hybrid process of the present invention can be described with reference to  FIG. 2  including the adsorption facility composed of three adsorption towers and two distillation tower and the distillation tower B as follows. 
         [0035]    The adsorption facility used in the apparatus of the invention is a facility for the separation of C4 olefins from a mixture gas of C4 olefins/paraffins, by carrying out repeated sequential adsorption, olefin rinse and desorption steps in such a way of performing displacement desorption with the desorbents to separate C4 olefins from the mixture gas, in three adsorption towers AD- 1 , AD- 2  and AD- 3  loaded with olefin selective adsorbents and two distillation towers (one distillation tower D 2  for the separation of olefins/desorbents and another distillation tower D 1  for the separation of paraffins/desorbents), which comprises the adsorption tower AD- 1  in which the bottom of the tower is connected with the feeding conduit  1  for the mixture gas of C4 olefins/paraffins through the valve  1   a , with the C4 olefin/desorbent discharging conduit  2  through the valve  2   a  which is connected to the distillation tower D 2 , and with the conduit  3  through the valve  3   a  which feeds an amount of C4 olefins produced by the distillation tower D 2 , and in which the top of the tower is connected with the conduit  4  through the valve  4   a  which introduces paraffins and desorbents from the cleaning step into the distillation tower D 1 , with the conduit  5  through the valve  5   a  which feeds paraffins and desorbents discharged from the adsorption step into the distillation tower D 1 , and with the conduit  6  through the valve  6   a  which feeds the desorbents into the adsorption tower; the adsorption tower AD- 2  in which the bottom of the tower is connected with the feeding conduit  1  for the mixture gas of C4 olefins/paraffins through the valve  1   b , with the C4 olefin/desorbent discharging conduit  2  through the valve  2   b  which is connected to the distillation tower D 2 , and with the conduit  3  through the valve  3   b  which feeds an amount of C4 olefins produced by the distillation tower D 2 , and in which the top of the tower is connected with the conduit  4  through the valve  4   b  which introduces paraffins and desorbents from the cleaning step into the distillation tower D 1 , with the conduit  5  through the valve  5   b  which feeds paraffins and desorbents discharged from the adsorption step into the distillation tower D 1 , and with the conduit  6  through the valve  6   b  which feeds the desorbents into the adsorption tower; the adsorption tower AD- 3  in which the bottom of the tower is connected with the feeding conduit  1  for the mixture gas of C4 olefins/paraffins through the valve  1 , with the C4 olefin/desorbent discharging conduit  2  through the valve  2   c  which is connected to the distillation tower D 2 , and with the conduit  3  through the valve  3   c  which feeds an amount of C4 olefins produced by the distillation tower D 2 , and in which the top of the tower is connected with the conduit  4  through the valve  4   c  which introduces paraffins and desorbents from the cleaning step into the distillation tower D 1 , with the conduit  5  through the valve  5   c  which feeds paraffins and desorbents discharged from the adsorption step into the distillation tower D 1 , and with the conduit  6  through the valve  6   c  which feeds the desorbents into the adsorption tower; the distillation tower D 1  which separates C4 paraffins and desorbents introduced from the adsorption towers AD- 1 , AD- 2  and AD- 3 ; and the distillation tower D 2  which separates C4 olefins and desorbents introduced from the adsorption towers AD- 1 , AD- 2  and AD- 3 . 
         [0036]    The distillation tower B in the present invention is a distillation tower for separating high purity butene-1 from C4 olefin mixture gas produced from the adsorption facility. 
         [0037]      FIG. 2  is a schematic view of the apparatus of producing butene-1 from a mixture gas of C4 olefins/paraffins according to the present invention. The adsorption facility of the apparatus of the present invention comprises three adsorption towers for separating C4 olefins via selective adsorption and two distillation towers for separating C4 olefins/desorbents and C4 paraffins/desorbents respectively. The basic process of the adsorption tower used in the present invention includes an adsorption step of selectively adsorbing C4 olefins from teed, a C4 olefin rinse step of removing a small amount of C4 paraffins adsorbed together with C4 olefins; and a C4 olefin desorption step using the desorbents and the process further can includes pressure equalization step, concurrent depressurization step, and pressurization step. The desorbent discharged from the adsorption step along with olefins or paraffins is separated in the distillation tower and then recycled into the adsorption tower. The preferable desorbents is C5 hydrocarbon or C6 hydrocarbon which has a large difference in boiling point from that of the C4 mixture, 
         [0038]    A cycle operation of the adsorption process can be described with reference to  FIG. 2  on the basis of  FIG. 3  which includes the operation steps of all the preferable adsorption process as follows. 
         [0039]    The mixture gas containing C4 olefins/paraffins is introduced into the adsorption tower AD- 1  loaded with olefin selective adsorbents through the conduit  1  and valve  1   a  to adsorb C4 olefins thereon (adsorption step), and the olefin free paraffin stream separated from the mixture is introduced together with the desorbents retained in the adsorption tower before the adsorption step into the distillation tower D 1  through the conduit  5  and the valve  5   a  to separate paraffins and desorbents. The adsorption tower AD- 2  carries out the step (desorption step) of desorbing olefin components with the desorbent while the adsorption tower AD- 1  carries out the adsorption step. The desorbents used in the desorption step is obtained from the bottoms of the distillation tower D 1  and the distillation tower D 2  and is introduced into adsorption tower AD- 2  through the conduit  6  and the valve  6   b.  The olefins discharged with the desorbents is introduced into the distillation tower D 2  through the valve  2   a  and the conduit  2  to separate the olefins and the desorbents. The adsorption tower AD- 3  is provided with a portion of the olefins separated from the distillation tower D 2  through the conduit  3  and the valve  3   c  to remove a small amount of paraffins adsorbed together with the olefins for the improvement of the purity of olefins (C4 olefin rinse step). At that time, the gas discharged from the adsorption tower AD- 3  is introduced into the distillation tower D 1  through the valve  4   c  and the conduit  4 . 
         [0040]    The adsorption tower AD- 1  at high pressure which just carried out the adsorption step is connected with the adsorption tower AD- 2  at low pressure through the valve  4   a  and the conduit  4  and thus a process (pressure equalization step) that allows the pressures of both towers to be in the same pressure is carried out. During the pressure equalization step, the valve  7  is closed. The adsorption tower AD- 3  after the rinse step carries out a desorption step of recovering olefins by introducing the desorbents thereto through the conduit  6  and the valve  6   c.  The olefins discharged together with the desorbents from the adsorption tower AD- 3  is sent to the distillation tower D 2  through the valve  2   c  and the conduit  2  and thus separated from the desorbent. 
         [0041]    In addition, in the adsorption process, the adsorption tower AD- 1  after the pressure equalization step is depressurized through the valve  4   a  and the conduit  4 , and at that time, the discharged gas is introduced into the distillation tower D 1  (concurrent depressurization step). During the concurrent depressurization of the adsorption tower AD- 1 , a C4 mixture gas is introduced into the adsorption tower AD- 2  through the conduit  1  and the valve  1   b  and the adsorption tower AD- 2  carries out a step (pressurization step) of increasing the pressure to the adsorption pressure. At that time, the adsorption tower AD- 3  continues to carry out the desorption step. 
         [0042]    The adsorption tower AD- 1  which just finished the concurrent depressurization step carry out a C4 olefin rinse step, the adsorption tower AD- 2  carries out the adsorption step, and the adsorption tower AD- 3  continues to carry out the desorption step. 
         [0043]    In this way, each adsorption tower carries out a sequential adsorption step-pressure equalization step-concurrent depressurization step-C4 olefin rinse step-desorption step-pressure equalization step-pressurization step. 
         [0044]    The pressure equalization step, the concurrent depressurization step or the pressurization step can be omitted from the constitution of the process depending on the processing pressure of the adsorption step. 
         [0045]    In addition, as can be seen in  FIG. 4 , the C4 olefins/paraffins mixture gas can be firstly distilled to give isobutane/butene-1 rich stream and normal butane/butene-2 rich stream and then the resulting isobutane/butene-1 rich stream can be fed into the adsorption process to obtain high purity butene-1, in place of obtaining high purity butene-1 by first processing the C4 olefins/paraffins mixture gas via the adsorption process to separate C4 olefins and then separating butene-1 from the resulting C4 olefins via the distillation process. In this case, paraffins, i.e., isobutane and olefin, i.e., butene-1 are separated by the same process as that described in said adsorption process. 
       EXAMPLE 1 
       [0046]    As shown in FIG  1 , the C4 mixture gas (table 2) was introduced into the adsorption process to separate C4 olefins and paraffins and then the separated C4 olefins was introduced into the distillation process to produce butene-1. The adsorption process was carried out by the facility of  FIG. 2  according to the process constitutions of  FIG. 3 . With the cycle sequence as shown in  FIG. 3  by using the apparatus as shown in  FIG. 2 , an experiment for separating olefins from a mixture gas of C4 olefins/paraffins was performed while using type 13X zeolite as an adsorbent for the separation of olefins/paraffins and using C5 mixture gas as a desorbent. The compositions of the C4 mixture gas and of the C5 mixture gas were shown In table 2. The C4 mixture gas was introduced into the adsorption process at the conditions of 60° C. 2000 mmHg and the flow rate of 1675 ml/min. A portion of high purity olefin containing gas obtained from the top of the distillation D 2  as shown in  FIG. 2  was used in the C4 olefin rinse step, and the rinse flow rate was 300 ml/min. The high purity olefin containing gas obtained from the adsorption process was introduced into the distillation tower having 115-stage tray and thus obtained 99.54 wt % of butene-1 with a yield of 99.54 wt % at reflux ratio of 9. The composition of the products obtained from each of the conduits according to the method of  FIG. 1  is presented in table 3. 
         [0000]    
       
         
               
             
               
               
             
               
               
               
             
           
               
                 TABLE 2 
               
             
             
               
                   
               
               
                 Composition of C4 mixture gas and desorbents 
               
             
          
           
               
                   
                 Composition (wt %) 
               
               
                   
                   
               
             
          
           
               
                   
                 Components of mixture gas 
                   
               
               
                   
                 Iso-butane 
                 4.73 
               
               
                   
                 Normal-butane 
                 15.3 
               
               
                   
                 1-Butene 
                 50.0 
               
               
                   
                 Trans-2-butene 
                 19.0 
               
               
                   
                 Cis-2-butene 
                 10.4 
               
               
                   
                 Trace components 
                 0.57 
               
               
                   
                 Components of desorbents 
               
               
                   
                 Normal-pentane 
                 80.65 
               
               
                   
                 Iso-pentane 
                 18.69 
               
               
                   
                 Cyclopentane 
                 0.56 
               
               
                   
                 Trace components 
                 0.10 
               
               
                   
                   
               
             
          
         
       
     
         [0000]    
       
         
               
             
               
               
               
               
               
               
               
               
               
               
               
             
               
               
               
               
               
               
               
               
               
               
               
             
           
               
                 TABLE 3 
               
             
             
               
                   
               
               
                 Process performance obtained from Example 1 
               
             
          
           
               
                 Components 
                 ml/min 
                 wt % 
                 ml/min 
                 wt % 
                 ml/min 
                 wt % 
                 ml/min 
                 wt % 
                 ml/min 
                 wt % 
               
               
                   
               
             
          
           
               
                 Isobutane 
                   
                 4.73 
                   
                 21.02 
                   
                 0.16 
                   
                 0.26 
                   
                 trace 
               
               
                 Normal butane 
                   
                 15.3 
                   
                 69.97 
                   
                 2.23 
                   
                 0.06 
                   
                 5.86 
               
               
                 butene-1 
                   
                 50.0 
                   
                 6.73 
                   
                 60.52 
                   
                 99.52 
                   
                 0.72 
               
               
                 Trans-2-butene 
                   
                 19.0 
                   
                 2.27 
                   
                 22.15 
                   
                 0.15 
                   
                 58.94 
               
               
                 Cis-2-butene 
                   
                 10.4 
                   
                 0.9 
                   
                 12.90 
                   
                 1 ppm 
                   
                 34.47 
               
               
                 Total 
                 1675 
                   
                 375 
                   
                 1300 
                   
                 27.20 
                   
                 16.18 
               
               
                   
               
             
          
         
       
     
         [0047]    In order to compare the process of the present invention with the process of the existing process, the yield and the purity of the butene-1 obtained by the hybrid process composed of the adsorption process and the distillation process according to the present invention and those of butene-1 obtained only by distillation as described in U.S. Pat. No. 4,718,986 are presented in table 4. The existing distillation process comprised a series of two distillation towers and these towers had the number of stages of 120 and 115 respectively, reflux ratio of 103 and 9 (on mass basis). The number of stage of the distillation tower used in the hybrid process of the adsorption process and the distillation process was 115 and the reflux ratio was 9. The yield increased by the hybrid process according to the present invention, and also installation costs and operation costs are reduced due to the reduction of one distillation tower with a large number of stage and a high reflux ratio. 
         [0000]    
       
         
               
             
               
               
               
             
               
               
               
               
             
           
               
                 TABLE 4 
               
             
             
               
                   
               
               
                 Yield and purity by the existing process and the invented process 
               
             
          
           
               
                   
                 Yield (wt %) 
                 Purity (wt %) 
               
               
                   
                   
               
             
          
           
               
                   
                 Existing process (two 
                 91.35 
                 99.50 
               
               
                   
                 distillation tower) 
               
               
                   
                 Adsorption tower + 
                 93.00 
                 99.58 
               
               
                   
                 distillation tower 
               
               
                   
                   
               
             
          
         
       
     
         [0048]    The present invention can reduce the butene-1 loss and investment costs over the process consisted only of multi-stage distillation tower by using a hybrid process consisted of a olefins/paraffins adsorption separation process and a olefin distillation process. 
         [0049]    Now, some embodiments of the present invention are illustrated with reference to the drawings accompanied. However, it is understood that the illustrated embodiments of the present invention are intended to be examples only and the invention is not limited to any embodiments. 
         [0050]    The present invention is useful in reducing the butene-1 loss on eliminating isobutane and increasing the yield of butene-1 in the separation of butene-1 by using the hybrid process consisting of the adsorption process and the distillation process, as proved in the Examples of the present invention, since a portion of normal butane is removed together at the time of removing isobutane and thus the concentration of the normal butane introduced into the distillation tower for production of butene-1 is lowered. 
         [0051]    Although the present invention has been described with respect to the exemplary embodiments in detail, these embodiments are intended only to be illustrative of the present invention and it is apparent to those skilled in the art that a variety of modifications and changes may be made without departing from the spirit and scope of the present invention.