KR101811676B1 - Purification device for naphtha and purification method for naphtha using the same - Google Patents

Abstract

The present application relates to a naphtha refining apparatus and a naphtha refining method using the naphtha refining apparatus, which can reduce the energy consumption and efficiently increase the production amount of the object.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a naphtha purification apparatus and a purification method using the same,

The present application relates to a naphtha purification apparatus and a naphtha purification method using the same.

Naphtha is a mixture of hydrocarbons flowing out of the boiling point range of 35 to 220 ° C when crude oil is distilled, which is also known as heavy gasoline. The range of boiling point and composition This is substantially the same as gasoline oil according to the configuration of hydrocarbons. This oil is called naphtha when it is used for purposes other than the fuel of the internal combustion engine, especially for petrochemical raw materials. In a broad sense, mineral oil, which is produced when crude oil is distilled and when coal and coal are carbonized, is collectively called naphtha.

This naphtha cracking process is a process of obtaining a small molecular weight oil by pyrolysis in a cracking heater using naphtha produced by refining crude oil. It is mainly used for cracking, quenching, compressing, cold box, and separation processes. It is the main process for producing ethylene and propylene.

The present application provides a naphtha refining apparatus capable of minimizing energy consumption and efficiently increasing the production amount of a desired product, and a naphtha refining method using the same.

The present application relates to a naphtha refining apparatus. An exemplary refinement apparatus may be represented by the apparatus shown in FIG. In one example, the purification apparatus may be a purification apparatus that decomposes naphtha. The naphtha refining apparatus comprises a pyrolysis furnace for introducing naphthafide and pyrolyzing naphtha, a naphtha cracking furnace for separating n-butane and discharging a C4 LPG stream, a condensate stripper for stripping condensate, a recycle ethane stream A pyrolysis gasoline stripper into which a feed containing pyrolysis gasoline is introduced, a storage drum of the pyrolysis gasoline stripper which stores gasoline and circulates the gasoline stream, a deaerator which separates ethane and drains the acetylene stream An ethane group, a depropan group for separating n-propane, and a fuel gas drum for discharging a fuel gas stream containing methane gas. The connection relationship of each of the above structures is not particularly limited and is well known to those skilled in the art of naphtha refining processes.

In an embodiment of the present application, the refining apparatus may further include a pyrolysis fractionation distillation section, a quenching section, and a heat exchange section. In one example, the pyrolysis fractionation distillation section of the refining apparatus includes a pyrolysis fractionator 100 into which a raw material flowing out of a pyrolysis furnace is introduced, a pyrolysis fractionator 100 which pyrolyses a bottom product of the pyrolysis fractionation distillation column 100 into the pyrolysis fractionation distillation column 100 And a bypass line 108 connected to the lower portion of the pyrolysis fractionation tower 100 from an arbitrary point of the first line 107. The quenching section of the refining apparatus includes a quench water tower 101 into which the upper product of the pyrolysis fractionation tower 100 is introduced and a lower product of the quench tower 101, And a second line 109 for circulating the liquid. The heat exchanger of the refining apparatus may include a first heat exchanger installed in the first line 107 or the bypass line 108 and performing heat exchange with the bottom product of the pyrolysis fractionation tower 100 or a second heat exchanger installed in the second line And a second heat exchanger for exchanging heat of the bottom product of the quenching tower. The purification apparatus of the present application can increase the energy efficiency of the entire process by transferring the heat of the lower product of the pyrolysis fractionation column to one of the internal processes or transferring the heat of the lower product of the quenching column to the internal process.

The first heat exchanger includes a first heat exchanger 111 for exchanging a lower product of the pyrolysis fractionation tower 100 with a naphtha feed 130 and a second heat exchanger 111 installed in the bypass line 108, A second heat exchanger 112 for exchanging the lower product of the fractionation tower 100 with the lower product of the condensate stripper 102 and a second heat exchanger 112 for supplying heat to the lower part of the thermal decomposition fractionation tower 100, And a third heat exchanger (115) for exchanging the product with the lower product of the debutizer (103). The second heat exchanger includes a fifth heat exchanger 113 for exchanging the lower product of the quenching tower 101 with the feed 131 of the pyrolysis gasoline stripper 104, a quenching tower 101, A seventh heat exchanger 117 for exchanging the lower product of the quenching tower 101 with the gasoline stream 133, a second heat exchanger 117 for exchanging the lower products of the second quenching tower 101 with the gasoline stream 133, An eighth heat exchanger 118 for exchanging the lower product of the deoxidizer 101 with the lower product of the deethanizer 105 and an eighth heat exchanger 118 for exchanging the lower product of the quenching tower 101 with the product of the de- A tenth heat exchanger 120 for exchanging the lower product of the quenching tower 101 with the fuel gas stream 134 and a heat exchanger 120 for exchanging the lower product of the quenching tower 101 with the acetylene flow 135, The eleventh heat exchanger 121 and the lower product of the quenching tower 101 are connected to C4 LPG Name may include one or more selected from the group consisting of claim 12, the heat exchanger 122 to 136 and the heat exchanger.

As used herein, the term " pyrolysis furnace " means a place where pyrolysis of naphtha is performed at high temperature in the naphtha cracking process. The naphtha cracking process is a process in which naphtha among the products (naphtha, gasoline, diesel oil, kerosene, heavy oil, etc.) produced in the refining process is transferred to an naphtha cracking process by transporting the naphtha to an oil pipeline or the like, pyrolyzes the introduced naphtha at a high temperature, Propylene, butadiene, benzene, toluene, and xylene, which are basic raw materials for petrochemicals, through compression and purification processes.

The term " upper " or " lower " as used herein may mean the relative positions of distillation columns such as pyrolysis fractionation tower, quenching tower, debenzane or deethanizer described later. For example, the upper part of the pyrolysis fractionation tower may mean a position of 5 or less when the number of stages of the distillation tower is 10, and the upper product may be a product generated at 5 or less positions have. Likewise, the lower part of the pyrolysis fractionation tower may mean a position of six or more stages when the distillation tower is assumed to be ten stages, and the bottom product may mean a product produced at six or more stages.

The term " naphthafide " as used herein means a flow of a raw material containing naphtha. When the crude oil is distilled as described above, the naphtha is a mixture of hydrocarbons flowing out at a boiling point range of 35 to 220 캜 it means. In one example, the naphthafide may be introduced into the first heat exchanger via a heat exchanger that is heat-exchanged with a lower product of the quench tower flowing through the second line. The naphthafide may be a stream which flows out of a pyrolysis furnace or is introduced into a pyrolysis furnace when it is distilled.

According to the present application, the purification apparatus can circulate the bottom product of the pyrolytic fractionation column 100 through the first line 107. In this process, the heat released can be recovered to minimize the energy consumption of the entire process. In one example, the first heat exchanger 111 can transfer the heat of the bottom product of the pyrolysis fractionation tower 100 to the naphtha feed 130, thereby reusing the heat released during the cooling process of the bottom product. The bottom product of the pyrolysis fractionation column 100 may be recycled to the bottom of the pyrolysis fractionation column 100 via the bypass line 108 at any point in the first line 107. In one example, the optional point may be located before the point where the first heat exchanger 111 is installed, with respect to the flow direction of the bottom product. In this bypass line 108, the bottom product can transfer heat to the bottom product of the condensate stripper 102 through the second heat exchanger 112.

The first heat exchanger includes a third heat exchanger 115 installed in the bypass line 108 and performing a heat exchange between the lower product of the pyrolysis fractionation tower 100 and the lower product of the de-buttizer 103 .

As used herein, the term " debutane " refers to a device for the separation of light hydrocarbons below n-butane. The product flowing out from the lower portion of the debutanizer is refluxed to the debutanizer through reboiler, and the third heat exchanger can take the role of reboiler. That is, the lower product of the pyrolysis fractionation tower 100 can transfer the heat to the lower product of the de-canister so that the heat released as a whole can be recycled. On the other hand, the lower product of the debutanizer may contain pyrolysis gasoline as a main component.

As used herein, the term " main component " refers to a specific component having the largest content among the components constituting the product or the flow. For example, the content may be 40 wt% or more, 60 wt% or more, 80 wt% Or at least 95% by weight, based on the total weight of the composition.

In one example, the upper product of the pyrolytic fractionation tower 100 may be introduced into the lower portion of the quenching tower 101. The quenching tower 101 can circulate the lower product generated from the quenching tower 101 through the second line 109. In this process, the heat released can be recovered to minimize the energy consumption of the entire process.

As described above, the quenching portion of the present application may include a second heat exchanging portion. In one example, the second heat exchanger includes a fifth heat exchanger (not shown) installed in the second line 109 and for exchanging the lower product of the quenching tower 101 with the feed 131 of the pyrolysis gasoline stripper 104 113). That is, the lower product of the quenching tower 101 can transfer heat to the feed 131 of the pyrolysis gasoline stripper 104 via the fifth heat exchanger 113. On the other hand, in the present specification, the feed of pyrolysis gasoline stripper may refer to a flow comprising a pyrolysis gasoline which is discharged from a two-stage compressor suction drum and introduced into the pyrolysis gasoline stripper 104. The fifth heat exchanger may deliver heat to the feed before the feed is heat exchanged by a fourth heat exchanger described below. The lower product of the pyrolysis gasoline stripper 104 may be heat-exchanged with the feed 131 of the pyrolysis gasoline stripper 104 through the fourth heat exchanger 114, as described below.

In the embodiment of the present application, the second heat exchanger of the refining apparatus is additionally provided with a sixth heat exchanger 116 installed in the second line 109 and heat-exchanging the lower product of the quenching tower 101 with the recycle ethane stream 132 As shown in FIG. The term " recycle ethane stream " as used herein may mean a stream that circulates ethane product produced in the lower portion of a column (C2 Stripper) that generates ethylene in the upper portion, and may mean a stream introduced into the ethane recycle pyrolysis furnace. have. The second heat exchanger of the purifier may further include a seventh heat exchanger 117 installed in the second line 109 for exchanging the lower product of the quenching tower 101 with the gasoline stream 133 have. The gasoline stream 133 is a flow mainly composed of gasoline generated from the purifier of the present application and flows out from the lower storage drum of the pyrolysis gasoline stripper and is introduced into the lower storage drum of the pyrolysis gasoline stripper through the seventh heat exchanger . The second heat exchanger of the refining apparatus may further include an eighth heat exchanger 118 installed in the second line 109 for exchanging the lower product of the quenching tower 101 with the lower product of the deaerator 105, . As used herein, the term "deethanizer" means an apparatus for separating light hydrocarbons below ethane. In addition, the lower product of the deethanizer may be composed mainly of propane. As described above, the lower product of the quenching tower 101 transfers heat through the recycle stream 132, the gasoline stream 133, or the deethanizer 105, which requires heat, thereby reducing the energy of the entire process .

In another embodiment of the present application, the second heat exchanger of the purifier is installed in the second line 109 and is connected to a ninth heat exchanger (not shown) for heat exchanging the lower product of the cooling tower 101 with the product of the depropanizer 106 (119). ≪ / RTI > The product of the depropan group may be the product produced in the lower or middle portion of the depropan group. As used herein, the term " depropanizer " means an apparatus for separating light hydrocarbons below n-propane. The product of the above depro- phan group is a stream which flows out from the lower part of the depro- phan group and is refluxed to the lower part of the depro- pan group, and can be mainly composed of butane. The second heat exchanger of the purifier may further include a tenth heat exchanger 120 installed in the second line 109 and performing heat exchange with the bottom product of the quenching tower 101 with the fuel gas stream 134 May be further included. The fuel gas stream 134 is a stream that flows out of the fuel gas drum and is introduced into a gas turbine generator, and may include methane gas as a main component. The second heat exchanger of the refining apparatus may further include an eleventh heat exchanger 121 installed in the second line 109 for exchanging the lower product of the quenching tower 101 with the acetylene flow 135 have. The acetylene stream 135 flows from the top of the deethanizer 105 and is introduced into the acetylene converter, and may contain ethane as a main component. The second heat exchanger of the purifier may further include a twelfth heat exchanger 122 installed in the second line 109 for exchanging the lower product of the quenching tower 101 with the C4 LPG stream 136 . The C4 LPG stream 136 may refer to the flow through which the C4 mixture coming from the lower portion of the debut unit 103 of the naphtha cracking process is discharged through the hydrogenation process. The C4 LPG stream 136 may be returned to the lower portion of the deburring unit 103, and may be C4 LPG as a main component. As described above, the lower product of the quenching tower 101 transfers heat to the desopropane 106, the fuel gas stream 134, the acetylene stream 135, or the C4 LPG stream 136 requiring heat, The energy of the process can be saved.

The refining apparatus of the present application may include a pyrolysis gasoline stripper 104 that introduces a feed 131 of a pyrolysis gasoline stripper 104 and introduces the overhead product into the lower portion of the quenching tower 101, have. And a fourth heat exchanger 114 for exchanging the lower product of the pyrolysis gasoline stripper 104 with the feed 131 of the pyrolysis gasoline stripper 104. The feed 131 must be sufficiently preheated before it is introduced into the stripper 104 so that the hot bottom product of the pyrolysis gasoline stripper 104 will transfer heat to preheat the feed 131, 131 can be reduced.

The term " stripper " as used herein refers to a device used for this operation in which the operation of transferring gas or vapor dissolved in a liquid into the vapor phase is referred to as stripping. The term " condensate " as used herein means a liquid hydrocarbon mixture obtained by condensing a gas mixture to condense high-boiling substances by physical phase change by compressing and cooling the gas mixture. In one example, the condensate stripper of the present application can be used for the purpose of lowering the vapor pressure by blowing low-boiling substances contained in a liquid hydrocarbon mixture obtained through a condensing process.

As used herein, the term " feed of a pyrolysis gasoline stripper " may refer to a pyrolysis gasoline stream introduced into a pyrolysis gasoline stripper.

As described above, the lower product of the quenching tower 101 of the present application can be circulated to the upper portion of the quenching tower 101 through the second line 109. The quenching apparatus may further include a quench water separating drum 110. The quenching water separating drum 110 separates a part of the lower product of the quenching tower 101 into the upper part of the pyrolysis fractionating tower 100 And the other part can be circulated to the upper part of the quenching tower 101 through the second line 109.

The present application also relates to a method for purifying naphtha. The above purification method can be used for the purification method. In one example, the purification method includes: introducing a raw material discharged from a thermal decomposition furnace into a thermal decomposition fractionation tower 100; Circulating the bottom product of the pyrolysis fractionation tower through the first line to the top of the pyrolysis fractionation tower and circulating the bottom product through the bypass line to the bottom of the pyrolysis fractionation tower; Introducing the upper product of the pyrolysis fractionation tower (100) into the quenching tower (101); Circulating the lower product of the quenching tower (101) to the upper part of the quenching tower (101) through the second line (109); And a step of heat-exchanging the lower product of the pyrolysis fractionation tower 100 through the first heat exchange unit or heat-exchanging the lower product of the quenching tower 101 through the second heat exchange unit.

In one example, the refining process comprises introducing a feed of a pyrolysis gasoline stripper into a pyrolysis gasoline stripper, introducing the pyrolysis gasoline stripper overhead product into the lower portion of the quench tower, and introducing the bottom product of the pyrolysis gasoline stripper into a fourth And heat exchanging the feed with the feed of the pyrolysis gasoline stripper through a heat exchanger.

According to the present application, the purification process can circulate the bottom product of the pyrolytic fractionation column 100 through the first line 107. As described above, the first heat exchanger may include at least one selected from the group consisting of a first heat exchanger, a second heat exchanger, and a third heat exchanger. In addition, the second heat exchanger may include at least one selected from the group consisting of fifth to twelfth heat exchangers. In the circulation process, the heat released can be recovered to minimize the energy consumption of the entire process. In one example, the first heat exchanger 111 can transfer the heat of the bottom product of the pyrolysis fractionation tower 100 to the naphtha feed 130, thereby reusing the heat released during the cooling process of the bottom product. The bottom product of the pyrolysis fractionation column 100 may be recycled to the bottom of the pyrolysis fractionation column 100 via the bypass line 108 at any point in the first line 107. In this bypass line 108, the bottom product can transfer heat to the bottom product of the condensate stripper 102 through the second heat exchanger 112.

In one example, the upper product of the pyrolytic fractionation tower 100 may be introduced into the lower portion of the quenching tower 101. The quenching tower 101 can circulate the lower product generated from the quenching tower 101 through the second line 109. In this process, the heat released can be recovered to minimize the energy consumption of the entire process. In one example, the bottom product of the quenching tower 101 may transfer heat to the feed 131 of the pyrolysis gasoline stripper 104 via a fifth heat exchanger 113. The bottom product of the pyrolysis gasoline stripper 104 may also be heat exchanged with the feed 131 of the pyrolysis gasoline stripper 104 through a fourth heat exchanger 114.

In the embodiment of the present application, the bottom product of the pyrolysis fractionation column 100 is passed through the reflux flow rate V1 through the bypass line 108 and the first line 107, which is not the bypass line 108, The ratio V1 / V2 of the flow rate V2 may be 0.2 to 0.5, 0.25 to 0.48, 0.3 to 0.45, 0.35 to 0.43, or 0.4 to 0.43. By limiting the ratio of the flow rate, the energy efficiency of the entire process can be increased.

In one example, the temperature T1 of the bottom product of the pyrolysis fractionation distillation column 100 before the introduction into the first heat exchanger 111 and the temperature T1 of the pyrolysis fractionation distillation column 100 after passing through the first heat exchanger 111 (T1 '/ T1) of the temperature (T1') of the lower product of the bottom product of the reaction product (A) may be 0.5 to 0.99, 0.6 to 0.98, 0.7 to 0.97 or 0.8 to 0.97. The temperature T2 of the bottom product of the pyrolysis fractionation distillation column 100 before introduction into the second heat exchanger 112 and the temperature of the bottom product of the pyrolysis fractionation column 100 after passing through the second heat exchanger 112 T2 ') may be 0.5 to 0.99, 0.6 to 0.97, 0.7 to 0.95, or 0.8 to 0.93. As described above, the temperature of the bottom product of the pyrolysis fractionation tower 100 is controlled at the above ratio, so that the heat source of the bottom product can be efficiently transferred to the bottom product of the naphthafide 130 or the condensate stripper 102 The purification method of the present application is characterized in that the temperature T3 of the lower product of the quenching tower 101 before being introduced into the fifth heat exchanger 113 and the temperature T3 of the lower product after passing through the fifth heat exchanger 113 The ratio (T3 '/ T3) of the temperature T3' of the lower product of the cooling tower 101 can be controlled to 0.5 to 0.99, 0.6 to 0.97, 0.7 to 0.95, or 0.8 to 0.95. The temperature T4 of the feed 131 of the pyrolysis gasoline stripper 104 before being introduced into the fourth heat exchanger 114 and the temperature T4 of the pyrolysis gasoline stripper 104 after passing through the fourth heat exchanger 114 1.3 to 1.9, 1.4 to 1.8, 1.5 to 1.7, or 1.5 to 1.6, of the temperature (T4 '/ T4) As described above, the temperature of the lower product of the quenching tower 101 is controlled at the above ratio, so that the heat source of the lower product can be efficiently transferred to the feed 131 of the pyrolysis gasoline stripper 104.

The purification apparatus and the purification method according to the present application can reduce the energy consumption in the purification process and can efficiently increase the production amount of the object.

1 is a view showing a purification apparatus of the present application.

Hereinafter, the present invention will be described in more detail by way of examples according to the present application (examples of maximally saving energy consumption), but the scope of the present invention is not limited by the following embodiments.

That is, it is apparent to those skilled in the art that the scope of the present application is not limited to the embodiments described below, and various modifications and changes may be made without departing from the spirit and scope of the present invention. Accordingly, such modifications or variations are intended to fall within the scope of the appended claims.

Example  One

A purification apparatus as shown in Fig. 1 was used. The amount of reflux from the quench water separating drum 110 to the upper portion of the pyrolysis fractionation distillation column 100 was set at 150 tons / hour when the amount of the raw material flowing out of the pyrolysis furnace 100 into the pyrolysis fractionation tower 100 was 509.8 tons / And operated under the conditions shown in Tables 1 to 12 below. The annual production of ethylene is 103 KTA.

Example  2

The amount of reflux from the quench water separating drum 110 to the upper portion of the pyrolysis fractionation distillation column 100 was set at 170 tons / hour when the amount of the raw material flowing out of the pyrolysis furnace 100 into the pyrolysis fractionation tower 100 was 630.5 tons / , The purification apparatus of the present application was operated in the same manner as in Example 1. As a result, The annual production of ethylene is 111 KTA.

In the following Tables 1 to 12, the lower product of the thermal decomposition fractionation column is referred to as Quench Oil, and the lower product of the quenching tower is referred to as Quench Water. The temperature (Temp, C) is expressed in ° C, and the flow rate (Flow, T / h) is expressed in units of ton / hour.

Additional devices Example 1 Example 2 The first heat exchanger In Out In Out Temp (C) Flow (T / h) Temp (C) Temp (C) Flow (T / h) Temp (C) Naphtha feed 66.5 93.4 103.1 64.4 164.4 101.2 Quench Oil 135.5 824.2 130.2 135.5 824.2 126.5 Duty 2.0 MMKcal / h 3.52 MMKcal / h Reduced Duty 2.0 MMKcal / h 3.52 MMKcal / h Saving Fuel 167 kg / h 294 kg / h

Additional devices Example 1 Example 2 The second heat exchanger In Out In Out Temp. (C) Flow (T / h) Temp. (C) Temp. (C) Flow (T / h) Temp. (C) Condensate 121.3 Circulation 121.3 121.3 Circulation 121.3 Quench Oil 159.7 350 146.4 159.7 350 146.6 Duty 2.36 MMKcal / h 2.36 MMKcal / h Reduced Duty 2.36 MMKcal / h 2.36 MMKcal / h Reduced steam 4155 kg / h 4155 kg / h

In Table 2 above, Condensate refers to the bottom product stream of the condensed stream stripper.

Additional devices Example 1 Example 2 The third heat exchanger In Out In Out Temp. (C) Flow (T / h) Temp. (C) Temp. (C) Flow (T / h) Temp. (C) DeC4 Btm 97.8 Circulation 101 97.8 Circulation 101 Quench Oil 146.4 350 132.8 146.6 350 124.8 Duty 2.37 MMKcal / h 3.8 MMKcal / h Reduced Duty 2.37 MMKcal / h 3.8 MMKcal / h Reduced steam 4650 kg / h 7450 kg / h

In Table 3 above, DeC4 Btm means the bottom product stream of the debutanizer.

Additional devices Example 1 Example 2 The fourth heat exchanger In Out In Out Temp. (C) Flow (T / h) Temp. (C) Temp. (C) Flow (T / h) Temp. (C) Feed 43.2 66.9 66.4 43.2 66.9 66.4 Bottom 90 64.9 66.4 90 64.9 66.4 Duty 0.637 MMKcal / h 0.637 MMKcal / h Reduced Duty 0.637 MMKcal / h 0.637 MMKcal / h Reduced steam 1237 kg / h 1237 kg / h

In Table 4, Feed is the feed of the pyrolysis gasoline stripper and Bottom is the bottom product stream of the pyrolysis gasoline stripper.

Additional devices Example 1 Example 2 The fifth heat exchanger In Out In Out Temp. (C) Flow (T / h) Temp. (C) Temp. (C) Flow (T / h) Temp. (C) PG Feed 43.7 62.1 68.3 43.2 66.9 69.2 Quench Water 72 187.3 68.3 87.3 43.4 69.2 Duty 0.69 MMKcal / h 0.79 MMKcal / h Reduced Duty 0.86 MMKcal / h 1.08 MMKcal / h Reduced steam 1670 kg / h 2110 kg / h

In Table 5, the PG Feed means a feed of pyrolysis gasoline stripper.

Additional devices Example 1 Example 2 The sixth heat exchanger In Out In Out Temp. (C) Flow (T / h) Temp. (C) Temp. (C) Flow (T / h) Temp. (C) C2 Recycle 12 27.2 30.6 12 27.2 30.6 Quench Water 72 50 68.2 66.9 50 65.2 Duty 0.22 MMKcal / h 0.22 MMKcal / h Reduced Duty 0.22 MMKcal / h 0.22 MMKcal / h Saving Fuel 18.3 kg / h 18.3 kg / h

In Table 6, C2 Recycle means recycled ethane flow.

Additional devices Example 1 Example 2 Seventh heat exchanger In Out In Out Temp. (C) Flow (T / h) Temp. (C) Temp. (C) Flow (T / h) Temp. (C) Wash Gasoline 42 38 63 42 38 63 Quench Water 72 95.1 68.2 66.9 172.3 65.2 Duty 0.37 MMKcal / h 0.37 MMKcal / h Reduced Duty 0.37 MMKcal / h 0.37 MMKcal / h Reduced steam 726 kg / h 726 kg / h

In Table 7, Wash Gasoline means gasoline flow.

Additional devices Example 1 Example 2 The eighth heat exchanger In Out In Out Temp. (C) Flow (T / h) Temp. (C) Temp. (C) Flow (T / h) Temp. (C) DeC2 IR 59.7 116.4 64.4 59.7 67.8 64.4 Quench Water 87 260 78.5 87.3 141.9 78 Duty 2.25 MMKcal / h 1.31 MMKcal / h Reduced Duty 0.95 MMKcal / h 0MMKcal / h Reduced steam 1830 kg / h 0 kg / h

In Table 8 above, DeC2 IR means the bottom product stream of the deethanizer.

Additional devices Example 1 Example 2 The ninth heat exchanger In Out In Out Temp. (C) Flow (T / h) Temp. (C) Temp. (C) Flow (T / h) Temp. (C) DeC3 IR 47.4 149.6 52.4 47.4 129.8 52.4 Quench Water 87 150 64.5 87.3 113.5 61.4 Duty 3.4 MMKcal / h 2.95 MMKcal / h Reduced Duty 1.12 MMKcal / h 1.23 MMKcal / h Reduced steam 2120 kg / h 2330 kg / h

In Table 9 above, DeC3 IR means the depropanizer product stream.

Additional devices Example 1 Example 2 The tenth heat exchanger In Out In Out Temp. (C) Flow (T / h) Temp. (C) Temp. (C) Flow (T / h) Temp. (C) Fuel Gas 56 61.8 78.1 56 69.7 74.1 Quench Water 87 58.9 78.1 87.3 45 74.1 Duty 0.53 MMKcal / h 0.598 MMKcal / h Reduced Duty 0.53 MMKcal / h 0.598 MMKcal / h Reduced steam 1040 kg / h 1170 kg / h

In Table 10, Fuel Gas means fuel gas flow.

Additional devices Example 1 Example 2 The eleventh heat exchanger In Out In Out Temp. (C) Flow (T / h) Temp. (C) Temp. (C) Flow (T / h) Temp. (C) Ac.Feed 35 141.7 39.3 35 153.9 39.4 Quench Water 77.5 60 65.1 75.5 12 50.1 Duty 0.28 MMKcal / h 0.3 MMKcal / h Reduced Duty 0.28 MMKcal / h 0.3 MMKcal / h Reduced steam 549 kg / h 588 kg / h

In Table 11, Ac.Feed means acetylene flow.

Additional devices Example 1 Example 2 The twelfth heat exchanger In Out In Out Temp. (C) Flow (T / h) Temp. (C) Temp. (C) Flow (T / h) Temp. (C) C4 LPG 20 50 60 20 50 60 Quench Water 72 385.6 68.2 66.9 223.3 60.2 Duty 1.5 MMKcal / h 1.5 MMKcal / h Reduced Duty 1.5 MMKcal / h 1.5 MMKcal / h Saving Fuel 125 kg / h 125 kg / h

In Table 12, C4 LPG means C4 LPG flow.

Additional devices Reduction Duty (MMKcal / h) Reduced steam
(kg / h) Saving Fuel
(kg / h) The first heat exchanger 2.0 - 167 The second heat exchanger 2.36 4155 - The third heat exchanger 2.37 4650 - The fourth heat exchanger 0.637 1237 - The fifth heat exchanger 0.86 1670 - The sixth heat exchanger 0.22 - 18.3 Seventh heat exchanger 0.37 726 - The eighth heat exchanger 0.95 1830 - The ninth heat exchanger 1.12 2120 - The tenth heat exchanger 0.53 1040 - The eleventh heat exchanger 0.28 549 - The twelfth heat exchanger 1.5 - 125 Sum 13.197 17977 310.3

Table 13 summarizes the energy saving contents of the first embodiment.

Additional devices Reduction Duty (MMKcal / h) Reduced steam
(kg / h) Saving Fuel
(kg / h) The first heat exchanger 3.52 - 294 The second heat exchanger 2.36 4155 - The third heat exchanger 3.8 7450 - The fourth heat exchanger 0.637 1237 - The fifth heat exchanger 1.08 2110 - The sixth heat exchanger 0.22 - 18.3 Seventh heat exchanger 0.37 726 - The eighth heat exchanger 0 0 - The ninth heat exchanger 1.23 2330 - The tenth heat exchanger 0.598 1170 - The eleventh heat exchanger 0.3 588 - The twelfth heat exchanger 1.5 - 125 Sum 15.615 19766 437.3

Table 14 summarizes the energy saving contents of the first embodiment.

Sum Example 1 Example 2 Reduced Duty 13.467 MMKcal / h 15.897 MMKcal / h Reduced steam 17977 kg / h 19766 kg / h Saving Fuel 310 kg / h 437 kg / h

100: pyrolysis fractionation tower
101: Cooling tower
102: Condensate stripper
103:
104: Pyrolysis gasoline stripper
105: Deethanizer
106: depropanizer
107: Line 1
108: Bypass line
109: Line 2
110: quenched water separation drum
111: first heat exchanger
112: second heat exchanger
113: fifth heat exchanger
114: fourth heat exchanger
115: third heat exchanger
116: Sixth heat exchanger
117: seventh heat exchanger
118: the eighth heat exchanger
119: Ninth heat exchanger
120: the tenth heat exchanger
121: eleventh heat exchanger
122: twelfth heat exchanger
130: naphtha feed
131: feed of pyrolysis gasoline stripper
132: Recycled ethane flow
133: Gasoline flow
134: fuel gas flow
135: Acetylene flow
136: C4 LPG flow

Claims (12)

A pyrolysis furnace that introduces naphthafide to pyrolyze naphtha, a debutizer separating n-butane and discharging the C4 LPG stream, a condensate stripper stripping the condensate, a C2 stripper discharging the recycled ethane stream, and pyrolysis gasoline A storage drum of the pyrolysis gasoline stripper for circulating a gasoline stream, a deethanizer for separating ethane and discharging the acetylene stream, a depropanizer for separating n-propane, and methane gas A naphtha refining apparatus comprising a fuel gas drum for discharging a fuel gas stream,
A pyrolytic fractionation tower into which the raw material flowing out of the pyrolysis furnace is introduced, a first line circulating the lower product of the pyrolysis fractionation tower above the pyrolysis fractionation tower, and a second line circulating the pyrolysis fractionation tower through the pyrolysis fractionation tower A pyrolytic fractionation distillation unit comprising a bypass line connected to the lower portion;
A quenching unit including a quenching tower to which the upper product of the pyrolysis fractionation tower is introduced and a second line for circulating the lower product of the quenching tower to the upper part of the quenching tower;
A quench water separation drum for circulating a part of the bottom product of the quenching tower to the upper portion of the pyrolysis fractionation column and the other part of the quenched water to circulate through the second line to the top of the quenching tower; And
A first heat exchange unit installed in the first line or the bypass line for heat-exchanging the lower products of the pyrolysis fractionation tower or a second heat exchange unit installed in the second line and performing heat exchange of the lower products of the quenching tower, Including,
The first heat exchanger includes a first heat exchanger for exchanging the lower product of the pyrolysis fractionation column with the naphtha feed, a second heat exchanger installed in the bypass line for heat exchange the lower product of the pyrolysis fractionation distillation column with the lower product of the condensation stripper, A second heat exchanger and a third heat exchanger installed in the bypass line for exchanging the lower product of the pyrolysis fractionation tower with the lower product of the de-buttizer,
The second heat exchanger includes a fifth heat exchanger for exchanging the lower product of the quenching tower with the feed of the pyrolysis gasoline stripper, a sixth heat exchanger for exchanging the lower product of the quenching tower with the recycle ethane flow, An eighth heat exchanger for exchanging a lower product of the quenching tower with a lower product of the deethanizer, a heat exchanger for exchanging a lower product of the quenching tower with a product of the desopropane, A ninth heat exchanger, a tenth heat exchanger for exchanging the lower product of the quenching tower with the fuel gas flow, an eleventh heat exchanger for exchanging the lower product of the quenching tower with the acetylene stream, And a twelfth heat exchanger for exchanging heat with the C4 LPG stream. Refining apparatus hereinafter. The apparatus of claim 1, wherein the pyrolysis gasoline stripper introduces the overhead product of the pyrolysis gasoline stripper into the lower portion of the quenching tower. The purification system of claim 1, comprising a fourth heat exchanger to heat exchange the bottom product of the pyrolysis gasoline stripper with the feed of the pyrolysis gasoline stripper. delete Introducing the raw material discharged from the pyrolysis furnace into the pyrolysis fractionation tower; Circulating the bottom product of the pyrolysis fractionation tower through the first line to the top of the pyrolysis fractionation tower and circulating the bottom product through the bypass line to the bottom of the pyrolysis fractionation tower; Introducing the upper product of the pyrolysis fractionation tower into a quenching tower; Circulating the lower product of the quenching tower to the upper portion of the quenching tower through the second line; And a step of heat-exchanging the lower product of the pyrolysis fractionation column through the first heat exchange unit or heat-exchanging the lower product of the quenching column through the second heat exchange unit. 6. The method according to claim 5, wherein the ratio (V1 / V2) of the flow rate (V1) of the bottom product of the thermal decomposition fractionation tower through the bypass line to the flow rate (V2) 0.2 to 0.5. [6] The apparatus of claim 5, wherein the first heat exchanger comprises a first heat exchanger for exchanging the lower product of the pyrolysis fractionation column with naphtha feed, a second heat exchanger installed in the bypass line, and a lower product of the pyrolysis fractionation column, A second heat exchanger for heat exchange and a third heat exchanger installed at the bypass line and for exchanging the lower product of the pyrolysis fractionation tower with the lower product of the de-buttizer. 6. The method of claim 5, wherein the second heat exchanger comprises a fifth heat exchanger for exchanging the lower product of the quenching tower with the feed of the pyrolysis gasoline stripper, a sixth heat exchanger for exchanging the lower product of the quenching tower with the recycle ethane stream, An eighth heat exchanger for exchanging the lower product of the quenching tower with the lower product of the deacetomer, a heat exchanger for exchanging the lower product of the quenching tower with the product of the depro- phan group, a seventh heat exchanger for heat- A ninth heat exchanger, a tenth heat exchanger for exchanging the lower product of the quenching tower with the fuel gas flow, an eleventh heat exchanger for exchanging the lower product of the quenching tower with the acetylene stream, and a C4 LPG flow And a twelfth heat exchanger for exchanging heat with the second heat exchanger. The method according to claim 7, wherein the ratio (T1 '/ T1 (T1)) of the temperature (T1) of the lower product of the pyrolysis fractionating distillation column before introduction into the first heat exchanger to the temperature ) Is from 0.5 to 0.99. The method according to claim 7, wherein the ratio (T2 '/ T2 (T2)) of the temperature (T2) of the lower product of the pyrolysis fractionation distillation column before introduction into the second heat exchanger and the temperature (T2') of the lower product of the pyrolysis fractionation distillation column after passing through the second heat exchanger ) Is from 0.5 to 0.99. 6. The method of claim 5, further comprising introducing a feed of a pyrolysis gasoline stripper into a pyrolysis gasoline stripper, introducing the overhead product of the pyrolysis gasoline stripper into a lower portion of the quench tower, and introducing the bottom product of the pyrolysis gasoline stripper into a fourth heat exchanger And heat-exchanging the feed with the feed of the pyrolysis gasoline stripper. 12. The method of claim 11, wherein the ratio (T4 '/ T4) of the temperature (T4) of the feed of the pyrolysis gasoline stripper prior to introduction into the fourth heat exchanger to the temperature of the feed of the pyrolysis gasoline stripper after passing through the fourth heat exchanger (T4' Is 1.2 to 2.0.

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