Optimization system for producing isobutene through butene isomerization

Abstract

The utility model discloses an optimization system for producing isobutene through butene isomerization. The optimization system comprises a feeding and discharging heat exchanger, a heating furnace, an isomerization reactor system, a gas-liquid separation tank, a compressor and a separation system, mixed C4 exchanges heat through a feeding and discharging heat exchanger, the feeding and discharging heat exchanger is communicated with a heating furnace, the heating furnace is communicated with an isomerization reactor system, the isomerization reactor system is communicated with the feeding and discharging heat exchanger, the feeding and discharging heat exchanger is communicated with a gas-liquid separation tank, a gas phase of the gas-liquid separation tank is communicated with an inlet of a compressor, and an outlet of the compressor is communicated with a separation system. A liquid phase of the gas-liquid separation tank is communicated with the separation system, and the separation system outputs an isobutene product. The method has the beneficial effects that the isomerization reaction part and the regeneration part are improved and optimized, so that the production process is simplified, and the energy consumption and the operation energy consumption are reduced.

Description

TECHNICAL FIELD

[0001] The utility model belongs to the technical field of butene isomerization production isobutene, especially relates to a butene isomerization production isobutene's optimization system. BACKGROUND

[0002] Isobutene is an important chemical raw material, and has a wide range of applications. It can be used to produce methyl tert-butyl ether (MTBE), which is a high-octane fuel additive that can improve the anti-knock performance of gasoline; it is a key raw material for producing butyl rubber, which is widely used in manufacturing inner tubes, pipeline seals, etc.; it is an important intermediate for producing ketone (MEK), isobutyl acetate, isobutyl benzene, allyl acetate and other chemical products; in the pharmaceutical field, derivatives of isobutene are used to synthesize medicines such as vitamin E and A.

[0003] As an important chemical raw material, the production cost of isobutene has been under pressure in recent years. Downstream products (such as MTBE) are greatly affected by the market, and the price fluctuates. To ensure stable market supply, it is necessary to reduce the production cost of isobutene and reduce the production energy consumption. Currently, the device for producing isobutene by isomerization of n-butane adopts three reactors, two open and one standby, which are switched according to the production situation. Two reactors are in reaction, and one reactor is in regeneration.

[0004] In the prior art, each reactor is equipped with an inlet and outlet heat exchanger and a heating furnace, which increases the equipment investment cost. Since the heating furnace needs to consider the driving condition, its design capacity is large, the actual running efficiency is low, and the running energy consumption is high. UTILITY MODEL CONTENTS

[0005] Therefore, the utility model aims to provide a butene isomerization production isobutene optimization system to solve at least one technical problem in the background art.

[0006] To achieve the above-mentioned purpose, the technical scheme of the utility model is as follows:

[0007] A butene isomerization production isobutene optimization system, comprising an inlet and outlet heat exchanger, a heating furnace, an isomerization reactor system, a gas-liquid separation tank, a compressor and a separation system. The mixed carbon four is heated by the inlet and outlet heat exchanger, the inlet and outlet heat exchanger is communicated with the heating furnace, the heating furnace is communicated with the isomerization reactor system, the isomerization reactor system is communicated with the inlet and outlet heat exchanger, the inlet and outlet heat exchanger is communicated with the gas-liquid separation tank, the gas phase of the gas-liquid separation tank is communicated with the inlet of the compressor, the outlet of the compressor is communicated with the separation system, the liquid phase of the gas-liquid separation tank is communicated with the separation system, and the separation system outputs isobutene products.

[0008] Further, the regeneration system is in communication with a regeneration heat exchanger, the regeneration heat exchanger is in communication with an electric heater, and the electric heater is in communication with the isomerization reactor system; the isomerization reactor system is in communication with the regeneration heat exchanger, the regeneration heat exchanger is in communication with a regeneration cooler, and the regeneration cooler is in communication with the regeneration system.

[0009] Further, the regeneration system is in communication with nitrogen and air.

[0010] Further, the isomerization reactor system comprises a plurality of first isomerization reactors and a plurality of second isomerization reactors, the heating furnace is in communication with the plurality of first isomerization reactors and the plurality of second isomerization reactors respectively, and the plurality of first isomerization reactors and the plurality of second isomerization reactors are in communication with the feed and discharge heat exchanger respectively.

[0011] The second isomerization reactor is a standby isomerization reactor.

[0012] The first isomerization reactor is in reaction, and the second isomerization reactor is switched among reaction, regeneration and standby states constantly, and the second isomerization reactor is switched to the first isomerization reactor with the reaction process.

[0013] Further, the isomerization reactor system comprises a plurality of first isomerization reactors and a plurality of second isomerization reactors, the plurality of first isomerization reactors and the plurality of second isomerization reactors are in communication with the regeneration heat exchanger respectively, and the electric heater is in communication with the plurality of first isomerization reactors and the plurality of second isomerization reactors respectively.

[0014] Further, a cooler is arranged between the feed and discharge heat exchanger and the gas-liquid separation tank.

[0015] Further, a pump is arranged between the gas-liquid separation tank and the separation system.

[0016] Compared with the prior art, the optimization system for producing isobutene by butene isomerization has the following advantages:

[0017] 1. The application reduces the number of equipment and reduces the investment cost.

[0018] 2. The application simplifies the production process.

[0019] 3. The application reduces heat loss, improves equipment efficiency, improves energy utilization rate, and reduces energy consumption. BRIEF DESCRIPTION OF DRAWINGS

[0020] The drawings constituting a part of the present application are used to provide a further understanding of the present application, and the schematic embodiments of the present application and the description thereof are used to explain the present application, and do not constitute an improper limitation on the present application. In the drawings:

[0021] Figure 1The flow chart of the optimization system for butene isomerization production of isobutene according to the utility model embodiment 1 or embodiment 2.

[0022] Figure 2 The flow chart of the optimization system for butene isomerization production of isobutene according to the utility model comparative example 1.

[0023] Explanation of reference signs:

[0024] Inlet and outlet heat exchanger; 2, heating furnace; 3, gas-liquid separation tank; 4, compressor; 5, separation system; 6, regeneration heat exchanger; 7, regeneration system; 8, first isomerization reactor; 9, second isomerization reactor; 10, electric heater; 11, regeneration cooler; 12, comparative cooler; 13, cooler; 14, pump; 15, comparative regeneration system; 16, comparative gas-liquid separation tank; 17, comparative compressor; 18, comparative separation system; 19, comparative pump; 20, comparative inlet and outlet heat exchanger; 21, comparative heater; 22, comparative isomerization reactor. DETAILED DESCRIPTION

[0025] It should be noted that the embodiments in the utility model and the features in the embodiments can be combined with each other without conflict.

[0026] In the description of the utility model, it should be understood that the orientation or position relationship indicated by the terms "center", "longitudinal", "transverse", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer" and the like is based on the orientation or position relationship shown in the drawings, and is only for the convenience of describing the utility model and simplifying the description, and therefore cannot be understood as indicating or implying that the devices or elements indicated must have a particular orientation, be constructed and operated in a particular orientation, and therefore cannot be understood as limiting the utility model. In addition, the terms "first", "second" and the like are only for the purpose of description, and cannot be understood as indicating or implying relative importance or implicitly indicating the number of the technical features indicated. Therefore, the features limited by "first", "second" and the like can explicitly or implicitly include one or more features. In the description of the utility model, unless otherwise specified, the meaning of "a plurality of" is two or more.

[0027] In the description of the utility model, it should be noted that, unless otherwise explicitly specified and limited, the terms "mounting", "connection", "connection" should be understood broadly, for example, it can be fixedly connected, or it can be detachably connected, or integrally connected; it can be mechanically connected, or it can be electrically connected; it can be directly connected, or it can be indirectly connected through an intermediate medium; it can be the communication inside two elements. For ordinary skilled in the art, the specific meaning of the above terms in the utility model can be understood according to the specific circumstances.

[0028] The utility model will be explained in detail below with reference to the drawings and in combination with the embodiments.

[0029] Comparative example 1

[0030] The mixed C4 is input into a plurality of comparative reaction systems, the comparative reaction systems are connected with the comparative gas-liquid separation tank 16 through pipelines, the comparative gas-liquid separation tank 16 is connected with the comparative compressor 17 through pipelines, the comparative compressor 17 is connected with the comparative separation system 18 through pipelines, the comparative gas-liquid separation tank 16 is connected with the comparative separation system 18 through pipelines, and the pipelines between the comparative gas-liquid separation tank 16 and the comparative separation system 18 are provided with the comparative pump 19. The comparative reaction system is connected with the comparative regeneration system 15.

[0031] The comparative reaction system comprises a comparative feed and discharge heat exchanger 20, a comparative heating furnace 21, a comparative isomerization reactor 22 and a comparative cooler 12. The mixed C4 is heat-exchanged in the comparative feed and discharge heat exchanger 20, the comparative feed and discharge heat exchanger 20 is connected with the comparative heating furnace 21 through pipelines, the comparative heating furnace 21 is connected with the comparative isomerization reactor 22 through pipelines, the comparative isomerization reactor 22 is connected with the comparative feed and discharge heat exchanger 20 through pipelines, the comparative feed and discharge heat exchanger 20 is connected with the comparative gas-liquid separation tank 16 through pipelines, and the pipelines between the comparative feed and discharge heat exchanger 20 and the comparative gas-liquid separation tank 16 are provided with the comparative cooler 12.

[0032] The mixed C4 is divided into two streams, which are heated in the comparative feed and discharge heat exchanger 20 and the comparative heating furnace 21 respectively, then enter the comparative isomerization reactor 22 to react, the reaction products are heat-exchanged in the comparative feed and discharge heat exchanger 20 and cooled in the comparative cooler 12 respectively, then are combined, then are separated in the comparative gas-liquid separation tank, the comparative gas phase is pressurized by a compressor, the liquid phase is pressurized by the comparative pump 19, then are separated in the comparative separation system 18 respectively, and finally, isobutylene products are obtained.

[0033] When the catalyst in the comparative isomerization reactor 22 needs to be regenerated, nitrogen or air enters the comparative feed and discharge heat exchanger 20 and the comparative heating furnace 21 to be heated, then is regenerated by the comparative isomerization reactor 22, the reactor outlet regeneration gas is heat-exchanged in the comparative feed and discharge heat exchanger, and finally returns to the regeneration system.

[0034] According to this route, taking a 360,000 tons / year butene isomerization device (based on mixed C4) as an example, the utility consumption is shown in the following table 1:

[0035]

[0036] The prices of steam, electricity, circulating water and fuel gas are 250 yuan / t, 0.7 yuan / kW.h, 0.15 yuan / t and 3.5 yuan / Nm 3According to the calculation, the cost of public utilities is 9603.9 yuan / h.

[0037] Embodiment 1

[0038] An optimization system for producing isobutene by butene isomerization comprises an inlet and outlet heat exchanger 1, a heating furnace 2, an isomerization reactor system, a gas-liquid separation tank 3, a compressor 4, a separation system 5; mixed carbon four is heated by the inlet and outlet heat exchanger 1, the inlet and outlet heat exchanger 1 is connected with the heating furnace 2 through a pipeline, the heating furnace 2 is connected with the isomerization reactor system through a pipeline, the isomerization reactor system is connected with the inlet and outlet heat exchanger 1 through a pipeline, the inlet and outlet heat exchanger 1 is connected with the gas-liquid separation tank 3 through a pipeline, the gas phase of the gas-liquid separation tank 3 is connected with the compressor 4 through a pipeline, the compressor 4 is connected with the separation system 5 through a pipeline, the liquid phase of the gas-liquid separation tank 3 is connected with the separation system 5 through a pipeline, and the separation system 5 outputs isobutene products.

[0039] The regeneration cooler 11 is connected with the regeneration system 7 through a pipeline, the regeneration system 7 is connected with the regeneration heat exchanger 6 through a pipeline, the isomerization reactor system is connected with the regeneration heat exchanger 6 through a pipeline, and the regeneration heat exchanger 6 is connected with the regeneration cooler 11 through a pipeline; the regeneration heat exchanger 6 is connected with the electric heater 10 through a pipeline, and the electric heater 10 is connected with the isomerization reactor system through a pipeline.

[0040] The regeneration system 7 is connected with nitrogen through a pipeline, and the regeneration system 7 is connected with air through a pipeline.

[0041] The isomerization reactor system comprises a plurality of first isomerization reactors 8 and a plurality of second isomerization reactors 9, the heating furnace 2 is communicated with the plurality of first isomerization reactors 8 and the plurality of second isomerization reactors 9 respectively, and the plurality of first isomerization reactors 8 and the plurality of second isomerization reactors 9 are connected with the inlet and outlet heat exchanger 1 respectively.

[0042] The number of the first isomerization reactors 8 and the second isomerization reactors 9 is determined according to the actual production scale, for example, 4 reactors, 2 reactors and 2 regeneration, 3 reactors and 1 regeneration, etc.

[0043] The isomerization reactor system comprises a plurality of first isomerization reactors 8 and a plurality of second isomerization reactors 9, the plurality of first isomerization reactors 8 and the plurality of second isomerization reactors 9 are communicated with the regeneration heat exchanger 6 respectively, and the electric heater 10 is communicated with the plurality of first isomerization reactors 8 and the plurality of second isomerization reactors 9 respectively. A cooler 13 is arranged between the inlet and outlet heat exchanger 1 and the gas-liquid separation tank 3 (whether to arrange the cooler 13 is selected according to the actual situation). A pump 14 is arranged between the gas-liquid separation tank 3 and the separation system 5.

[0044] For example, Figure 1As shown, the embodiment 1 takes three reactors as an example, assuming that two first isomerization reactors 8 are running (operation period one to two months) and one second isomerization reactor 9 (regeneration period 7 days) in the three reactors, and the second isomerization reactor 9 is a standby reactor. The three isomerization reactors are only matched with one inlet and outlet heat exchanger 1 and one heating furnace 2, and one electric heater 10 is added, and two regeneration gas system heat exchangers.

[0045] First, the mixed carbon four is heated in the inlet and outlet heat exchanger 1 and the heating furnace 2, and then divided into two streams, which are respectively introduced into two first isomerization reactors 8 for reaction. The reaction products are combined at the outlet of the two first isomerization reactors 8, and then introduced into the inlet and outlet heat exchanger 1 and the cooler 13 for cooling. The gas phase is pressurized by the compressor 4, and the liquid phase is pressurized by the pump 14, and then respectively introduced into the separation system 5 for separation, and finally the isobutene product is obtained.

[0046] When one of the two first isomerization reactors 8 is at the end of the reaction and the catalyst needs to be regenerated, the second isomerization reactor 9 is opened and the first isomerization reactor 8 is closed, and the raw material mixed carbon four is no longer introduced. The regeneration gas is introduced into the reactor through the regeneration system 7, the regeneration gas heat exchanger 6 and the electric heater 10, and then returned to the regeneration system 7 through the regeneration heat exchanger 6 and the regeneration cooler 11.

[0047] At this time, nitrogen or air is introduced into the regeneration system 7, heated by the regeneration heat exchanger 6 and the electric heater 10, and regenerated by the above-mentioned first isomerization reactor 8. The regeneration gas at the outlet of the reactor is heat-exchanged by the regeneration heat exchanger 6 and cooled by the regeneration cooler 11, and finally returned to the regeneration system 7.

[0048] According to this route, taking a 360,000 tons / year butene isomerization device (based on mixed carbon four) as an example, the utility consumption is shown in Table 2:

[0049]

[0050] The price of steam is 250 yuan / t, the price of electricity is 0.7 yuan / kW.h, the price of circulating water is 0.15 yuan / t, and the price of fuel gas is 3.5 yuan / kg. The cost of utilities is 9392.5 yuan / h.

[0051] Comparing the embodiment 1 with the comparative example, the embodiment 1 has fewer equipment configurations than the comparative example, i.e. two inlet and outlet heat exchangers and two heating furnaces of the same specification are reduced, one electric heater and two heat exchangers are added, the equipment cost is reduced by 2.15 million yuan, the energy consumption cost is reduced by 211.4 yuan / h, and the annual operating time is 8000 hours. The annual energy saving cost is 169.12 million yuan / year.

[0052] Embodiment 2

[0053] This embodiment 2 takes three reactors as an example, assuming that the first isomerization reactor 8 is running (running period one to two months) in the three reactors, a second isomerization reactor is regenerated (regeneration period 7 days), three isomerization reactors are only matched with one high-efficiency heat exchanger and one heating furnace 2, and one electric heater 10 is added, and two regeneration gas system heat exchangers.

[0054] First, the mixed carbon four is heated in the feed- discharge heat exchanger 1 and the heating furnace 2, and then is divided into two streams, which are respectively introduced into two first isomerization reactors 8 for reaction. The reaction products are combined at the outlets of the two first isomerization reactors 8, and then are introduced into the feed- discharge heat exchanger 1 and the cooler 13 for cooling. The gas phase is pressurized by the compressor 4, and the liquid phase is pressurized by the pump 14, and then is respectively introduced into the separation system 5 for separation, so that the isobutene product is finally obtained.

[0055] When one of the two first isomerization reactors 8 is at the end of the reaction, and the catalyst needs to be regenerated, the second isomerization reactor 9 is opened, and one of the first isomerization reactors 8 is closed, and the raw material mixed carbon four is no longer introduced. At this time, the nitrogen or air is introduced into the regeneration system 7, and is heated by the regeneration heat exchanger 6 and the electric heater 10, and then is introduced into the above-mentioned first isomerization reactor 8 for regeneration. The regeneration gas at the outlet of the reactor is heat-exchanged by the regeneration heat exchanger 6, and is finally returned to the regeneration system 7.

[0056] According to this route, taking a 360,000 tons / year butene isomerization device (based on mixed carbon four) as an example, the utility consumption is shown in Table 3:

[0057]

[0058] The cost of the utility is 8826.3 yuan / h, which is calculated according to the price of steam of 250 yuan / t, the price of electricity of 0.7 yuan / kW.h, the price of circulating water of 0.15 yuan / t, and the price of fuel gas of 3.5 yuan / kg.

[0059] It can be known from the comparative example 2 and the embodiment 1 that the feed- discharge heat exchanger in the embodiment 1 is replaced by the high-efficiency heat exchanger in the scheme of the embodiment 2, the equipment cost is increased by 210,000 yuan, the energy consumption cost is reduced by 566.2 yuan / h, the annual operation time is 8000 hours, and the annual energy saving cost is 452.96 million yuan / year.

[0060] It can be known from the comparative example 2 and the comparative example that the equipment cost is reduced by 1.94 million yuan, the energy consumption cost is reduced by 777.6 yuan / h, the annual operation time is 8000 hours, and the annual energy saving cost is 622.08 million yuan / year.

[0061] The above only describes the preferred embodiments of the utility model, and does not limit the utility model. Any modification, equivalent replacement, improvement, etc. within the spirit and principle of the utility model should be included in the protection scope of the utility model.

Claims

1. An optimization system for isobutene production from butene isomerization, characterized by: The system comprises an inlet-outlet heat exchanger, a heating furnace, an isomerization reactor system, a gas-liquid separation tank, a compressor, and a separation system. The mixed C4 is exchanged by the inlet-outlet heat exchanger, the inlet-outlet heat exchanger is communicated with the heating furnace, the heating furnace is communicated with the isomerization reactor system, the isomerization reactor system is communicated with the inlet-outlet heat exchanger, the inlet-outlet heat exchanger is communicated with the gas-liquid separation tank, the gas phase of the gas-liquid separation tank is communicated with the inlet of the compressor, the outlet of the compressor is communicated with the separation system, the liquid phase of the gas-liquid separation tank is communicated with the separation system, and the separation system outputs isobutylene product. The regeneration system is communicated with the regeneration heat exchanger, the regeneration heat exchanger is communicated with the electric heater, the electric heater is communicated with the isomerization reactor system, the isomerization reactor system is communicated with the regeneration heat exchanger, and the regeneration heat exchanger is communicated with the regeneration cooler; the regeneration cooler is communicated with the regeneration system.

2. The system for optimization of isobutene production by butene isomerization as claimed in claim 1, wherein: The regeneration system is communicated with nitrogen and air.

3. The system for optimization of isobutene production by butene isomerization as claimed in claim 1, wherein: The isomerization reactor system comprises a plurality of first isomerization reactors and a plurality of second isomerization reactors, the heating furnace is respectively communicated with the plurality of first isomerization reactors and the plurality of second isomerization reactors, and the plurality of first isomerization reactors and the plurality of second isomerization reactors are respectively communicated with the inlet-outlet heat exchanger.

4. The system for optimization of isobutene production by butene isomerization as claimed in claim 1, wherein: The isomerization reactor system comprises a plurality of first isomerization reactors and a plurality of second isomerization reactors, the plurality of first isomerization reactors and the plurality of second isomerization reactors are respectively communicated with the regeneration heat exchanger, and the electric heater is respectively communicated with the plurality of first isomerization reactors and the plurality of second isomerization reactors.

5. The system for optimization of isobutene production by butene isomerization as claimed in claim 1, wherein: A cooler is arranged between the inlet-outlet heat exchanger and the gas-liquid separation tank.

6. The system for optimization of isobutene production by butene isomerization as claimed in claim 1, wherein: A pump is arranged between the gas-liquid separation tank and the separation system.

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