Method for improving utilization rate of synthesis gas of carbonyl synthesis reactor

Abstract

The invention provides a method for improving the utilization rate of synthesis gas in a carbonyl synthesis reactor, which comprises the following steps: mixing carbonyl reaction tail gas with part of fresh synthesis gas to form mixed gas, and introducing the mixed gas into the bottom of the carbonyl synthesis reactor; introducing the carbonyl reaction liquid into the bottom of a carbonyl synthesis reactor; the reaction liquid is located in a reaction zone of the carbonyl reactor, and propylene in the carbonyl reaction tail gas and the synthesis gas are subjected to a contact reaction in the reaction liquid; reactants synthesized in the reaction zone are conveyed to the next process; exhaust gas at the top of the reaction zone is conveyed and circulated into the bottom of the reaction zone through a pump body; an outer circulating liquid pipeline is arranged in the reaction area. Carbonyl reaction tail gas and fresh synthesis gas are introduced for mixed reaction, and the micro-interface reactor and an external circulation liquid entrainment reflux technology are combined, so that the utilization rate of the synthesis gas and propylene is increased, and the waste of raw materials is reduced. The circulation amount is automatically adjusted through the pressure control system, the pressure of the reaction area is accurately controlled, and the continuity and stability of the reaction process are improved.

Description

Technical Field

[0001] The invention relates to a method, in particular to a method for improving the utilization rate of synthesis gas in a carbonyl synthesis reactor, and belongs to the technical field of chemical industry. Background Art

[0002] In the field of oxo synthesis, the reaction of syngas with propylene using conventional reactors is a common process, but this process has significant drawbacks. First, unreacted tail gas is directly discharged, with syngas and propylene accounting for over 60% of the tail gas, resulting in significant waste of raw materials and increased production costs. Second, conventional reactors lack effective tail gas recirculation and pressure control mechanisms, leading to frequent fluctuations in the gas phase composition in the reaction zone. This makes it difficult to stabilize the reactor operating pressure, which can easily cause system load fluctuations, affecting the continuity of the reaction process and product yield. Summary of the Invention

[0003] Based on the above background, the purpose of the present invention is to provide a method for improving the utilization rate of synthesis gas in a carbonyl synthesis reactor by efficiently recovering tail gas and accurately controlling the reaction pressure, thereby solving the problems described in the background technology.

[0004] In order to achieve the above-mentioned object of the invention, the present invention provides the following technical solutions:

[0005] A method for improving the utilization rate of synthesis gas in an oxo synthesis reactor, comprising:

[0006] The carbonyl reaction tail gas is mixed with a portion of fresh synthesis gas to form a mixed gas, which is introduced into the bottom of the carbonyl synthesis reactor; the carbonyl reaction liquid is introduced into the bottom of the carbonyl synthesis reactor;

[0007] The reaction liquid is located in the reaction zone of the carbonylation reactor, and the propylene in the carbonylation reaction tail gas and the synthesis gas are contacted and reacted in the reaction liquid;

[0008] The reactants synthesized in the reaction zone are transported to the next process;

[0009] The exhaust gas at the top of the reaction zone is transported and circulated into the bottom of the reaction zone through the pump body;

[0010] The reaction zone is provided with an external circulating liquid pipeline, and the material in the reaction zone is circulated into the reaction zone through the external circulating liquid pipeline to remove the reaction heat;

[0011] The reaction zone is provided with a gas phase circulation pipeline, and the gas phase circulation pipeline circulates the gas phase entrained by the external circulation liquid in the external circulation liquid pipeline into the bottom of the reaction zone through a pump body;

[0012] The gas phase and inert gas that have not completely participated in the reaction at the top of the reaction zone enter the condenser for condensation, and the remaining gas after condensation is transported to the tail gas treatment unit.

[0013] Preferably, the external circulating liquid pipeline includes a circulating liquid pipeline and a cooler, and the material in the reaction zone is cooled by the cooler.

[0014] Preferably, the gas phase circulation pipeline includes a gas phase pipeline and a regulating valve, and the gas phase entrained by the external circulating liquid in the external circulating liquid pipeline circulates through the gas phase pipeline to the bottom of the reaction zone, and its circulation amount is controlled by the regulating valve.

[0015] Preferably, the reaction zone is a microinterface reactor, and a microinterface distributor is provided in the microinterface reactor; the mixed gas is evenly dispersed into the reaction liquid through the microinterface distributor.

[0016] Preferably, the operating conditions of the reaction zone further include: the flow rate of the external circulation liquid is 20% to 60% of the feed flow rate of the reaction zone.

[0017] Preferably, a pressure control system is provided at the top of the reaction zone, and the pressure control system is electrically connected to the regulating valve. The pressure control system automatically changes the opening of the regulating valve according to the pressure at the top of the reaction zone.

[0018] Preferably, an exhaust gas detection system is provided on the top of the reaction zone, and the exhaust gas detection system monitors the concentrations of carbon monoxide, hydrogen and propylene in real time.

[0019] Preferably, the operating conditions of the reaction zone include: pressure of 1.6-1.7 MPag, and temperature of 85-93°C.

[0020] Compared with the prior art, the present invention has the following advantages:

[0021] The present invention provides a method for improving the utilization rate of syngas in an oxo synthesis reactor. By introducing carbonyl reaction tail gas into a mixed reaction with fresh syngas, combined with a micro-interface reactor and external circulating liquid entrainment reflux technology, the utilization rate of syngas and propylene is increased, while reducing feedstock waste. A pressure control system automatically adjusts the circulation volume, precisely controlling the pressure in the reaction zone and improving the continuity and stability of the reaction process. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the embodiments or the description of the prior art. Obviously, the drawings described below are merely embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on the provided drawings without paying any creative work.

[0023] Figure 1 It is a schematic flow chart of the method of the present invention.

[0024] In the figure: 1. Carbonyl synthesis reactor; 2. Cooler; 3. Condenser; 4. Pump body; 5. Control valve; 6. Exhaust gas detection system. DETAILED DESCRIPTION

[0025] The technical solution of the present invention will be further described in detail below through specific embodiments and in conjunction with the accompanying drawings. It should be understood that the implementation of the present invention is not limited to the following embodiments, and any form of modification and / or change made to the present invention will fall within the scope of protection of the present invention.

[0026] In the present invention, unless otherwise specified, all parts and percentages are by weight. The equipment and raw materials used are commercially available or commonly used in the art. The methods in the following embodiments, unless otherwise specified, are conventional methods in the art. The components or equipment in the following embodiments, unless otherwise specified, are all universal standard parts or components known to those skilled in the art. Their structures and principles are known to those skilled in the art through technical manuals or routine experimental methods.

[0027] The following detailed description of the embodiments of the present invention is made in conjunction with the accompanying drawings. In the following detailed description, for ease of explanation, many specific details are set forth to provide a comprehensive understanding of the embodiments of the present invention. However, one or more embodiments may be implemented by those skilled in the art without these specific details.

[0028] A method for improving the utilization rate of synthesis gas in carbonyl synthesis reactor, such as Figure 1 As shown, the carbonyl reaction tail gas is mixed with part of the fresh synthesis gas to form a mixed gas, which is introduced into the bottom of the carbonyl synthesis reactor 1 through the mixed gas delivery pipeline. At the same time, the carbonyl reaction liquid is introduced into the bottom of the carbonyl synthesis reactor 1 through the reaction liquid delivery pipeline.

[0029] Oxo reactor 1 includes a reaction zone, which is a micro-interface reactor equipped with a micro-interface distributor. The micro-interface distributor evenly disperses the mixed gas into bubbles smaller than 10 microns and distributes them throughout the reaction solution containing the rhodium catalyst, allowing the synthesis gas and propylene to fully contact and react within the reaction solution.

[0030] The reaction zone is provided with an external circulating liquid pipeline. The material in the reaction zone is cooled by the cooler 2 in the external circulating liquid pipeline and then circulated back to the interior of the reaction zone to remove the reaction heat and achieve continuous cooling.

[0031] A gas phase circulation pipeline is provided on the external circulating liquid pipeline. During the circulation process, the external circulating liquid generates a liquid entrainment effect, entraining the unreacted gas phase discharged from the top of the reaction zone. The entrained gas phase is transported to the bottom of the reaction zone through the gas phase circulation pipeline, pump body 4 and regulating valve 5, and contacts and reacts with the reaction liquid again. A pressure control system is provided at the top of the reaction zone. The pressure control system is electrically connected to the regulating valve 5 and is used to monitor the pressure at the top of the reaction zone in real time. The pressure control system automatically adjusts the opening of the regulating valve 5 according to pressure changes, thereby controlling the gas phase circulation volume and achieving precise control of the reaction zone pressure. The external circulating liquid flow rate is preferably 20% to 60% of the feed flow rate of the carbonyl synthesis reactor 1.

[0032] An exhaust gas detection system 6 is provided at the top of the reaction zone for real-time monitoring of the concentrations of carbon monoxide, hydrogen and propylene in the exhaust gas, wherein the carbon monoxide concentration is controlled at 0.1% to 3%, the hydrogen concentration is controlled at 5% to 8%, and the propylene concentration is controlled at 10% to 15%.

[0033] A portion of the unreacted gas and inert gas at the top of the reaction zone is refluxed to the bottom of the reaction zone via the gas phase circulation pipeline. The remaining portion is condensed and recovered in condenser 3, and the remaining gas is discharged into the tail gas treatment unit. The tail gas treatment unit is preferably a flare system or a tail gas recovery system to treat the remaining gas that is not recovered after condensation at the top of the reaction zone.

[0034] The operating conditions of the carbonyl synthesis reactor 1 are: the pressure is controlled within the range of 1.6-1.7 MPag, and the temperature is controlled within the range of 85-93° C. to ensure the stability of the reaction.

[0035] Through the above method, not only the utilization rate of synthesis gas and propylene is significantly improved, and the waste of resources caused by tail gas emissions is reduced, but also the continuity and stability of system operation are improved by precisely controlling the reactor pressure, while reducing the overall energy consumption and realizing the optimization of the carbonyl synthesis reaction process. It is particularly suitable for the carbonyl synthesis reaction system of butyl octanol.

[0036] The implementation principle of the method for improving the utilization rate of synthesis gas in the carbonyl synthesis reactor of the present invention is as follows:

[0037] The carbonyl reaction tail gas is mixed with a portion of fresh synthesis gas and then introduced into the bottom of the carbonyl synthesis reactor 1, and the carbonyl reaction liquid is introduced simultaneously. The micro-interface distributor provided inside the micro-interface reactor is used to refine the mixed gas into tiny bubbles and evenly disperse them in the reaction liquid containing the rhodium catalyst, so that the synthesis gas and propylene can fully contact and react in the micro-interface environment, thereby improving the gas-liquid mass transfer efficiency and the reaction rate, thereby improving the conversion rate of the synthesis gas and propylene.

[0038] In order to remove the reaction heat generated during the reaction, an external circulating liquid pipeline is set in the reaction zone to cool the reaction liquid through cooler 2 to avoid the internal temperature of the reactor being too high, which may lead to side reactions or decreased catalyst activity, further ensuring the efficiency and stability of the reaction.

[0039] At the same time, a gas phase circulation pipeline is provided within the external circulating liquid pipeline. The entrainment effect of the liquid flow generated during the flow of the external circulating liquid is utilized to entrain the unreacted gas phase discharged from the top of the reaction zone and reflux it to the bottom of the reaction zone. A regulating valve 5 is provided within the gas phase circulation pipeline, and a pressure control system is provided at the top of the reaction zone. The pressure control system is electrically connected to the regulating valve 5 and can monitor the pressure at the top of the reaction zone in real time and automatically adjust the opening of the regulating valve 5 according to pressure changes, thereby dynamically controlling the reflux gas volume and accurately stabilizing the pressure within the reaction zone.

[0040] A tail gas monitoring system 6 is installed at the top of the reaction zone to monitor the concentrations of carbon monoxide, hydrogen, and propylene in the tail gas in real time, enabling timely adjustment of process parameters to ensure optimal reaction operation. A condenser 3 is located at the gas phase outlet at the top of the reaction zone to recover condensable components, further improving resource utilization. Uncondensed inert gases and residual tail gas are discharged or recovered through the tail gas treatment unit.

[0041] This document uses specific examples to illustrate the principles and implementation methods of the present invention. The above examples are only intended to help understand the method and core concept of the present invention. It should be noted that those skilled in the art can make various improvements and modifications to the present invention without departing from the principles of the present invention, and such improvements and modifications also fall within the scope of protection of the claims of the present invention.

Claims

1. A method for improving the utilization rate of synthesis gas in an oxo synthesis reactor, characterized in that: include: Mixing the carbonyl reaction tail gas with a portion of fresh synthesis gas to form a mixed gas, and introducing the mixed gas into the bottom of the carbonyl synthesis reactor (1); introducing the carbonyl reaction liquid into the bottom of the carbonyl synthesis reactor (1); The reaction liquid is located in the reaction zone of the carbonylation reactor, and the propylene in the carbonylation reaction tail gas and the synthesis gas are contacted and reacted in the reaction liquid; The reactants synthesized in the reaction zone are transported to the next process; The exhaust gas at the top of the reaction zone is transported and circulated into the bottom of the reaction zone through a pump body (4); The reaction zone is provided with an external circulating liquid pipeline, and the material in the reaction zone is circulated into the reaction zone through the external circulating liquid pipeline to remove the reaction heat; The reaction zone is provided with a gas phase circulation pipeline, and the gas phase circulation pipeline circulates the gas phase entrained by the external circulation liquid in the external circulation liquid pipeline into the bottom of the reaction zone through a pump body (4); The gas phase and inert gas that have not completely participated in the reaction at the top of the reaction zone after the reaction enter the condenser (3) for condensation, and the remaining gas after condensation is transported to the tail gas treatment unit.

2. The method for improving the utilization rate of synthesis gas in an oxo synthesis reactor according to claim 1, characterized in that: The external circulating liquid pipeline comprises a circulating liquid pipeline and a cooler (2), and the material in the reaction zone is cooled by the cooler (2).

3. The method for improving the utilization rate of synthesis gas in an oxo synthesis reactor according to claim 1, characterized in that: The gas phase circulation pipeline comprises a gas phase pipeline and a regulating valve (5); the gas phase entrained by the external circulating liquid in the external circulating liquid pipeline circulates through the gas phase pipeline to the bottom of the reaction zone, and its circulation amount is controlled by the regulating valve (5).

4. The method for improving the utilization rate of synthesis gas in an oxo synthesis reactor according to claim 1, characterized in that: The reaction zone is a microinterface reactor, and a microinterface distributor is arranged in the microinterface reactor; The mixed gas is evenly dispersed into the reaction liquid through a micro-interface distributor.

5. The method for improving the utilization rate of synthesis gas in an oxo synthesis reactor according to claim 3, characterized in that: The operating conditions of the reaction zone also include: the flow rate of the external circulation liquid is 20% to 60% of the feed flow rate of the reaction zone.

6. The method for improving the utilization rate of synthesis gas in an oxo synthesis reactor according to claim 3, characterized in that: A pressure control system is provided at the top of the reaction zone. The pressure control system is electrically connected to the regulating valve (5). The pressure control system automatically changes the opening of the regulating valve (5) according to the pressure at the top of the reaction zone.

7. The method for improving the utilization rate of synthesis gas in an oxo synthesis reactor according to claim 4, characterized in that: A tail gas detection system (6) is provided on the top of the reaction zone, and the tail gas detection system (6) monitors the concentrations of carbon monoxide, hydrogen and propylene in real time.

8. The method for improving the utilization rate of synthesis gas in an oxo synthesis reactor according to claim 5, characterized in that: The operating conditions of the reaction zone include: pressure of 1.6-1.7 MPag and temperature of 85-93°C.

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