CN113277924A - A high-efficient heat exchange system for propylene preparation - Google Patents
A high-efficient heat exchange system for propylene preparation Download PDFInfo
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Abstract
The invention provides a high-efficiency heat exchange system for preparing propylene, which comprises a raw material treatment and reaction system, a propylene purification system, a methyl nitrite regeneration system, a dimethyl oxalate reaction system and a byproduct refining system; wherein, raw materials is handled and reaction system includes raw materials preliminary treatment tower, shell and tube fixed bed reactor and double-effect flash distillation system, propylene purification system includes two decarbonization towers, pressure swing adsorption cooler, heat pump rectifying column and propylene holding vessel, methyl nitrite regeneration system includes nitrogen oxygen blending tank, methyl nitrite regeneration reactor and methyl alcohol recovery tower, dimethyl oxalate reaction system includes coupling reactor, methyl alcohol stripping tower and dimethyl oxalate purifying column, the by-product refining system includes methyl nitrite recovery tower, methyl alcohol pressure swing rectifying column and dimethyl carbonate pressure swing rectifying column. The system can effectively treat byproducts generated in the process of preparing propylene from propane, and can realize heat energy balance through the cooperation of the systems, thereby avoiding energy waste.
Description
Technical Field
The invention relates to the technical field of petrochemical industry, in particular to a high-efficiency heat exchange system for preparing propylene.
Background
Propylene is an important industrial feedstock and plays an important role in modern industry. In recent years, with the continuous increase of the demand of propylene in China, the yield of the propylene has a large gap. Currently, propylene production technologies mainly include petroleum catalytic cracking (FCC), naphtha steam cracking, Methanol To Propylene (MTP), and C4／C5Hydrocarbon selective cracking, olefin disproportionation, Propane Dehydrogenation (PDH) and the like, wherein the proportion of the naphtha steam cracking and the petroleum catalytic cracking for preparing the propylene is the largest. With the rising of oil price and the exhaustion of petroleum energy in the future, the development of petrochemical industry is restricted, so that the search for high-efficiency propylene yield increasing technology suitable for industrial scale has become an urgent need of China and the global chemical industry.
At present, the requirement of industrial production on propylene is difficult to meet by relying on the traditional naphtha steam cracking and catalytic cracking device to produce propylene as a byproduct, the market price of alkane and alkene is greatly different, people pay attention to the process for producing high-value-added alkene by alkane dehydrogenation with low price, and a plurality of large-scale propane dehydrogenation propylene preparation devices are put into production worldwide and are an important way for producing propylene besides catalytic cracking and naphtha cracking. However, the propane dehydrogenation to propylene reaction is a strongly endothermic, equilibrium limited process, requiring a large heat supply in an industrial unit to increase propane per pass conversion.
Meanwhile, propane does not have a structure of single electron and empty orbit, and the C-H bond energy is higher, so that more energy is needed for activating the C-H bond than for activating the C-C bond, and therefore, in the oxidation process of propane, the C-C bond is inevitably broken, which causes a series of side reactions, not only reduces the selectivity, generates byproducts such as carbon monoxide, carbon dioxide and the like, and if the byproducts are directly discharged, the air quality is affected, the greenhouse effect is aggravated and other adverse effects are caused, and simultaneously, the carbon monoxide has high toxicity and can harm the body health of operators. At present, the traditional high-temperature combustion method is mostly adopted for treating the waste gas generated in the preparation of propylene by propane dehydrogenation, fuel is fuel gas or fuel oil, and the principle is that tail gas, fuel and air are combusted in a high-temperature incinerator (750-800 ℃), so that volatile organic compounds, carbon monoxide and the like in the tail gas are converted into nontoxic carbon dioxide and water vapor to be discharged, and meanwhile, the heat of the high-temperature tail gas is recovered for producing steam as a byproduct. However, the method consumes a large amount of fuel gas or liquefied gas, has high cost and influences economic benefits.
Disclosure of Invention
Aiming at the problems in the prior art, the invention aims to provide a high-efficiency heat exchange system for preparing propylene, so as to solve the technical problems that in the background art, the environment is affected and the human body is harmed by a byproduct easily generating CO in the process of preparing propylene by propane dehydrogenation, the process is a strong heat absorption process, a large amount of energy is wasted, and the yield of propylene is low.
The purpose of the invention is realized by the following technical scheme:
a high-efficiency heat exchange system for propylene production, characterized in that:
the method comprises the following steps:
the raw material processing and reaction system is used for mixing and pressurizing raw materials consisting of propane and carbon dioxide, and carrying out oxidation synthesis and dehydration reaction to obtain crude propylene saturated gas; the crude propylene saturated gas comprises propylene, carbon monoxide, carbon dioxide, unreacted propane and methanol;
the propylene purification system is used for rectifying crude propylene saturated gas and separating propylene from propane, carbon monoxide from carbon dioxide and methanol;
a methyl nitrite regeneration system for recovering methanol in the propylene purification system to produce methyl nitrite for use in treating carbon monoxide;
the dimethyl oxalate reaction system is used for mixing carbon monoxide and methyl nitrite to generate dimethyl oxalate;
the byproduct refining system is used for rectifying the product in the dimethyl oxalate reaction system and simultaneously recovering the rectified dimethyl carbonate product and methanol;
the raw material treatment and reaction system and the propylene purification system comprise heat transfer systems, the methyl nitrite regeneration system, the dimethyl oxalate reaction system and the byproduct refining system comprise waste heat recovery systems, the heat transfer systems and the waste heat recovery systems are composed of heat exchangers, and the waste heat recovery systems are connected with the heat exchangers of the heat transfer systems.
The raw material treatment and reaction system further comprises a raw material pretreatment tower, a tubular fixed bed reactor and a double-effect flash evaporation system; the raw material pretreatment tower is used for pretreating a propane raw material, and mixing and pressurizing the pretreated propane and a carbon dioxide raw material; the shell-and-tube fixed bed reactor is used for heating and reacting raw materials to obtain undehydrated crude propylene saturated gas, and the heat of a heat transfer system is converted into high-pressure steam by a high-pressure steam pipe in an inner shell of the shell-and-tube fixed bed reactor for heat supplement in the heating and reacting process; the double-effect flash evaporation system is used for removing moisture in the undehydrated crude propylene saturated gas.
The tubular fixed bed reactor can effectively monitor and control the temperature in the reaction process, thereby controlling the reaction speed and the catalyst activity and achieving chemical balance.
The propylene purification system comprises a double decarbonization tower, a pressure swing adsorption cooler, a heat pump rectifying tower and a propylene storage tank; the double decarbonization tower is used for removing carbon dioxide in the crude propylene saturated gas; the pressure swing adsorption cooler is used for compressing and condensing the crude propylene saturated gas without carbon dioxide to form saturated liquid, and then separating carbon monoxide and methanol to enter a methyl nitrite regeneration system and a dimethyl oxalate reaction system; the heat pump rectifying tower is used for separating propylene and propane, the propylene enters the propylene storage tank, and the propane enters the raw material treatment and reaction system for continuous reaction.
Further optimizing, the methyl nitrite regeneration system comprises a nitrogen-oxygen mixing tank, a methyl nitrite regeneration reactor and a methanol recovery tower; the nitrogen-oxygen mixing tank is used for mixing newly added oxygen, nitrogen and nitric oxide; the methyl nitrite regeneration reactor comprises a reaction tower, a tower top cooler and a tower bottom reboiler, mixed gas in the nitrogen-oxygen mixing tank enters the reaction tower for reaction after being preheated, the methyl nitrite is separated after being cooled by the tower top cooler, wastewater of tower bottom liquid after passing through the tower bottom reboiler is sent to a sewage treatment system, and liquid except the wastewater directly flows into a methanol recovery tower for recovery.
Further optimized, the dimethyl oxalate reaction system comprises a coupling reactor, a methanol stripping tower and a dimethyl oxalate purifying tower; the coupling reactor is used for conducting carbonylation reaction on methyl nitrite in a methyl nitrite regeneration system and carbon monoxide in a propylene purification system to synthesize dimethyl oxalate, cooling the dimethyl oxalate through a cooler after reaction, enabling the dimethyl oxalate to enter a methanol stripping tower for absorption, enabling coupling gas separated from the top of the tower to be sent to a mixer intermediate storage tank, enabling rich liquid at the bottom of the tower to be sent to a dimethyl oxalate purification tower, purifying the dimethyl oxalate purification tower to obtain a dimethyl oxalate product, and enabling liquid at the top of the dimethyl oxalate purification tower to enter a byproduct refining system.
Further optimizing, wherein the byproduct refining system comprises a methyl nitrite recovery tower, a methanol pressure swing rectifying tower and a dimethyl carbonate pressure swing rectifying tower; the methyl nitrite recovery tower is used for separating and recovering liquid at the top of the dimethyl oxalate purification tower, wherein gas components containing methyl nitrite are at the top of the tower and are conveyed to an intermediate storage tank after being condensed and emptied, methanol and dimethyl carbonate are at the bottom of the tower, the methanol is recovered by a methanol pressure swing rectifying tower, and the dimethyl carbonate is recovered by a dimethyl carbonate pressure swing rectifying tower.
And in the further optimization, the heat exchanger adopts a dividing wall type heat exchanger.
For further optimization, the high efficiency heat exchange system further comprises a DCS (distributed control system).
Further optimization, compressors in the raw material treatment and reaction system, the propylene purification system, the methyl nitrite regeneration system, the dimethyl oxalate reaction system and the byproduct refining system adopt a bypass control method, namely when the flow is small, a bypass is opened for adjustment.
Surge is the vibration of the compressor under an abnormal condition that occurs when the flow is reduced to a certain extent; surge presents a serious hazard to the compressor. The defect of serious negative pressure at the inlet end caused by directly adjusting the inlet flow can be effectively avoided by adopting a bypass control method, and the surge of the compressor is further avoided.
The invention has the following technical effects:
the system realizes the treatment of byproducts in the process of preparing propylene from propane and carbon dioxide through a methyl nitrite regeneration system, a dimethyl oxalate reaction system and a byproduct refining system, utilizes a large amount of high-temperature and high-heat material flows existing in the regeneration, dimethyl oxalate production and refining stages of methyl nitrite, and uses waste heat for producing low-pressure steam through the combination of a waste heat recovery system and a heat transfer system, thereby meeting the requirement of endothermic reaction in a raw material treatment and reaction system and a propylene purification system, further realizing the recycling of heat, reducing the energy consumption in the heat exchange process and having energy-saving and economic effects.
The system enables the reaction process to be more complete through the recycling of heat and the recycling of materials, and the purity of products such as propylene, dimethyl oxalate, methanol and the like is higher. In the present system, the purity of propylene finally obtained was 99.5% (mole fraction), the purity of dimethyl oxalate was 99.9% (mole fraction), the purity of dimethyl carbonate was 99.9% (mole fraction), and the purity of methanol was 98.76% (mole fraction).
Drawings
Fig. 1 is a schematic structural diagram of a high-efficiency heat exchange system in an embodiment of the invention.
Wherein, 1, a raw material processing and reaction system; 11. a raw material pretreatment tower; 12. a tubular fixed bed reactor; 13. a double effect flash system; 2. a propylene purification system; 21. a double decarbonization tower; 22. a pressure swing adsorption cooler; 23. a heat pump rectifying tower; 24. a propylene storage tank; 3. a methyl nitrite regeneration system; 31. a nitrogen-oxygen mixing tank; 32. a methyl nitrite regeneration reactor; 33. a methanol recovery tower; 4. a dimethyl oxalate reaction system; 41. a coupling reactor; 42. a methanol stripping tower; 43. a dimethyl oxalate purifying tower; 44. a mixer intermediate storage tank; 5. a byproduct refining system; 51. a methyl nitrite recovery tower; 52. a methanol pressure swing rectifying tower; 53. a dimethyl carbonate pressure swing rectifying tower; 100. a heat exchanger.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example (b):
as shown in fig. 1, a high efficiency heat exchange system for propylene production is characterized in that:
the method comprises the following steps:
the system comprises a raw material processing and reaction system 1, wherein the raw material processing and reaction system 1 is used for mixing and pressurizing raw materials consisting of propane and carbon dioxide, and carrying out oxidation synthesis and dehydration reaction to obtain crude propylene saturated gas; the crude propylene saturated gas includes propylene, carbon monoxide, carbon dioxide, unreacted propane and methanol. The raw material treatment and reaction system 1 comprises a raw material pretreatment tower 11, a tubular fixed bed reactor 12 and a double-effect flash evaporation system 13; the raw material pretreatment tower 11 is used for pretreating a propane raw material, and mixing and pressurizing the pretreated propane and a carbon dioxide raw material; the tubular fixed bed reactor 13 is used for heating and reacting the raw materials to obtain crude propylene saturated gas without dehydration, and the heat of a heat transfer system is converted into high-pressure steam for heat supplement by a high-pressure steam pipe in an inner shell of the tubular fixed bed reactor 12 in the heating and reacting process; the double effect flash system 13 is used to remove water from the crude propylene saturated gas that is not dehydrated.
The tubular fixed bed reactor 12 can effectively monitor and control the temperature in the reaction process, so as to control the reaction speed and the catalyst activity and achieve chemical balance.
The propylene purification system 2 is used for rectifying the crude propylene saturated gas, and separating propylene from propane, carbon monoxide from carbon dioxide and methanol; the propylene purification system 2 comprises a double-decarbonization tower 21, a pressure swing adsorption cooler 22, a heat pump rectifying tower 23 and a propylene storage tank 24; the double decarbonization tower 21 is used for removing carbon dioxide in the crude propylene saturated gas; the pressure swing adsorption cooler 22 is used for compressing and condensing the crude propylene saturated gas from which carbon dioxide is removed to form saturated liquid, and further separating carbon monoxide and methanol to enter a methyl nitrite regeneration system 3 and a dimethyl oxalate reaction system 4; the heat pump rectifying tower 23 is used for separating propylene and propane, the propylene enters the propylene storage tank 24, and the propane enters the raw material treatment and reaction system 1 for continuous reaction.
A methyl nitrite regeneration system 3, wherein the methyl nitrite regeneration system 3 is used for recovering methanol in the propylene purification system 2 to generate methyl nitrite for treating carbon monoxide; the methyl nitrite regeneration system 3 comprises a nitrogen-oxygen mixing tank 31, a methyl nitrite regeneration reactor 32 and a methanol recovery tower 33; the nitrogen-oxygen mixing tank 31 is used for mixing newly added oxygen, nitrogen and nitric oxide; the methyl nitrite regeneration reactor 32 comprises a reaction tower, a tower top cooler and a tower bottom reboiler, mixed gas in the nitrogen-oxygen mixing tank enters the reaction tower for reaction after being preheated, the methyl nitrite is separated after being cooled by the tower top cooler, wastewater of tower bottom liquid after passing through the tower bottom reboiler is sent to a sewage treatment system, and liquid except the wastewater directly flows into the methanol recovery tower 33 for recovery.
The dimethyl oxalate reaction system 4 is used for mixing carbon monoxide and methyl nitrite to generate dimethyl oxalate; the dimethyl oxalate reaction system 4 comprises a coupling reactor 41, a methanol stripping tower 42 and a dimethyl oxalate purifying tower 43; the coupling reactor 41 is used for conducting carbonylation reaction on methyl nitrite in the methyl nitrite regeneration system 3 and carbon monoxide in the propylene purification system to synthesize dimethyl oxalate, cooling the dimethyl oxalate through a cooler after reaction, entering a methanol stripping tower 42 for absorption, sending coupling gas separated from the tower top into a mixer intermediate storage tank 44, sending rich liquid at the tower bottom into a dimethyl oxalate purification tower 43, purifying the dimethyl oxalate purification tower 43 to obtain a dimethyl oxalate product, and sending liquid at the tower top of the dimethyl oxalate purification tower 43 into a byproduct refining system 5.
A byproduct refining system 5, wherein the byproduct refining system 5 is used for rectifying the product in the dimethyl oxalate reaction system 4 and simultaneously recovering the rectified dimethyl carbonate product and methanol; the byproduct refining system comprises a methyl nitrite recovery tower 51, a methanol pressure swing rectifying tower 52 and a dimethyl carbonate pressure swing rectifying tower 53; the methyl nitrite recovery tower 51 is used for separating and recovering liquid at the top of the dimethyl oxalate purification tower 43, wherein gas components containing methyl nitrite are at the top of the tower and are conveyed to an intermediate storage tank after being condensed and evacuated, methanol and dimethyl carbonate are at the bottom of the tower, the methanol is recovered by a methanol pressure swing rectification tower 52, and the dimethyl carbonate is recovered by a dimethyl carbonate pressure swing rectification tower 53.
The raw material treatment and reaction system 1 and the propylene purification system 2 comprise a heat transfer system, the methyl nitrite regeneration system 3, the dimethyl oxalate reaction system 4 and the byproduct refining system 5 comprise a waste heat recovery system, the heat transfer system and the waste heat recovery system are both composed of heat exchangers 100, and the heat exchangers 100 of the waste heat recovery system and the heat transfer system are connected with each other. The heat exchanger 100 is a dividing wall type heat exchanger.
The high-efficiency heat exchange system also comprises a DCS (distributed control system); the compressors in the raw material treatment and reaction system 1, the propylene purification system 2, the methyl nitrite regeneration system 3, the dimethyl oxalate reaction system 4 and the byproduct refining system 5 adopt a bypass control method, namely when the flow is small, a bypass is opened for adjustment.
Surge is the vibration of the compressor under an abnormal condition that occurs when the flow is reduced to a certain extent; surge presents a serious hazard to the compressor. The defect of serious negative pressure at the inlet end caused by directly adjusting the inlet flow can be effectively avoided by adopting a bypass control method, and the surge of the compressor is further avoided.
The method comprises the following specific steps:
firstly, the propane raw material is added into a raw material pretreatment tower 11 for pretreatment and separation C4Mixing the mixture, adding the pretreated propane raw material and the carbon dioxide raw material into a tubular fixed bed reactor 12 after mixing, and carrying out oxidation heating reaction to synthesize propylene, wherein the reaction equation is as follows:
C3H8+CO2=C3H6+H2O+CO，
the generated mixed gas enters a double-effect flash system 13 to remove moisture, so that crude propylene saturated gas is obtained;
then the crude propylene saturated gas enters a double decarbonization tower 21, the carbon dioxide which is not reacted completely is removed and then flows out from the bottom of the tower, the mixed gas of which the carbon dioxide is removed passes through a pressure swing adsorption cooler 22, the pressure swing adsorption cooler 22 separates carbon monoxide and methanol gas and sends the carbon monoxide and the methanol gas to a methyl nitrite regeneration system 3 and a dimethyl oxalate reaction system 4, propylene and propane which are reacted completely enter a heat pump rectifying tower 23, the heat pump rectifying tower 23 separates the propylene from the propane, the propylene enters a propylene storage tank 24, a part of the propane is used as a raw material to continuously participate in a cyclic reaction, and a part of the propylene circulates and returns to the rectifying tower, and the purity of the separated propylene is 99.5% (mole fraction).
Mixing oxygen, nitrogen and nitric oxide which are newly added from the outside by a nitrogen-oxygen mixing tank 31, mixing the mixture with methanol separated in a pressure swing adsorption cooler 22, feeding the mixture into a methyl nitrite regeneration reactor 32 for reaction to generate methyl nitrite, removing the mixture of the methanol and water at the bottom of the tower after the reaction, feeding the mixture into a methanol recovery tower 33, cooling the mixture by a tower top cooler, separating the methyl nitrite, feeding the methyl nitrite into a dimethyl oxalate reaction system 4, and carrying out carbonylation reaction with carbon monoxide separated in the pressure swing adsorption cooler 22 in a coupling reactor 41 to generate dimethyl oxalate, wherein the purity of the dimethyl oxalate is 99.9 percent (mole fraction); after the reaction, the reaction product is cooled by a cooler, the reaction product enters a methanol stripping tower 42 for absorption, coupling gas separated from the tower top is sent to a mixer intermediate storage tank 44, rich liquid at the tower bottom is sent to a dimethyl oxalate purification tower 43, a dimethyl oxalate product is obtained by purification of the dimethyl oxalate purification tower 43, and liquid at the tower top of the dimethyl oxalate purification tower 43 enters a byproduct refining system 5; the methyl nitrite recovery tower 51 is used for separating and recovering liquid at the top of the dimethyl oxalate purification tower 43, wherein the top of the tower is a gas component containing methyl nitrite, the gas component is conveyed to an intermediate storage tank after being condensed and evacuated, the bottom of the tower is methanol and dimethyl carbonate, the methanol is recovered by a methanol pressure swing rectification tower 52, the methanol purity is 98.76% (mole fraction), and the dimethyl carbonate is recovered by a dimethyl carbonate pressure swing rectification tower 53, and the dimethyl carbonate purity is 99.9% (mole fraction).
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (6)
1. A high-efficiency heat exchange system for propylene production, characterized in that:
the method comprises the following steps:
the system comprises a raw material processing and reaction system (1), wherein the raw material processing and reaction system (1) is used for mixing and pressurizing raw materials consisting of propane and carbon dioxide, and carrying out oxidation synthesis and dehydration reaction to obtain crude propylene saturated gas; the crude propylene saturated gas comprises propylene, carbon monoxide, carbon dioxide, unreacted propane and methanol;
the propylene purification system (2), the propylene purification system (2) is used for rectifying the crude propylene saturated gas, and separating propylene from propane, carbon monoxide from carbon dioxide and methanol;
a methyl nitrite regeneration system (3), wherein the methyl nitrite regeneration system (3) is used for recovering methanol in the propylene purification system to generate methyl nitrite for treating carbon monoxide;
the dimethyl oxalate reaction system (4), the dimethyl oxalate reaction system (4) is used for mixing carbon monoxide and methyl nitrite to generate dimethyl oxalate;
the byproduct refining system (5), the byproduct refining system (5) is used for rectifying the product in the dimethyl oxalate reaction system (4) and simultaneously recovering the rectified dimethyl carbonate product and methanol;
the raw material processing and reaction system (1) and the propylene purification system (2) comprise heat transfer systems, the methyl nitrite regeneration system (3), the dimethyl oxalate reaction system (4) and the byproduct refining system (5) comprise waste heat recovery systems, the heat transfer systems and the waste heat recovery systems are both composed of heat exchangers (100), and the waste heat recovery systems are connected with the heat exchangers (100) of the heat transfer systems.
2. The high efficiency heat exchange system for propylene production as claimed in claim 1, wherein: the raw material treatment and reaction system (1) also comprises a raw material pretreatment tower (11), a tubular fixed bed reactor (12) and a double-effect flash evaporation system (13); the raw material pretreatment tower (11) is used for pretreating a propane raw material, and mixing and pressurizing the pretreated propane and a carbon dioxide raw material; the shell-and-tube fixed bed reactor (12) is used for heating and reacting raw materials to obtain crude propylene saturated gas without dehydration, and the heat of a heat transfer system is converted into high-pressure steam for heat supplement by a high-pressure steam pipe in an inner shell of the shell-and-tube fixed bed reactor (12) in the heating and reacting process; the double-effect flash system (13) is used for removing water in the undehydrated crude propylene saturated gas.
3. A high efficiency heat exchange system for propylene production as claimed in any one of claims 1 or 2 wherein: the propylene purification system (2) comprises a double-decarbonization tower (21), a pressure swing adsorption cooler (22), a heat pump rectifying tower (23) and a propylene storage tank (24); the double decarbonization tower (21) is used for removing carbon dioxide in the saturated gas of crude propylene; the pressure swing adsorption cooler (22) is used for compressing and condensing the crude propylene saturated gas without carbon dioxide to form saturated liquid, and then separating carbon monoxide and methanol to enter a methyl nitrite regeneration system (3) and a dimethyl oxalate reaction system (4); the heat pump rectifying tower (23) is used for separating propylene and propane, the propylene enters the propylene storage tank (24), and the propane enters the raw material treatment and reaction system (1) for continuous reaction.
4. A high efficiency heat exchange system for propylene production according to any one of claims 1 to 3, wherein: the methyl nitrite regeneration system (3) comprises a nitrogen-oxygen mixing tank (31), a methyl nitrite regeneration reactor (32) and a methanol recovery tower (33); the nitrogen-oxygen mixing tank (31) is used for mixing newly added oxygen, nitrogen and nitric oxide; the methyl nitrite regeneration reactor (32) comprises a reaction tower, a tower top cooler and a tower bottom reboiler, mixed gas in the nitrogen-oxygen mixing tank (31) enters the reaction tower after being preheated for reaction, the methyl nitrite is separated after being cooled by the tower top cooler, wastewater of tower bottom liquid after passing through the tower bottom reboiler is sent to a sewage treatment system, and liquid except the wastewater directly flows into a methanol recovery tower (33) for recovery.
5. A high efficiency heat exchange system for propylene production as claimed in any one of claims 1 or 4 wherein: the dimethyl oxalate reaction system (4) comprises a coupling reactor (41), a methanol stripping tower (42) and a dimethyl oxalate purifying tower (43); the coupling reactor (41) is used for conducting carbonylation reaction on methyl nitrite in the methyl nitrite regeneration system (3) and carbon monoxide in the propylene purification system (2) to synthesize dimethyl oxalate, the dimethyl oxalate is cooled by a cooler after reaction, the dimethyl oxalate enters a methanol stripping tower (42) for absorption, coupling gas separated from the tower top is sent to a mixer intermediate storage tank (44), rich liquid at the tower bottom is sent to a dimethyl oxalate purification tower (43), a dimethyl oxalate product is obtained through purification of the dimethyl oxalate purification tower (43), and liquid at the tower top of the dimethyl oxalate purification tower (43) enters a byproduct refining system (5).
6. The high efficiency heat exchange system for propylene production as claimed in claim 5, wherein: the byproduct refining system (5) comprises a methyl nitrite recovery tower (51), a methanol pressure swing rectifying tower (52) and a dimethyl carbonate pressure swing rectifying tower (53); the methyl nitrite recovery tower (51) is used for separating and recovering liquid at the top of the dimethyl oxalate purifying tower (43), wherein gas components containing methyl nitrite are at the top of the tower and are conveyed to an intermediate storage tank after being condensed and emptied, methanol and dimethyl carbonate are at the bottom of the tower, the methanol is recovered through a methanol pressure swing rectifying tower (52), and the dimethyl carbonate is recovered through a dimethyl carbonate pressure swing rectifying tower (53).
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