Propane dehydrogenation and hydroformylation coupling system and process

Abstract

The invention belongs to the technical field of petrochemical engineering and organic synthesis, and discloses a propane dehydrogenation and hydroformylation coupling system and a propane dehydrogenation and hydroformylation coupling process, and butyraldehyde with higher additional value than propylene can be generated in one step by coupling propylene and hydrogen generated by propane dehydrogenation reaction and propylene and hydrogen required by propylene hydroformylation reaction as raw materials. Only carbon monoxide is used as an additional raw material for propylene hydroformylation, so that links such as storage and transportation of propylene and hydrogen required by a hydroformylation process and a production process of single propylene and hydrogen are avoided, the energy utilization efficiency is improved, the equipment investment and the operation cost are reduced, the construction land is reduced, and the process intensification degree is improved; the operation is easier, and the economic benefit is better.

Description

Technical Field

[0001] The present invention belongs to the technical field of petrochemical industry and organic synthesis, and in particular relates to a system and process for coupling propane dehydrogenation and hydroformylation. Background Art

[0002] Propylene hydroformylation is a core reaction in the organic synthesis industry for producing high-value oxygenates (such as butyraldehyde and isobutyraldehyde). Approximately 70% of global plasticizers rely on butyraldehyde derivatives, which are widely used in industries such as PVC plastics, rubber, and coatings, supporting trillion-dollar markets such as construction, automotive, and packaging. Therefore, butyraldehyde and its derivatives are key links in the global supply chain, and independent control of hydroformylation technology is crucial to ensuring the security of the supply chain.

[0003] Propylene hydroformylation uses propylene (C3H6) and synthesis gas (CO / H2) as feedstocks, producing C4 aldehydes over a catalyst. Ideally, hydroformylation requires a 1:1 ratio of H2 / CO. However, controlling the synthesis gas ratio in practice is difficult. Excessive H2 can easily trigger the hydrogenation of propylene to propane (a side reaction), while excess CO inhibits the reaction rate. Furthermore, conventional processes have limited sources of synthesis gas, primarily relying on fossil fuel reforming, resulting in high carbon emissions and contradicting the trend toward green chemistry. Existing hydroformylation processes rely on external propylene as feedstock. As a petrochemical raw material, propylene's price is significantly affected by fluctuations in the crude oil market, resulting in high costs and instability associated with externally purchased propylene. Furthermore, propylene is a flammable gas, requiring high-pressure liquefaction for long-distance transportation, which poses significant safety risks and consumes a lot of energy. Overall, the production process for hydroformylation feedstock is complex, costly, and poses significant transportation safety risks.

[0004] With the rise of shale gas development, propane dehydrogenation (PDH) has gradually become a mainstream technology for propylene production. This process uses a catalyst to directly dehydrogenate propane to produce propylene and hydrogen (H2) as a by-product. It boasts excellent conversion rates and high propylene selectivity, with a near 1:1 ratio of propylene to hydrogen. The process technology is mature. However, the propylene produced requires high storage and transportation costs to downstream plants for production of high-value-added products. Furthermore, the hydrogen produced as a by-product of the near 1:1 reaction with propylene is often burned directly as fuel, rather than converted into high-value-added chemicals, resulting in a significant waste of resources.

[0005] In the prior art, Chinese patents CN 116178107 A and CN 116178107 B disclose a method for producing mixed alcohols by coupling two reaction processes of Fischer-Tropsch synthesis and hydroformylation. First, synthesis gas is converted into alkanes, olefins, alcohols, aldehydes, etc. in a Fischer-Tropsch synthesis reactor. Secondly, the obtained synthesis product is passed into a hydroformylation reactor to convert the olefins into aldehydes. Finally, hydrogenation is performed to obtain a mixture of alkanes and mixed alcohols, which is further distilled and separated to obtain mixed alcohols. The above patents all require specific and cumbersome processes to obtain synthesis gas in a specific proportion, and the Fischer-Tropsch synthesis reaction products involved are complex, which will undoubtedly increase the cost of obtaining raw materials and the cost of separating intermediate products. Summary of the Invention

[0006] The present invention discloses a propane dehydrogenation and propylene hydroformylation coupling system and process. The system couples propylene and hydrogen produced by a propane dehydrogenation reaction with propylene and hydrogen required for a propylene hydroformylation reaction as raw materials. This avoids the storage and transportation of propylene and hydrogen required for the hydroformylation process, as well as the production process of a single propylene and hydrogen product. This reduces the cost of complex processes and improves process efficiency.

[0007] The above-mentioned object of the present invention is achieved through the following technical solutions:

[0008] According to one aspect of the present invention, a propane dehydrogenation and hydroformylation coupling system is provided, comprising a propane dehydrogenation subsystem and a hydroformylation subsystem; wherein the propane dehydrogenation subsystem produces propylene and hydrogen through a propane dehydrogenation reaction unit (105); the propane dehydrogenation subsystem and the hydroformylation subsystem are coupled using a hydroformylation feed gas mixing unit (401); and the hydroformylation reaction unit (405) consumes propylene and hydrogen and produces n-butyraldehyde and isobutyraldehyde.

[0009] Furthermore, it includes a C4 removal distillation tower (101), a propane dehydrogenation raw gas mixing unit (102), a propane dehydrogenation raw gas heat exchange unit (103), a propane dehydrogenation raw gas preheating unit (104), a propane dehydrogenation reaction unit (105), a dehydrogenation reaction gas separation unit (106), a dehydrogenation reaction gas heat exchange unit (201), a dehydrogenation reaction gas precooling unit (202), a dehydrogenation reaction gas compression unit (203), a dehydrogenation reaction gas cooling box unit (204), a dehydrogenation reaction gas cold trap (205), a hydrogen separation unit (206), a hydrogen secondary separation and purification unit I (207), a hydrogen secondary separation and purification unit II (208), a C2 removal distillation unit (301), a C3 mixture pumping unit (302), a propylene propane distillation unit (303), a circulating propane extraction unit (304), a circulating propane preheating unit (30 5), propylene secondary separation and purification unit (306), hydroformylation feed gas mixing unit (401), circulating gas adding mixing unit (402), hydroformylation feed gas pre-compression unit (403), hydroformylation feed gas preheating unit (404), hydroformylation reaction unit (405), hydroformylation reactant separation unit I (406), hydroformylation reactant separation unit II (407), circulating catalyst extraction unit (408), hydroformylation reaction gas mixing unit (409), hydroformylation reaction gas compression unit (410), hydroformylation reaction gas preheating unit (411), de-feed gas distillation unit (412), circulating feed gas extraction unit (413), C4 product distillation unit (414), homogeneous catalyst mixing unit (501), catalyst pumping unit (502), catalyst preheating unit (503);

[0010] The inlet of the C4 removal distillation tower (101) is used to introduce the propane LPG raw material (R1); the top gas phase of the C4 removal distillation tower (101) is connected to the inlet of the propane dehydrogenation raw gas mixing unit (102); the bottom liquid phase outlet of the C4 removal distillation tower (101) is used to obtain the C4 and other heavy component products (1); the outlet of the propane dehydrogenation raw gas mixing unit (102) is connected to the inlet of the propane dehydrogenation raw gas heat exchange unit (103); the high temperature phase outlet of the propane dehydrogenation raw gas heat exchange unit (103) is connected to the inlet of the propane dehydrogenation raw gas heat exchange unit (103). The inlet of the propane dehydrogenation feed gas preheating unit (104) is connected, the outlet of the propane dehydrogenation feed gas preheating unit (104) is connected to the inlet of the propane dehydrogenation reaction unit (105), the outlet of the propane dehydrogenation reaction unit (105) is connected to the inlet of the dehydrogenation reaction gas separation unit (106), the solid phase outlet of the dehydrogenation reaction gas separation unit (106) obtains the carbon deposition (7) product, and the gas phase outlet of the dehydrogenation reaction gas separation unit (106) is connected to the inlet of the propane dehydrogenation feed gas heat exchange unit (103);

[0011] The low-temperature phase outlet of the propane dehydrogenation feed gas heat exchange unit (103) is connected to the inlet of the dehydrogenation reaction gas heat exchange unit (201), the outlet of the dehydrogenation reaction gas heat exchange unit (201) is connected to the inlet of the dehydrogenation reaction gas precooling unit (202), the outlet of the dehydrogenation reaction gas precooling unit (202) is connected to the inlet of the dehydrogenation reaction gas compression unit (203), the outlet of the dehydrogenation reaction gas compression unit (203) is connected to the compressed reaction gas inlet of the dehydrogenation reaction gas cooling box unit (204), the low-temperature gas outlet of the dehydrogenation reaction gas cooling box unit (204) is connected to the inlet of the dehydrogenation reaction gas cold trap (205), and the outlet of the dehydrogenation reaction gas cold trap (205) is connected to the The inlet of the hydrogen separation unit (206) is connected, the gas phase outlet of the hydrogen separation unit (206) is connected to the cryogenic gas inlet of the dehydrogenation reaction gas cooling box unit (204), the high-temperature gas outlet of the dehydrogenation reaction gas cooling box unit (204) is connected to the inlet of the hydrogen secondary separation and purification unit I (207), the first outlet of the hydrogen secondary separation and purification unit I (207) is connected to the inlet of the propane dehydrogenation raw gas mixing unit (102), the second outlet of the hydrogen secondary separation and purification unit I (207) is connected to the inlet of the hydrogen secondary separation and purification unit II (208), and the first outlet of the hydrogen secondary separation and purification unit II (208) obtains a hydrogen mixed gas (20);

[0012] The liquid phase outlet of the hydrogen separation unit (206) is connected to the inlet of the C2 removal distillation unit (301), the gas phase outlet of the C2 removal distillation unit (301) obtains the C2 light component gas (23), the liquid phase outlet of the C2 removal distillation unit (301) is connected to the inlet of the C3 mixture pumping unit (302), the outlet of the C3 mixture pumping unit (302) is connected to the inlet of the propylene propane distillation unit (303), and the gas phase outlet of the propylene propane distillation unit (303) is connected to the inlet of the circulating propane extraction unit (304). , the first outlet of the circulating propane production unit (304) obtains produced propane (27), the second outlet of the circulating propane production unit (304) is connected to the inlet of the circulating propane preheating unit (305), the outlet of the circulating propane preheating unit (305) is connected to the inlet of the propane dehydrogenation feed gas mixing unit (102), the liquid phase outlet of the propylene propane distillation unit (303) is connected to the inlet of the propylene secondary separation and purification unit (306), and the liquid phase outlet of the propylene secondary separation and purification unit (306) obtains the propylene impurity-removed product (31);

[0013] The second outlet of the hydrogen secondary separation and purification unit II (208) is connected to the first inlet of the hydroformylation feed gas mixing unit (401), the gas phase outlet of the propylene secondary separation and purification unit (306) is connected to the second inlet of the hydroformylation feed gas mixing unit (401), the third inlet of the hydroformylation feed gas mixing unit (401) is used to introduce carbon monoxide feed (R2), the outlet of the hydroformylation feed gas mixing unit (401) is connected to the first inlet of the recycle gas mixing unit (402), the outlet of the recycle gas mixing unit (402) is connected to the inlet of the hydroformylation feed gas pre-compression unit (403), and the The outlet of the hydroformylation feed gas precompression unit (403) is connected to the inlet of the hydroformylation feed gas preheating unit (404), the outlet of the hydroformylation feed gas preheating unit (404) is connected to the first inlet of the hydroformylation reaction unit (405), the outlet of the hydroformylation reaction unit (405) is connected to the inlet of the hydroformylation reactant separation unit I (406), the liquid phase outlet of the hydroformylation reactant separation unit I (406) is connected to the inlet of the hydroformylation reactant separation unit II (407), and the liquid phase outlet of the hydroformylation reactant separation unit II (407) is connected to the circulating catalyst extraction unit (408). The first outlet of the circulating catalyst extraction unit (408) extracts the homogeneous catalyst (41), the gas phase outlets of the hydroformylation reactant separation unit I (406) and the hydroformylation reactant separation unit II (407) are connected to the inlet of the hydroformylation reaction gas mixing unit (409), the outlet of the hydroformylation reaction gas mixing unit (409) is connected to the inlet of the hydroformylation reaction gas compression unit (410), the outlet of the hydroformylation reaction gas compression unit (410) is connected to the inlet of the hydroformylation reaction gas preheating unit (411), and the outlet of the hydroformylation reaction gas preheating unit (411) is connected to the outlet of the degassing raw gas purification unit (411). The inlet of the degassing unit (412) is connected to the inlet of the degassing unit (412), the gas phase outlet of the degassing unit (412) is connected to the inlet of the circulating raw gas extraction unit (413), the first outlet of the circulating raw gas extraction unit (413) is connected to the second inlet of the circulating gas adding mixing unit (402), the second outlet of the circulating raw gas extraction unit (413) extracts the circulating raw material (51), the liquid phase outlet of the degassing unit (412) is connected to the inlet of the C4 product distillation unit (414), the first outlet of the C4 product distillation unit obtains the isobutyraldehyde product (53), and the second outlet of the C4 product distillation unit obtains the normal butyraldehyde product (54);

[0014] The second outlet of the circulating catalyst extraction unit (408) is connected to the first inlet of the homogeneous catalyst mixing unit (501), the homogeneous catalyst feed (R3) is connected to the second inlet of the homogeneous catalyst mixing unit (501), the outlet of the homogeneous catalyst mixing unit (501) is connected to the inlet of the catalyst pumping unit (502), the outlet of the catalyst pumping unit (502) is connected to the inlet of the catalyst preheating unit (503), and the outlet of the catalyst preheating unit (503) is connected to the second inlet of the hydroformylation reaction unit (405).

[0015] According to another aspect of the present invention, a coupled process of propane dehydrogenation and hydroformylation is provided, comprising the following reaction process:

[0016] The propane LPG raw material (R1) enters a C4 removal distillation tower (101) to remove C4 heavy component liquid, and the C4 and other heavy component products (1) are obtained at the bottom liquid phase outlet of the C4 removal distillation tower (101), and the C3 component gas (2) is obtained at the top gas phase outlet of the C4 removal distillation tower (101);

[0017] The C3 component gas (2), split hydrogen II (18) and preheated circulating propane (29) enter the propane dehydrogenation raw gas mixing unit (102) to obtain a propane mixed gas (3);

[0018] The relatively low-temperature propane mixed gas (3) and the relatively high-temperature carbon removal reaction gas (8) are heat-exchanged in the propane dehydrogenation raw gas heat exchange unit (103) to obtain a relatively high-temperature heat-exchanged propane mixed gas (4) and a relatively low-temperature heat-exchanged cooling reaction gas I (9);

[0019] The heat exchange propane mixed gas (4) passes through a propane dehydrogenation feed gas preheating unit (104) to obtain a preheated propane mixed gas (5);

[0020] The preheated propane mixed gas (5) passes through a propane dehydrogenation reaction unit (105) and flows through a catalyst bed to react to obtain a propane dehydrogenation reaction gas (6);

[0021] The propane dehydrogenation reaction gas (6) passes through the dehydrogenation reaction gas separation unit (106) to obtain carbon deposits (7) and a relatively high-temperature gas phase carbon removal reaction gas (8);

[0022] The relatively low-temperature heat exchange and cooling reaction gas I (9) is passed through the dehydrogenation reaction gas heat exchange unit (201) and then heat-exchanged with circulating water to obtain the low-temperature heat exchange and cooling reaction gas II (10);

[0023] The heat exchange and cooling reaction gas II (10) is cooled by cooling water in the dehydrogenation reaction gas pre-cooling unit (202) to obtain the heat exchange and cooling reaction gas III (11);

[0024] The heat exchange and cooling reaction gas III (11) is compressed by the dehydrogenation reaction gas compression unit (203) to obtain a relatively high-pressure dehydrogenation reaction compressed gas (12);

[0025] The dehydrogenation reaction compressed gas (12) and the cryogenically separated circulating hydrogen (15) pass through the dehydrogenation reaction gas cooling box unit (204) to obtain a relatively low-temperature condensed product (13) and a relatively high-temperature heat exchange circulating hydrogen (16);

[0026] The condensed product (13) is passed through a dehydrogenation reaction gas cooling trap (205) to obtain a cryogenic product (14) at a lower temperature;

[0027] The cryogenic product (14) passes through a hydrogen separation unit (206) to obtain cryogenic separation circulating hydrogen (15) mainly composed of hydrogen and hydrogen-removed reaction gas (21);

[0028] The heat exchange cycle hydrogen (16) passes through the hydrogen secondary separation and purification unit I (207) to obtain split hydrogen I (17) and split hydrogen II (18);

[0029] The split hydrogen I (17) passes through the hydrogen secondary separation and purification unit II (208) to obtain secondary purified hydrogen (19) and a hydrogen mixed gas (20) mainly composed of hydrogen;

[0030] The split hydrogen II (18) enters the propane dehydrogenation feed gas mixing unit (102) to participate in the hydrogen cycle;

[0031] The dehydrogenated reaction gas (21) passes through the C2 removal distillation unit (301) to obtain a gaseous C2 light component gas (23) at the top of the tower, and a liquid C3 component reactant (22) is obtained in the bottom of the tower;

[0032] The C3 component reactant (22) enters the C3 mixture pumping unit (302) to obtain the pressurized pumped C3 component reactant (24);

[0033] The C3 component reactant (24) is pumped under pressure into the propylene propane distillation unit (303) to obtain distilled propylene (25) and circulating propane I (26);

[0034] Circulating propane I (26) enters the circulating propane production unit (304) to obtain produced propane (27) and circulating propane II (28);

[0035] The circulating propane II (28) passes through the circulating propane preheating unit (305) to obtain preheated circulating propane (29) to participate in the propane raw material circulation;

[0036] The distilled propylene (25) enters the propylene secondary separation and purification unit (306) to obtain a propylene impurity-removed product (31) and secondary purified propylene (30);

[0037] The secondary purified propylene (30), the secondary purified hydrogen (19) and the carbon monoxide feed (R2) enter the hydroformylation raw gas mixing unit (401) to obtain a fully mixed carbon monoxide / propylene / hydrogen mixed gas (32);

[0038] The carbon monoxide / propylene / hydrogen mixed gas (32) and the circulating carbon monoxide / propylene / hydrogen mixed gas II (52) enter the circulating gas mixing unit (402) and are mixed to obtain the circulating mixed gas (33);

[0039] Adding the circulating mixed gas (33) into the hydroformylation raw gas pre-compression unit (403) to obtain a compressed pre-compressed mixed gas (34);

[0040] The pre-compressed mixed gas (34) enters the hydroformylation raw gas preheating unit (404) to obtain the pre-compressed preheated mixed gas (35);

[0041] The pre-compressed and pre-heated mixed gas (35) and the pre-heated and pre-compressed catalyst (45) enter the hydroformylation reaction unit (405) to undergo a hydroformylation reaction to obtain a hydroformylation reaction gas (36);

[0042] The hydroformylation reaction gas (36) passes through the hydroformylation reactant separation unit I (406) to obtain a gas phase light component reaction gas (37) and a liquid phase heavy component reaction gas (38);

[0043] The heavy component reaction gas (38) passes through the hydroformylation reactant separation unit II (407) to obtain a gas phase secondary separation light component reaction gas (39) and a liquid phase circulating homogeneous catalyst I (40);

[0044] The liquid phase circulating homogeneous catalyst I (40) passes through the circulating catalyst extraction unit (408) to obtain the extracted homogeneous catalyst (41) and the circulating homogeneous catalyst II (42);

[0045] The circulating homogeneous catalyst II (42) and the fresh homogeneous catalyst feed (R3) enter the homogeneous catalyst mixing unit (501) and are fully mixed to obtain the fresh and circulating mixed homogeneous catalyst (43);

[0046] Fresh and recycled mixed homogeneous catalyst (43) is passed through a catalyst pumping unit (502) to obtain pre-compressed catalyst (44);

[0047] The pre-compressed catalyst (44) passes through the catalyst preheating unit (503) to obtain the preheated pre-compressed catalyst (45) to participate in the catalyst cycle;

[0048] The light component reaction gas (37) and the secondary separated light component reaction gas (39) enter the hydroformylation reaction gas mixing unit (409) to obtain a mixed light component reaction gas (46);

[0049] The mixed light component reaction gas (46) enters the hydroformylation reaction gas compression unit (410) to obtain the hydroformylation reaction compressed gas (47);

[0050] The hydroformylation reaction compressed gas (47) passes through the hydroformylation reaction gas preheating unit (411) to obtain preheated reaction compressed gas (48);

[0051] The preheated reaction compressed gas (48) enters the degassing and rectification unit (412) to obtain a liquid C4 product mixture (49) and a circulating carbon monoxide / propylene / hydrogen mixed gas I (50);

[0052] The circulating carbon monoxide / propylene / hydrogen mixed gas I (50) passes through the circulating raw material gas extraction unit (413) to obtain the extracted circulating raw material (51) and the circulating carbon monoxide / propylene / hydrogen mixed gas II (52) to participate in the reaction raw material circulation;

[0053] The C4 product mixture (49) is passed through a C4 product distillation unit (414) to obtain an isobutyraldehyde product (53) and an n-butyraldehyde product (54).

[0054] Furthermore, the operating conditions of the reactor in the propane dehydrogenation reaction unit (105) are a reaction temperature of 500-600°C, a reaction pressure of 0.1-0.5 MPaA, and a reaction space velocity of 100-1500 h -1 .

[0055] Furthermore, the flow ratio of carbon monoxide, propylene and hydrogen in the hydroformylation feed gas mixing unit (401), the recycle gas mixing unit (402) and the mixed flow path is any ratio.

[0056] Furthermore, the operating conditions of the reactor in the hydroformylation reaction unit (405) are a reaction temperature of 50-150°C and a reaction pressure of 1.5-2.5 MPaA.

[0057] Furthermore, the operating pressure of the degassing and rectification unit (412) is 1.5-2.5 MPaA.

[0058] Furthermore, the operating pressure of the C4 product distillation unit (414) is 0.1-0.2 MPaA.

[0059] The beneficial effects of the present invention are:

[0060] The coupled propane dehydrogenation and hydroformylation system and process of the present invention can simultaneously produce high-quality propylene and butyraldehyde. In the propane dehydrogenation system, the hydrogen from the PSA light component separation section and the propylene from the propylene-propylene separation section, after dehydrogenation, only need to be further purified and diverted before being mixed with CO as needed before entering the hydroformylation system to produce butyraldehyde. Compared to traditional propylene hydroformylation processes, this system avoids the cumbersome production processes of fossil fuel hydrogen production and propylene production, and also avoids the storage and transportation of propylene and hydrogen. The hydrogen generated by the propane dehydrogenation reaction can be utilized as a resource. By avoiding the storage and transportation of propylene and hydrogen required in the hydroformylation process, as well as the production process of a single propylene and hydrogen product, this coupled system and process reduces the costs associated with complex processes, reduces construction land, and achieves better economic benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0061] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the following briefly introduces the drawings required for use in the embodiments. It should be understood that the following drawings only illustrate certain embodiments of the present invention and therefore should not be regarded as limiting the scope of the present invention.

[0062] Figure 1 This is a structural schematic diagram of the propane dehydrogenation and hydroformylation coupling system and process provided by the present invention.

[0063] In the above figure, R1-propane LPG raw material, R2-carbon monoxide feed, R3-homogeneous catalyst feed, 1-C4 and other heavy component products, 2-C3 component gas, 3-propane mixed gas, 4-heat exchange propane mixed gas, 5-preheated propane mixed gas, 6-propane dehydrogenation reaction gas, 7-carbon deposition, 8-decarbon deposition removal reaction gas, 9-heat exchange and cooling reaction gas I, 10-heat exchange and cooling reaction gas II, 11-heat exchange and cooling reaction gas III, 12-dehydrogenation reaction compressed gas , 13-condensed product, 14-cryogenic product, 15-cryogenic separation circulating hydrogen, 16-heat exchange circulating hydrogen, 17-diverted hydrogen I, 18-diverted hydrogen II, 19-secondary purified hydrogen, 20-hydrogen mixed gas, 21-dehydrogenation reaction gas, 22-C3 component reactant, 23-C2 light component gas, 24-pressure pumping C3 component reactant, 25-distilled propylene, 26-circulating propane I, 27-produced propane, 28-circulating propane II , 29-preheating circulating propane, 30-secondary purification of propylene, 31-propylene impurity removal, 32-carbon monoxide / propylene / hydrogen mixed gas, 33-adding circulating mixed gas, 34-precompressed mixed gas, 35-precompressed preheated mixed gas, 36-hydroformylation reaction gas, 37-light component reaction gas, 38-heavy component reaction gas, 39-secondary separation of light component reaction gas, 40-circulating homogeneous catalyst I, 41-extraction of homogeneous catalyst, 42-circulating homogeneous catalyst II, 43-fresh and recycled mixed homogeneous catalyst, 44-precompressed catalyst, 45-preheated precompressed catalyst, 46-mixed light component reaction gas, 47-hydroformylation reaction compressed gas, 48-preheated reaction compressed gas, 49-C4 product mixture, 50-recycled carbon monoxide / propylene / hydrogen mixture I, 51-extracted recycled feedstock, 52-recycled carbon monoxide / propylene / hydrogen mixture II, 53-isobutyraldehyde product, 54-n-butyraldehyde product;

[0064] 101-C4 removal distillation tower, 102-propane dehydrogenation raw gas mixing unit, 103-propane dehydrogenation raw gas heat exchange unit, 104-propane dehydrogenation raw gas preheating unit, 105-propane dehydrogenation reaction unit, 106-dehydrogenation reaction gas separation unit, 201-dehydrogenation reaction gas heat exchange unit, 202-dehydrogenation reaction gas precooling unit, 203-dehydrogenation reaction gas compression unit, 204-dehydrogenation reaction gas cooling box unit, 205-dehydrogenation reaction gas cold trap, 206-hydrogen separation unit, 207-hydrogen secondary separation and purification unit I, 208-hydrogen secondary separation and purification unit II, 301-C2 removal distillation unit, 302-C3 mixture pumping unit, 303-propylene propane distillation unit, 304-circulating propane extraction unit, 305-circulating propane preheating unit, 3 06-propylene secondary separation and purification unit, 401-hydroformylation feed gas mixing unit, 402-recycled gas mixing unit, 403-hydroformylation feed gas pre-compression unit, 404-hydroformylation feed gas preheating unit, 405-hydroformylation reaction unit, 406-hydroformylation reactant separation unit I, 407-hydroformylation reactant separation unit II, 408-circulating catalyst extraction unit, 409-hydroformylation reaction gas mixing unit, 410-hydroformylation reaction gas compression unit, 411-hydroformylation reaction gas preheating unit, 412-de-feed gas distillation unit, 413-circulating feed gas extraction unit, 414-C4 product distillation unit, 501-homogeneous catalyst mixing unit, 502-catalyst pumping unit, 503-catalyst preheating unit. DETAILED DESCRIPTION

[0065] like Figure 1As shown, this embodiment provides a propane dehydrogenation and hydroformylation coupling system. It includes a C4 removal distillation tower 101, a propane dehydrogenation feed gas mixing unit 102, a propane dehydrogenation feed gas heat exchange unit 103, a propane dehydrogenation feed gas preheating unit 104, a propane dehydrogenation reaction unit 105, a dehydrogenation reaction gas separation unit 106, a dehydrogenation reaction gas heat exchange unit 201, a dehydrogenation reaction gas precooling unit 202, a dehydrogenation reaction gas compression unit 203, a dehydrogenation reaction gas cooling box unit 204, a dehydrogenation reaction gas cold trap 205, a hydrogen separation unit 206, a hydrogen secondary separation and purification unit I 207, a hydrogen secondary separation and purification unit II 208, a C2 removal distillation unit 301, a C3 mixture pumping unit 302, a propylene propane distillation unit 303, a circulating propane extraction unit 304, and a circulating propane preheating unit 305. Propylene secondary separation and purification unit 306, hydroformylation feed gas mixing unit 401, circulating gas adding mixing unit 402, hydroformylation feed gas pre-compression unit 403, hydroformylation feed gas preheating unit 404, hydroformylation reaction unit 405, hydroformylation reactant separation unit I 406, hydroformylation reactant separation unit II 407, circulating catalyst extraction unit 408, hydroformylation reaction gas mixing unit 409, hydroformylation reaction gas compression unit 410, hydroformylation reaction gas preheating unit 411, degassing feed gas distillation unit 412, circulating feed gas extraction unit 413, C4 product distillation unit 414, homogeneous catalyst mixing unit 501, catalyst pumping unit 502, catalyst preheating unit 503.

[0066] The inlet of the C4 removal distillation tower 101 is used to introduce propane LPG feedstock R1. The top gas phase outlet of the C4 removal distillation tower 101 is connected to the inlet of the propane dehydrogenation feed gas mixing unit 102. The bottom liquid phase outlet of the C4 removal distillation tower 101 is used to produce heavy components such as C4 product 1. The outlet of the propane dehydrogenation feed gas mixing unit 102 is connected to the inlet of the propane dehydrogenation feed gas heat exchange unit 103. The high-temperature phase outlet of the propane dehydrogenation feed gas heat exchange unit 103 is connected to the inlet of the propane dehydrogenation feed gas preheating unit 104. The outlet of the propane dehydrogenation feed gas preheating unit 104 is connected to the inlet of the propane dehydrogenation reaction unit 105. The outlet of the propane dehydrogenation reaction unit 105 is connected to the inlet of the dehydrogenation reaction gas separation unit 106. The solid phase outlet of the dehydrogenation reaction gas separation unit 106 produces the carbon deposit 7 product. The gas phase outlet of the dehydrogenation reaction gas separation unit 106 is connected to the inlet of the propane dehydrogenation feed gas heat exchange unit 103.

[0067] As a preferred embodiment, the operating conditions of the reactor in the propane dehydrogenation reaction unit 105 are a reaction temperature of 500-600°C, a reaction pressure of 0.1-0.5 MPaA, a reaction space velocity of 100-1500 h -1 .

[0068] In this embodiment, the reaction temperature in the propane dehydrogenation reaction unit 105 is 550°C, the reaction pressure is 0.1 MPaA, and the reaction space velocity is 1000 h -1 .

[0069] The low temperature phase outlet of the propane dehydrogenation feed gas heat exchange unit 103 is connected to the inlet of the dehydrogenation reaction gas heat exchange unit 201, the outlet of the dehydrogenation reaction gas heat exchange unit 201 is connected to the inlet of the dehydrogenation reaction gas precooling unit 202, the outlet of the dehydrogenation reaction gas precooling unit 202 is connected to the inlet of the dehydrogenation reaction gas compression unit 203, the outlet of the dehydrogenation reaction gas compression unit 203 is connected to the compressed reaction gas inlet of the dehydrogenation reaction gas cooling box unit 204, the low temperature gas outlet of the dehydrogenation reaction gas cooling box unit 204 is connected to the inlet of the dehydrogenation reaction gas cold trap 205, and the outlet of the dehydrogenation reaction gas cold trap 205 is connected to the hydrogen The inlet of the separation unit 206 is connected, the gas phase outlet of the hydrogen separation unit 206 is connected to the deep cold gas inlet of the dehydrogenation reaction gas cooling box unit 204, the high temperature gas outlet of the dehydrogenation reaction gas cooling box unit 204 is connected to the inlet of the hydrogen secondary separation and purification unit I 207, the first outlet of the hydrogen secondary separation and purification unit I 207 is connected to the inlet of the propane dehydrogenation raw gas mixing unit 102, the second outlet of the hydrogen secondary separation and purification unit I 207 is connected to the inlet of the hydrogen secondary separation and purification unit II 208, and the first outlet of the hydrogen secondary separation and purification unit II 208 obtains the hydrogen mixed gas 20.

[0070] The liquid phase outlet of the hydrogen separation unit 206 is connected to the inlet of the C2 removal distillation unit 301, the gas phase outlet of the C2 removal distillation unit 301 obtains the C2 light component gas 23, the liquid phase outlet of the C2 removal distillation unit 301 is connected to the inlet of the C3 mixture pumping unit 302, the outlet of the C3 mixture pumping unit 302 is connected to the inlet of the propylene propane distillation unit 303, the gas phase outlet of the propylene propane distillation unit 303 is connected to the inlet of the circulating propane production unit 304, the first outlet of the circulating propane production unit 304 obtains produced propane 27, the second outlet of the circulating propane production unit 304 is connected to the inlet of the circulating propane preheating unit 305, the outlet of the circulating propane preheating unit 305 is connected to the inlet of the propane dehydrogenation raw gas mixing unit 102, the liquid phase outlet of the propylene propane distillation unit 303 is connected to the inlet of the propylene secondary separation and purification unit 306, and the liquid phase outlet of the propylene secondary separation and purification unit 306 obtains the propylene impurity-removed product 31.

[0071] The second outlet of the hydrogen secondary separation and purification unit II 208 is connected to the first inlet of the hydroformylation feed gas mixing unit 401, the gas phase outlet of the propylene secondary separation and purification unit 306 is connected to the second inlet of the hydroformylation feed gas mixing unit 401, the third inlet of the hydroformylation feed gas mixing unit 401 is used to introduce carbon monoxide feed R2, the outlet of the hydroformylation feed gas mixing unit 401 is connected to the first inlet of the recycle gas mixing unit 402, the outlet of the recycle gas mixing unit 402 is connected to the inlet of the hydroformylation feed gas pre-compression unit 403, the hydroformylation feed gas pre-compression unit 403 is connected to the recycle gas mixing unit 402, and the recycle gas pre-compression unit 403 is connected to the recycle gas mixing unit 402. The outlet of the hydroformylation feed gas precompression unit 403 is connected to the inlet of the hydroformylation feed gas preheating unit 404, the outlet of the hydroformylation feed gas preheating unit 404 is connected to the first inlet of the hydroformylation reaction unit 405, the outlet of the hydroformylation reaction unit 405 is connected to the inlet of the hydroformylation reactant separation unit I 406, the liquid phase outlet of the hydroformylation reactant separation unit I 406 is connected to the inlet of the hydroformylation reactant separation unit II 407, the liquid phase outlet of the hydroformylation reactant separation unit II 407 is connected to the inlet of the circulating catalyst extraction unit 408, and the circulating catalyst is discharged from the circulating catalyst extraction unit 408. The first outlet of the catalyst extraction unit 408 obtains the extracted homogeneous catalyst 41, the gas phase outlets of the hydroformylation reactant separation unit I 406 and the hydroformylation reactant separation unit II 407 are connected to the inlet of the hydroformylation reaction gas mixing unit 409, the outlet of the hydroformylation reaction gas mixing unit 409 is connected to the inlet of the hydroformylation reaction gas compression unit 410, the outlet of the hydroformylation reaction gas compression unit 410 is connected to the inlet of the hydroformylation reaction gas preheating unit 411, and the outlet of the hydroformylation reaction gas preheating unit 411 is connected to the inlet of the degassing gas distillation unit 412. The gas phase outlet of the de-raw gas distillation unit 412 is connected to the inlet of the circulating raw gas production unit 413, the first outlet of the circulating raw gas production unit 413 is connected to the second inlet of the circulating gas mixing unit 402, the second outlet of the circulating raw gas production unit 413 obtains the produced circulating raw material 51, the liquid phase outlet of the de-raw gas distillation unit 412 is connected to the inlet of the C4 product distillation unit 414, the first outlet of the C4 product distillation unit 414 obtains the isobutyraldehyde product 53, and the second outlet of the C4 product distillation unit 414 obtains the normal butyraldehyde product 54.

[0072] As a preferred embodiment, the operating conditions of the reactor in the hydroformylation reaction unit 405 are a reaction temperature of 50-150° C. and a reaction pressure of 1.5-2.5 MPaA.

[0073] In this embodiment, the reaction temperature of the reactor in the hydroformylation reaction unit 405 is 90° C. and the pressure is 2.0 MPaA.

[0074] The second outlet of the circulating catalyst extraction unit 408 is connected to the first inlet of the homogeneous catalyst mixing unit 501, the homogeneous catalyst feed R3 is connected to the second inlet of the homogeneous catalyst mixing unit 501, the outlet of the homogeneous catalyst mixing unit 501 is connected to the inlet of the catalyst pumping unit 502, the outlet of the catalyst pumping unit 502 is connected to the inlet of the catalyst preheating unit 503, and the outlet of the catalyst preheating unit 503 is connected to the second inlet of the hydroformylation reaction unit 405.

[0075] Based on the propane dehydrogenation and hydroformylation coupling system of this embodiment, this embodiment also provides a propane dehydrogenation and hydroformylation coupling process, including the following reaction process:

[0076] Propane LPG feedstock R1 enters C4 removal distillation tower 101, where the propane LPG feedstock includes ethane, propane, butane, etc. The bottom liquid outlet of C4 removal distillation tower 101 produces C4 and other heavy components 1, primarily butane. The top gas outlet of C4 removal distillation tower 101 produces C3 component gas 2.

[0077] The C3 component gas 2, split hydrogen II 18 and preheated recycled propane 29 enter the propane dehydrogenation raw gas mixing unit 102 to obtain a propane mixed gas 3.

[0078] The relatively low temperature propane mixed gas 3 and the relatively high temperature carbon removal reaction gas 8 are heat exchanged in the propane dehydrogenation raw gas heat exchange unit 103 to obtain the relatively high temperature heat exchange propane mixed gas 4 and the relatively low temperature heat exchange cooling reaction gas I9.

[0079] The heat exchanged propane mixed gas 4 passes through the propane dehydrogenation feed gas preheating unit 104 to obtain a preheated propane mixed gas 5. The preheated propane mixed gas 5 passes through the propane dehydrogenation heterogeneous catalyst bed through the propane dehydrogenation reaction unit 105 to react and obtain a propane dehydrogenation reaction gas 6.

[0080] As a preferred embodiment, the operating conditions of the reactor in the propane dehydrogenation reaction unit 105 are a reaction temperature of 500-600°C, a reaction pressure of 0.1-0.5 MPaA, a reaction space velocity of 100-1500 h -1 .

[0081] In this embodiment, the reaction temperature in the propane dehydrogenation reaction unit 105 is 550°C, the reaction pressure is 0.1 MPaA, and the reaction space velocity is 1000 h -1 .

[0082] The propane dehydrogenation reaction gas 6 passes through the dehydrogenation reaction gas separation unit 106 to separate the carbon deposits in the reaction process to obtain carbon deposits 7 and a relatively high-temperature carbon-removed reaction gas 8 in the gas phase.

[0083] The relatively low-temperature heat exchange and cooling reaction gas I9 passes through the dehydrogenation reaction gas heat exchange unit 201 and is heat-exchanged with circulating water to obtain the low-temperature heat exchange and cooling reaction gas II10.

[0084] The heat exchange and temperature reduction reaction gas II10 is cooled by cooling water in the dehydrogenation reaction gas pre-cooling unit 202 to obtain the heat exchange and temperature reduction reaction gas III11.

[0085] The heat exchange and temperature reduction reaction gas III 11 is compressed by the dehydrogenation reaction gas compression unit 203 to obtain a relatively high-pressure dehydrogenation reaction compressed gas 12 .

[0086] The dehydrogenation reaction compressed gas 12 and the cryogenic separation circulating hydrogen 15 pass through the dehydrogenation reaction gas cooling box unit 204 to obtain a relatively low-temperature condensation product 13 and a relatively high-temperature heat exchange circulating hydrogen 16; the condensation product 13 passes through the dehydrogenation reaction gas cold trap 205 to obtain a lower-temperature cryogenic product 14; the cryogenic product 14 passes through the hydrogen separation unit 206 to obtain a cryogenic separation circulating hydrogen 15 mainly composed of hydrogen and a dehydrogenation reaction gas 21.

[0087] The heat exchange cycle hydrogen 16 passes through the hydrogen secondary separation and purification unit I 207 to obtain split hydrogen I 17 and split hydrogen II 18. The split hydrogen I 17 passes through the hydrogen secondary separation and purification unit II 208 to obtain secondary purified hydrogen 19 and a hydrogen mixture 20 mainly composed of hydrogen. The split hydrogen II 18 enters the propane dehydrogenation raw gas mixing unit 102 to participate in the hydrogen cycle.

[0088] The dehydrogenated reaction gas 21 obtained by the hydrogen separation unit 206 passes through the C2 removal distillation unit 301 to obtain the gaseous C2 light component gas 23 at the top of the tower, and the liquid C3 component reactant 22 is obtained in the bottom of the tower. The C3 component reactant 22 enters the C3 mixture pumping unit 302 to obtain the pressurized pumped C3 component reactant 24, and the pressurized pumped C3 component reactant 24 enters the propylene propane distillation unit 303 to obtain distilled propylene 25 and circulating propane I 26.

[0089] Circulating propane I 26 enters the circulating propane production unit 304 to obtain produced propane 27 and circulating propane II 28. Circulating propane II 28 passes through the circulating propane preheating unit 305 to obtain preheated circulating propane 29 to participate in the propane raw material cycle.

[0090] The distilled propylene 25 obtained by the propylene propane distillation unit 303 enters the propylene secondary separation and purification unit 306 to obtain the propylene impurity-free product 31 and the secondary purified propylene 30.

[0091] The secondary purified propylene 30 and the secondary purified hydrogen 19 obtained in the hydrogen secondary separation and purification unit II 208 and the carbon monoxide feed R2 enter the hydroformylation raw gas mixing unit 401 to obtain a fully mixed carbon monoxide / propylene / hydrogen mixed gas 32. The carbon monoxide / propylene / hydrogen mixed gas 32 and the recycled carbon monoxide / propylene / hydrogen mixed gas II 52 enter the recycled gas mixing unit 402 to be mixed to obtain the recycled mixed gas 33.

[0092] In this embodiment, the flow ratio of carbon monoxide:propylene:hydrogen in the hydroformylation feed gas mixing unit 401, the recycle gas mixing unit 402, the carbon monoxide / propylene / hydrogen mixed gas 32, and the recycle mixed gas 33 is 1:1:1.

[0093] The recycled mixed gas 33 enters the hydroformylation raw gas precompression unit 403 to obtain a compressed precompressed mixed gas 34. The precompressed mixed gas 34 enters the hydroformylation raw gas preheating unit 404 to obtain a precompressed preheated mixed gas 35. The precompressed preheated mixed gas 35 and the preheated precompressed catalyst 45 enter the hydroformylation reaction unit 405 for a hydroformylation reaction to obtain a hydroformylation reaction gas 36.

[0094] As a preferred embodiment, the operating conditions of the reactor in the hydroformylation reaction unit 405 are a reaction temperature of 50-150° C. and a reaction pressure of 1.5-2.5 MPaA.

[0095] In this embodiment, the reaction temperature of the reactor in the hydroformylation reaction unit 405 is 90° C. and the pressure is 2.0 MPaA.

[0096] The hydroformylation reaction gas 36 passes through the hydroformylation reactant separation unit I 406 to obtain a gaseous light component reaction gas 37 and a liquid-phase heavy component reaction gas 38. The heavy component reaction gas 38 passes through the hydroformylation reactant separation unit II 407 to obtain a gaseous secondary separation light component reaction gas 39 and a liquid-phase circulating homogeneous catalyst I 40. The liquid-phase circulating homogeneous catalyst I 40 passes through the circulating catalyst extraction unit 408 to obtain a extracted homogeneous catalyst 41 and a circulating homogeneous catalyst II 42.

[0097] The circulating homogeneous catalyst II 42 and the fresh homogeneous catalyst feed R3 enter the homogeneous catalyst mixing unit 501 together and are fully mixed to obtain a fresh and circulating mixed homogeneous catalyst 43. The fresh and circulating mixed homogeneous catalyst 43 passes through the catalyst pumping unit 502 to obtain a pre-compressed catalyst 44. The pre-compressed catalyst 44 passes through the catalyst preheating unit 503 to obtain a preheated pre-compressed catalyst 45 to participate in the catalyst circulation.

[0098] The gaseous light component reaction gas 37 obtained by the hydroformylation reactant separation unit I 406 and the secondary separated light component reaction gas 39 enter the hydroformylation reaction gas mixing unit 409 to obtain mixed light component reaction gas 46. The mixed light component reaction gas 46 enters the hydroformylation reaction gas compression unit 410 to obtain hydroformylation reaction compressed gas 47. The hydroformylation reaction compressed gas 47 passes through the hydroformylation reaction gas preheating unit 411 to obtain preheated reaction compressed gas 48.

[0099] The preheated reaction compressed gas 48 enters the de-raw gas distillation unit 412 to obtain a liquid C4 product mixture 49 and a circulating carbon monoxide / propylene / hydrogen mixed gas I 50. The circulating carbon monoxide / propylene / hydrogen mixed gas I 50 passes through the circulating raw material gas extraction unit 413 to obtain the extracted circulating raw material 51 and the circulating carbon monoxide / propylene / hydrogen mixed gas II 52 to participate in the reaction raw material circulation.

[0100] As a preferred embodiment, the operating pressure of the degassing and rectification unit 412 is 1.5-2.5 MPaA.

[0101] In this embodiment, the operating pressure of the degassing rectification unit 412 is 2.0 MPaA.

[0102] The liquid C4 product mixture 49 obtained by the degassing and rectification unit 412 is passed through the C4 product rectification unit 414 to obtain an isobutyraldehyde product 53 and a normal butyraldehyde product 54.

[0103] As a preferred embodiment, the operating pressure of the C4 product distillation unit 414 is 0.1-0.2 MPaA.

[0104] In this embodiment, the operating pressure of the C4 product distillation unit 414 is 0.2 MPaA.

[0105] In summary, the coupled propane dehydrogenation and hydroformylation system and process of the present invention utilizes the characteristics of the propane dehydrogenation and propylene hydroformylation reactions to achieve coupling, eliminating the storage and transportation of propylene and hydrogen required in the hydroformylation process, as well as the production of propylene and hydrogen alone. This system improves energy efficiency, enhances the atomic economy of raw materials, reduces costs associated with complex processes, and reduces construction land. Furthermore, it enables long-term stable production and achieves better economic benefits.

[0106] Although the preferred embodiments of the present invention have been described above in conjunction with the accompanying drawings, the present invention is not limited to the above-mentioned specific embodiments. The above-mentioned specific embodiments are merely illustrative and not restrictive. Under the guidance of the present invention, ordinary technicians in this field can also make many forms of specific changes without departing from the scope of protection of the present invention and the claims. These all fall within the scope of protection of the present invention.

Claims

1. A propane dehydrogenation and hydroformylation coupling system, characterized in that: The invention comprises a propane dehydrogenation subsystem and a hydroformylation subsystem; wherein the propane dehydrogenation subsystem produces propylene and hydrogen through a propane dehydrogenation reaction unit (105); the propane dehydrogenation subsystem and the hydroformylation subsystem are coupled using a hydroformylation raw gas mixing unit (401); the propylene and hydrogen are consumed by the hydroformylation reaction unit (405) and n-butyraldehyde and isobutyraldehyde are produced.

2. A propane dehydrogenation and hydroformylation coupling system according to claim 1, characterized in that: The invention comprises a C4 removal distillation tower (101), a propane dehydrogenation raw gas mixing unit (102), a propane dehydrogenation raw gas heat exchange unit (103), a propane dehydrogenation raw gas preheating unit (104), a propane dehydrogenation reaction unit (105), a dehydrogenation reaction gas separation unit (106), a dehydrogenation reaction gas heat exchange unit (201), a dehydrogenation reaction gas precooling unit (202), a dehydrogenation reaction gas compression unit (203), a dehydrogenation reaction gas cooling box unit (204), a dehydrogenation reaction gas cold trap (205), a hydrogen separation unit (206), a hydrogen secondary separation and purification unit I (207), a hydrogen secondary separation and purification unit II (208), a C2 removal distillation unit (301), a C3 mixture pumping unit (302), a propylene propane distillation unit (303), a circulating propane extraction unit (304), and a circulating propane preheating unit (305). , propylene secondary separation and purification unit (306), hydroformylation feed gas mixing unit (401), circulating gas adding mixing unit (402), hydroformylation feed gas pre-compression unit (403), hydroformylation feed gas preheating unit (404), hydroformylation reaction unit (405), hydroformylation reactant separation unit I (406), hydroformylation reactant separation unit II (407), circulating catalyst extraction unit (408), hydroformylation reaction gas mixing unit (409), hydroformylation reaction gas compression unit (410), hydroformylation reaction gas preheating unit (411), de-feed gas distillation unit (412), circulating feed gas extraction unit (413), C4 product distillation unit (414), homogeneous catalyst mixing unit (501), catalyst pumping unit (502), catalyst preheating unit (503); The inlet of the C4 removal distillation tower (101) is used to introduce the propane LPG raw material (R1); the top gas phase of the C4 removal distillation tower (101) is connected to the inlet of the propane dehydrogenation raw gas mixing unit (102); the bottom liquid phase outlet of the C4 removal distillation tower (101) is used to obtain the C4 and other heavy component products (1); the outlet of the propane dehydrogenation raw gas mixing unit (102) is connected to the inlet of the propane dehydrogenation raw gas heat exchange unit (103); the high temperature phase outlet of the propane dehydrogenation raw gas heat exchange unit (103) is connected to the inlet of the propane dehydrogenation raw gas heat exchange unit (103). The inlet of the propane dehydrogenation feed gas preheating unit (104) is connected, the outlet of the propane dehydrogenation feed gas preheating unit (104) is connected to the inlet of the propane dehydrogenation reaction unit (105), the outlet of the propane dehydrogenation reaction unit (105) is connected to the inlet of the dehydrogenation reaction gas separation unit (106), the solid phase outlet of the dehydrogenation reaction gas separation unit (106) obtains the carbon deposition (7) product, and the gas phase outlet of the dehydrogenation reaction gas separation unit (106) is connected to the inlet of the propane dehydrogenation feed gas heat exchange unit (103); The low-temperature phase outlet of the propane dehydrogenation feed gas heat exchange unit (103) is connected to the inlet of the dehydrogenation reaction gas heat exchange unit (201), the outlet of the dehydrogenation reaction gas heat exchange unit (201) is connected to the inlet of the dehydrogenation reaction gas precooling unit (202), the outlet of the dehydrogenation reaction gas precooling unit (202) is connected to the inlet of the dehydrogenation reaction gas compression unit (203), the outlet of the dehydrogenation reaction gas compression unit (203) is connected to the compressed reaction gas inlet of the dehydrogenation reaction gas cooling box unit (204), the low-temperature gas outlet of the dehydrogenation reaction gas cooling box unit (204) is connected to the inlet of the dehydrogenation reaction gas cold trap (205), and the outlet of the dehydrogenation reaction gas cold trap (205) is connected to the The inlet of the hydrogen separation unit (206) is connected, the gas phase outlet of the hydrogen separation unit (206) is connected to the cryogenic gas inlet of the dehydrogenation reaction gas cooling box unit (204), the high-temperature gas outlet of the dehydrogenation reaction gas cooling box unit (204) is connected to the inlet of the hydrogen secondary separation and purification unit I (207), the first outlet of the hydrogen secondary separation and purification unit I (207) is connected to the inlet of the propane dehydrogenation raw gas mixing unit (102), the second outlet of the hydrogen secondary separation and purification unit I (207) is connected to the inlet of the hydrogen secondary separation and purification unit II (208), and the first outlet of the hydrogen secondary separation and purification unit II (208) obtains a hydrogen mixed gas (20); The liquid phase outlet of the hydrogen separation unit (206) is connected to the inlet of the C2 removal distillation unit (301), the gas phase outlet of the C2 removal distillation unit (301) obtains the C2 light component gas (23), the liquid phase outlet of the C2 removal distillation unit (301) is connected to the inlet of the C3 mixture pumping unit (302), the outlet of the C3 mixture pumping unit (302) is connected to the inlet of the propylene propane distillation unit (303), and the gas phase outlet of the propylene propane distillation unit (303) is connected to the inlet of the circulating propane extraction unit (304). , the first outlet of the circulating propane production unit (304) obtains produced propane (27), the second outlet of the circulating propane production unit (304) is connected to the inlet of the circulating propane preheating unit (305), the outlet of the circulating propane preheating unit (305) is connected to the inlet of the propane dehydrogenation feed gas mixing unit (102), the liquid phase outlet of the propylene propane distillation unit (303) is connected to the inlet of the propylene secondary separation and purification unit (306), and the liquid phase outlet of the propylene secondary separation and purification unit (306) obtains the propylene impurity-removed product (31); The second outlet of the hydrogen secondary separation and purification unit II (208) is connected to the first inlet of the hydroformylation feed gas mixing unit (401), the gas phase outlet of the propylene secondary separation and purification unit (306) is connected to the second inlet of the hydroformylation feed gas mixing unit (401), the third inlet of the hydroformylation feed gas mixing unit (401) is used to introduce carbon monoxide feed (R2), the outlet of the hydroformylation feed gas mixing unit (401) is connected to the first inlet of the recycle gas mixing unit (402), the outlet of the recycle gas mixing unit (402) is connected to the inlet of the hydroformylation feed gas pre-compression unit (403), and the The outlet of the hydroformylation feed gas precompression unit (403) is connected to the inlet of the hydroformylation feed gas preheating unit (404), the outlet of the hydroformylation feed gas preheating unit (404) is connected to the first inlet of the hydroformylation reaction unit (405), the outlet of the hydroformylation reaction unit (405) is connected to the inlet of the hydroformylation reactant separation unit I (406), the liquid phase outlet of the hydroformylation reactant separation unit I (406) is connected to the inlet of the hydroformylation reactant separation unit II (407), and the liquid phase outlet of the hydroformylation reactant separation unit II (407) is connected to the circulating catalyst extraction unit (408). The first outlet of the circulating catalyst extraction unit (408) extracts the homogeneous catalyst (41), the gas phase outlets of the hydroformylation reactant separation unit I (406) and the hydroformylation reactant separation unit II (407) are connected to the inlet of the hydroformylation reaction gas mixing unit (409), the outlet of the hydroformylation reaction gas mixing unit (409) is connected to the inlet of the hydroformylation reaction gas compression unit (410), the outlet of the hydroformylation reaction gas compression unit (410) is connected to the inlet of the hydroformylation reaction gas preheating unit (411), and the outlet of the hydroformylation reaction gas preheating unit (411) is connected to the outlet of the degassing raw gas purification unit (411). The inlet of the degassing unit (412) is connected to the inlet of the degassing unit (412), the gas phase outlet of the degassing unit (412) is connected to the inlet of the circulating raw gas extraction unit (413), the first outlet of the circulating raw gas extraction unit (413) is connected to the second inlet of the circulating gas adding mixing unit (402), the second outlet of the circulating raw gas extraction unit (413) extracts the circulating raw material (51), the liquid phase outlet of the degassing unit (412) is connected to the inlet of the C4 product distillation unit (414), the first outlet of the C4 product distillation unit obtains the isobutyraldehyde product (53), and the second outlet of the C4 product distillation unit obtains the normal butyraldehyde product (54); The second outlet of the circulating catalyst extraction unit (408) is connected to the first inlet of the homogeneous catalyst mixing unit (501), the homogeneous catalyst feed (R3) is connected to the second inlet of the homogeneous catalyst mixing unit (501), the outlet of the homogeneous catalyst mixing unit (501) is connected to the inlet of the catalyst pumping unit (502), the outlet of the catalyst pumping unit (502) is connected to the inlet of the catalyst preheating unit (503), and the outlet of the catalyst preheating unit (503) is connected to the second inlet of the hydroformylation reaction unit (405).

3. A propane dehydrogenation and hydroformylation coupling process, characterized in that: The reaction process includes the following: The propane LPG raw material (R1) enters a C4 removal distillation tower (101) to remove C4 heavy component liquid, and the C4 and other heavy component products (1) are obtained at the bottom liquid phase outlet of the C4 removal distillation tower (101), and the C3 component gas (2) is obtained at the top gas phase outlet of the C4 removal distillation tower (101); The C3 component gas (2), split hydrogen II (18) and preheated circulating propane (29) enter the propane dehydrogenation raw gas mixing unit (102) to obtain a propane mixed gas (3); The relatively low-temperature propane mixed gas (3) and the relatively high-temperature carbon removal reaction gas (8) are heat-exchanged in the propane dehydrogenation raw gas heat exchange unit (103) to obtain a relatively high-temperature heat-exchanged propane mixed gas (4) and a relatively low-temperature heat-exchanged cooling reaction gas I (9); The heat exchange propane mixed gas (4) passes through a propane dehydrogenation feed gas preheating unit (104) to obtain a preheated propane mixed gas (5); The preheated propane mixed gas (5) passes through a propane dehydrogenation reaction unit (105) and flows through a catalyst bed to react to obtain a propane dehydrogenation reaction gas (6); The propane dehydrogenation reaction gas (6) passes through the dehydrogenation reaction gas separation unit (106) to obtain carbon deposits (7) and a relatively high-temperature gas phase carbon removal reaction gas (8); The relatively low-temperature heat exchange and cooling reaction gas I (9) is passed through the dehydrogenation reaction gas heat exchange unit (201) and then heat-exchanged with circulating water to obtain the low-temperature heat exchange and cooling reaction gas II (10); The heat exchange and cooling reaction gas II (10) is cooled by cooling water in the dehydrogenation reaction gas pre-cooling unit (202) to obtain the heat exchange and cooling reaction gas III (11); The heat exchange and cooling reaction gas III (11) is compressed by the dehydrogenation reaction gas compression unit (203) to obtain a relatively high-pressure dehydrogenation reaction compressed gas (12); The dehydrogenation reaction compressed gas (12) and the cryogenically separated circulating hydrogen (15) pass through the dehydrogenation reaction gas cooling box unit (204) to obtain a relatively low-temperature condensed product (13) and a relatively high-temperature heat exchange circulating hydrogen (16); The condensed product (13) is passed through a dehydrogenation reaction gas cooling trap (205) to obtain a cryogenic product (14) at a lower temperature; The cryogenic product (14) passes through a hydrogen separation unit (206) to obtain cryogenic separation circulating hydrogen (15) mainly composed of hydrogen and hydrogen-removed reaction gas (21); The heat exchange cycle hydrogen (16) passes through the hydrogen secondary separation and purification unit I (207) to obtain split hydrogen I (17) and split hydrogen II (18); The split hydrogen I (17) passes through the hydrogen secondary separation and purification unit II (208) to obtain secondary purified hydrogen (19) and a hydrogen mixed gas (20) mainly composed of hydrogen; The split hydrogen II (18) enters the propane dehydrogenation feed gas mixing unit (102) to participate in the hydrogen cycle; The dehydrogenated reaction gas (21) passes through the C2 removal distillation unit (301) to obtain a gaseous C2 light component gas (23) at the top of the tower, and a liquid C3 component reactant (22) is obtained in the bottom of the tower; The C3 component reactant (22) enters the C3 mixture pumping unit (302) to obtain the pressurized pumped C3 component reactant (24); The C3 component reactant (24) is pumped under pressure into the propylene propane distillation unit (303) to obtain distilled propylene (25) and circulating propane I (26); Circulating propane I (26) enters the circulating propane production unit (304) to obtain produced propane (27) and circulating propane II (28); The circulating propane II (28) passes through the circulating propane preheating unit (305) to obtain preheated circulating propane (29) to participate in the propane raw material circulation; The distilled propylene (25) enters the propylene secondary separation and purification unit (306) to obtain a propylene impurity-removed product (31) and secondary purified propylene (30); The secondary purified propylene (30), the secondary purified hydrogen (19) and the carbon monoxide feed (R2) enter the hydroformylation raw gas mixing unit (401) to obtain a fully mixed carbon monoxide / propylene / hydrogen mixed gas (32); The carbon monoxide / propylene / hydrogen mixed gas (32) and the circulating carbon monoxide / propylene / hydrogen mixed gas II (52) enter the circulating gas mixing unit (402) and are mixed to obtain the circulating mixed gas (33); Adding the circulating mixed gas (33) into the hydroformylation raw gas pre-compression unit (403) to obtain a compressed pre-compressed mixed gas (34); The pre-compressed mixed gas (34) enters the hydroformylation raw gas preheating unit (404) to obtain the pre-compressed preheated mixed gas (35); The pre-compressed and pre-heated mixed gas (35) and the pre-heated and pre-compressed catalyst (45) enter the hydroformylation reaction unit (405) to undergo a hydroformylation reaction to obtain a hydroformylation reaction gas (36); The hydroformylation reaction gas (36) passes through the hydroformylation reactant separation unit I (406) to obtain a gas phase light component reaction gas (37) and a liquid phase heavy component reaction gas (38); The heavy component reaction gas (38) passes through the hydroformylation reactant separation unit II (407) to obtain a gas phase secondary separation light component reaction gas (39) and a liquid phase circulating homogeneous catalyst I (40); The liquid phase circulating homogeneous catalyst I (40) passes through the circulating catalyst extraction unit (408) to obtain the extracted homogeneous catalyst (41) and the circulating homogeneous catalyst II (42); The circulating homogeneous catalyst II (42) and the fresh homogeneous catalyst feed (R3) enter the homogeneous catalyst mixing unit (501) and are fully mixed to obtain the fresh and circulating mixed homogeneous catalyst (43); Fresh and recycled mixed homogeneous catalyst (43) is passed through a catalyst pumping unit (502) to obtain pre-compressed catalyst (44); The pre-compressed catalyst (44) passes through the catalyst preheating unit (503) to obtain the preheated pre-compressed catalyst (45) to participate in the catalyst cycle; The light component reaction gas (37) and the secondary separated light component reaction gas (39) enter the hydroformylation reaction gas mixing unit (409) to obtain a mixed light component reaction gas (46); The mixed light component reaction gas (46) enters the hydroformylation reaction gas compression unit (410) to obtain the hydroformylation reaction compressed gas (47); The hydroformylation reaction compressed gas (47) passes through the hydroformylation reaction gas preheating unit (411) to obtain preheated reaction compressed gas (48); The preheated reaction compressed gas (48) enters the degassing and rectification unit (412) to obtain a liquid C4 product mixture (49) and a circulating carbon monoxide / propylene / hydrogen mixed gas I (50); The circulating carbon monoxide / propylene / hydrogen mixed gas I (50) passes through the circulating raw material gas extraction unit (413) to obtain the extracted circulating raw material (51) and the circulating carbon monoxide / propylene / hydrogen mixed gas II (52) to participate in the reaction raw material circulation; The C4 product mixture (49) is passed through a C4 product distillation unit (414) to obtain an isobutyraldehyde product (53) and an n-butyraldehyde product (54).

4. A propane dehydrogenation and hydroformylation coupling process according to claim 3, characterized in that: The operating conditions of the reactor in the propane dehydrogenation reaction unit (105) are reaction temperature 500-600°C, reaction pressure 0.1-0.5 MPaA, reaction space velocity 100-1500h -1 .

5. A propane dehydrogenation and hydroformylation coupling process according to claim 3, characterized in that: The flow ratio of carbon monoxide, propylene and hydrogen in the hydroformylation feed gas mixing unit (401), the recycle gas mixing unit (402) and the mixed flow path is any ratio.

6. A coupled process of propane dehydrogenation and hydroformylation according to claim 3, characterized in that: The operating conditions of the reactor in the hydroformylation reaction unit (405) are a reaction temperature of 50-150°C and a reaction pressure of 1.5-2.5 MPaA.

7. A coupled process of propane dehydrogenation and hydroformylation according to claim 3, characterized in that: The operating pressure of the degassing and rectification unit (412) is 1.5-2.5 MPaA.

8. The coupled process of propane dehydrogenation and hydroformylation according to claim 3, characterized in that: The operating pressure of the C4 product distillation unit (414) is 0.1-0.2 MPaA.

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