Propane dehydrogenation, propane dry reforming 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, propane dry reforming and hydroformylation coupling system and a propane dehydrogenation, propane dry reforming and hydroformylation coupling process, which realize coupling of propane dehydrogenation reaction and propane dry reforming reaction by co-feeding carbon dioxide in a propane dehydrogenation reaction process. Further, propylene generated by propane dehydrogenation reaction and synthesis gas generated by propane dry reforming reaction are coupled with downstream hydroformylation reaction, so that butyraldehyde with a higher additional value can be generated from the raw materials propane and CO2 in one step. According to the method, links such as storage and transportation when propylene, hydrogen and carbon monoxide required by a hydroformylation process are used as raw materials and a tedious production process of single propylene, hydrogen and carbon monoxide are avoided, and meanwhile, carbon dioxide is recycled, so that the atom economy energy utilization efficiency is improved, the equipment investment and operation cost are reduced, and the method is suitable for industrial production. And the construction land is reduced, the process intensity is improved, the operation is easier, and the economic and environment-friendly benefits are 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, propane dry reforming and propylene hydroformylation. Background Art

[0002] Propylene hydroformylation is a core reaction in the organic synthesis industry for producing high-value-added 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. As the world's largest plasticizer producer (accounting for over 60% of production capacity), China's independent and controllable 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 hydrogenation of propylene to propane (a side reaction), while excess CO inhibits the reaction rate. Furthermore, conventional processes have limited synthesis gas sources, primarily relying on fossil fuel reforming. This requires high energy consumption and requires maintaining high temperatures (700-1000°C). External heating energy accounts for 60-70% of the total synthesis gas cost, and thermal efficiency is low, with actual efficiency only approximately 65-75%. A significant amount of heat is lost as waste heat, contradicting the trend toward green chemical production. Existing hydroformylation processes rely on external supplies of propylene and synthesis gas. As a petrochemical raw material, propylene's price is significantly affected by fluctuations in the crude oil market, making externally purchased propylene expensive and unstable. 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 problems of hydroformylation raw materials include complex production process, high cost, and high transportation safety risks.

[0004] With the rise of shale gas development, propane dehydrogenation (PDH) has become a mainstream technology for propylene production. 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 byproduct of the near-1:1 reaction with propylene is often directly burned as fuel, rather than converted into high-value chemicals. This results in low propane atomic utilization and significant resource waste.

[0005] In the prior art, Chinese patents CN 116178107 A and CN 116178107 B disclose a method for producing mixed alcohols by coupling the two reaction processes of Fischer-Tropsch synthesis and hydroformylation. First, the 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 a specific ratio of C3H6 / CO / H2. It is impossible to obtain C3H6, CO, and H2 simultaneously from a single source, 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 coupled process of propane dehydrogenation, propane dry reforming and hydroformylation. In the process of propane dehydrogenation, CO2 is introduced as a reaction raw material. A propane dry reforming reaction occurs simultaneously with the propane dehydrogenation reaction, and C3H6, CO and H2 are produced. These are coupled with a downstream hydroformylation reaction as raw materials, thereby avoiding the storage and transportation of C3H6, CO and H2 required in the hydroformylation process and the production process of single propylene and synthesis gas. This improves the atomic economy of propane, reduces the high energy consumption and economic costs caused by the complicated process and independent production of synthesis gas, and improves the process concentration.

[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, propane dry reforming and hydroformylation coupling system is provided, comprising a propane dehydrogenation subsystem, a propane dry reforming subsystem and a hydroformylation subsystem; wherein the propane dehydrogenation subsystem and the propane dry reforming subsystem are coupled via a propane dehydrogenation coupling dry reforming reaction unit (105) to co-produce propylene and synthesis gas; the propylene produced by the propane dehydrogenation subsystem and the synthesis gas produced by the propane dry reforming subsystem are coupled via a hydroformylation feed gas mixing unit (401) to the hydroformylation subsystem to co-produce n-butyraldehyde and isobutyraldehyde.

[0009] Furthermore, it includes a C4 removal distillation unit (101), a propane and carbon dioxide premixing unit (102), a propane dehydrogenation coupled dry reforming raw gas heat exchange unit (103), a propane dehydrogenation coupled dry reforming raw gas preheating unit (104), a propane dehydrogenation coupled dry reforming reaction unit (105), a dehydrogenation coupled dry reforming reaction gas separation unit (106), a dehydrogenation coupled dry reforming reaction gas heat exchange unit (201), a water separation unit (202), a dehydrogenation coupled dry reforming reaction gas precooling unit (203 ), dehydrogenation coupled dry reforming reaction gas compression unit (204), dehydrogenation coupled dry reforming reaction gas cooling box unit (205), dehydrogenation coupled dry reforming reaction gas cooling trap (206), synthesis gas hydrocarbon separation unit (207), hydrogen carbon monoxide separation unit (208), carbon monoxide production unit (209), hydrogen production unit (210), carbon oxide hydrocarbon distillation unit (301), C3 mixture pumping unit (302), propylene propane distillation unit (303), circulating propane production unit Element (304), circulating propane preheating unit (305), propylene extraction unit (306), propylene secondary separation and purification unit (307), hydroformylation raw gas mixing unit (401), hydroformylation raw gas preheating unit I (402), adding circulating gas mixing unit (403), hydroformylation raw gas precompression unit (404), hydroformylation raw gas preheating unit II (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), degassing feed gas distillation unit (413), circulating feed gas extraction unit (414), C4 product distillation unit (415), homogeneous catalyst mixing unit (501), homogeneous catalyst pumping unit (502), homogeneous catalyst preheating unit (503);

[0010] The inlet of the C4 removal distillation unit (101) is used to introduce the reaction raw material propane LPG (R1), the top gas phase of the C4 removal distillation unit (101) is connected to the first inlet of the propane and carbon dioxide premixing unit (102), the second inlet of the propane and carbon dioxide premixing unit (102) is connected to the carbon dioxide feed (R2), and the bottom liquid phase outlet of the C4 removal distillation unit (101) is used to obtain C4 and other heavy component products (1); the outlet of the propane and carbon dioxide premixing unit (102) is connected to the inlet of the propane dehydrogenation coupled dry reforming raw gas heat exchange unit (103), and the outlet of the propane dehydrogenation coupled dry reforming raw gas heat exchange unit (103) is connected to the inlet of the propane dehydrogenation coupled dry reforming raw gas heat exchange unit (103). The high-temperature phase outlet is connected to the inlet of the propane dehydrogenation coupled dry reforming raw gas preheating unit (104), the outlet of the propane dehydrogenation coupled dry reforming raw gas preheating unit (104) is connected to the inlet of the propane dehydrogenation coupled dry reforming reaction unit (105), the outlet of the propane dehydrogenation coupled dry reforming reaction unit (105) is connected to the inlet of the dehydrogenation coupled dry reforming reaction gas separation unit (106), the solid phase outlet of the dehydrogenation coupled dry reforming reaction gas separation unit (106) obtains the carbon deposition product (7), and the gas phase outlet of the dehydrogenation coupled dry reforming reaction gas separation unit (106) is connected to the inlet of the propane dehydrogenation coupled dry reforming raw gas heat exchange unit (103);

[0011] The low temperature phase outlet of the propane dehydrogenation coupled dry reforming feed gas heat exchange unit (103) is connected to the inlet of the dehydrogenation coupled dry reforming reaction gas heat exchange unit (201), the outlet of the dehydrogenation coupled dry reforming reaction gas heat exchange unit (201) is connected to the inlet of the water separation unit (202), the liquid phase outlet of the water separation unit (202) obtains the water vapor (12) product, the gas phase outlet of the water separation unit (202) is connected to the inlet of the dehydrogenation coupled dry reforming reaction gas precooling unit (203) The outlet of the dehydrogenation-coupled dry reforming reaction gas precooling unit (203) is connected to the inlet of the dehydrogenation-coupled dry reforming reaction gas compression unit (204), the outlet of the dehydrogenation-coupled dry reforming reaction gas compression unit (204) is connected to the compressed reaction gas inlet of the dehydrogenation-coupled dry reforming reaction gas cooling box unit (205), the low-temperature gas outlet of the dehydrogenation-coupled dry reforming reaction gas cooling box unit (205) is connected to the inlet of the dehydrogenation-coupled dry reforming reaction gas cold trap (206), and the dehydrogenation-coupled dry reforming reaction gas cooling box unit (205) is connected to the inlet of the dehydrogenation-coupled dry reforming reaction gas cold trap (206). The outlet of the hydrogen-coupled dry reforming reaction gas cold trap (206) is connected to the inlet of the synthesis gas hydrocarbon separation unit (207), the gas phase outlet of the synthesis gas hydrocarbon separation unit (207) is connected to the deep cold gas inlet of the dehydrogenation-coupled dry reforming reaction gas cold box unit (205), the high temperature gas outlet of the dehydrogenation-coupled dry reforming reaction gas cold box unit (205) is connected to the inlet of the hydrogen-carbon monoxide separation unit (208), and the liquid phase outlet of the hydrogen-carbon monoxide separation unit (208) is connected to the inlet of the hydrogen-carbon monoxide separation unit (208). to C2 and other light component gases (22), the first gas phase outlet of the hydrogen and carbon monoxide separation unit (208) is connected to the inlet of the carbon monoxide production unit (209), the first outlet of the carbon monoxide production unit (209) obtains the produced carbon monoxide product (25), the second gas phase outlet of the hydrogen and carbon monoxide separation unit (208) is connected to the inlet of the hydrogen production unit (210), and the first outlet of the hydrogen production unit (210) obtains the produced hydrogen product (24);

[0012] The liquid phase outlet of the synthesis gas hydrocarbon separation unit (207) is connected to the inlet of the carbon oxide hydrocarbon distillation unit (301), the gas phase outlet of the oxide hydrocarbon distillation unit (301) obtains a carbon monoxide and carbon dioxide mixed gas (28), the liquid phase outlet of the oxide hydrocarbon 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 first outlet of the propylene propane distillation unit (303) is connected to the inlet of the circulating propane production unit (304), and the first outlet of the circulating propane production unit (304) obtains produced propane. (32), 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 and carbon dioxide premixing unit (102), the second outlet of the propylene propane distillation unit (303) is connected to the inlet of the propylene production unit (306), the first outlet of the propylene production unit (306) obtains the produced propylene product (35), the second outlet of the propylene production unit (306) is connected to the inlet of the propylene secondary separation and purification unit (307), and the liquid phase outlet of the propylene secondary separation and purification unit (307) obtains the propylene impurity-removed product (38);

[0013] The second outlet of the carbon monoxide extraction unit (209) is connected to the first inlet of the hydroformylation feed gas mixing unit (401), the second outlet of the hydrogen extraction unit (210) is connected to the second inlet of the hydroformylation feed gas mixing unit (401), the gas phase outlet of the propylene secondary separation and purification unit (307) is connected to the third inlet of the hydroformylation feed gas mixing unit (401), the outlet of the hydroformylation feed gas mixing unit (401) is connected to the inlet of the hydroformylation feed gas preheating unit I (402), the outlet of the hydroformylation feed gas preheating unit I (402) is connected to the inlet of the recycle gas mixing unit (403), and the recycle gas mixing unit (403) is connected to the inlet of the hydroformylation feed gas preheating unit I (402). The outlet of the element (403) is connected to the inlet of the hydroformylation raw gas precompression unit (404), the outlet of the hydroformylation raw gas precompression unit (404) is connected to the inlet of the hydroformylation raw gas preheating unit II (405), the outlet of the hydroformylation raw gas preheating unit II (405) is connected to the first inlet of the hydroformylation reaction unit (406), the outlet of the hydroformylation reaction unit (406) is connected to the inlet of the hydroformylation reactant separation unit I (407), the liquid phase outlet of the hydroformylation reactant separation unit I (407) is connected to the inlet of the hydroformylation reactant separation unit II (408), and the hydroformylation reactant separation unit II (408) is connected to the inlet of the hydroformylation reactant separation unit II (408). ) is connected to the inlet of the circulating catalyst extraction unit (409), the first outlet of the circulating catalyst extraction unit (409) obtains the extracted homogeneous catalyst (49), the gaseous phase outlets of the hydroformylation reactant separation unit I (407) and the hydroformylation reactant separation unit II (408) are connected to the inlet of the hydroformylation reaction gas mixing unit (410), the outlet of the hydroformylation reaction gas mixing unit (410) is connected to the inlet of the hydroformylation reaction gas compression unit (411), the outlet of the hydroformylation reaction gas compression unit (411) is connected to the inlet of the hydroformylation reaction gas preheating unit (412), and the hydroformylation reaction gas preheating unit (412) is connected to the inlet of the hydroformylation reaction gas compression unit (411). The outlet of the degassing unit (413) is connected to the inlet of the degassing unit (413), the gas phase outlet of the degassing unit (413) is connected to the inlet of the circulating raw gas extraction unit (414), the first outlet of the circulating raw gas extraction unit (414) is connected to the second inlet of the adding circulating gas mixing unit (403), the second outlet of the circulating raw gas extraction unit (414) obtains the extracted circulating raw material (58), the liquid phase outlet of the degassing unit (413) is connected to the inlet of the C4 product distillation unit (415), the first outlet of the C4 product distillation unit obtains the isobutyraldehyde product (61), and the second outlet of the C4 product distillation unit obtains the normal butyraldehyde product (62);

[0014] The second outlet of the circulating catalyst extraction unit (409) 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 (406).

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

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

[0017] The C3 component gas (2), carbon dioxide feed (18) and preheated circulating propane (34) enter the propane and carbon dioxide premixing unit (102) to obtain a propane carbon dioxide 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 coupled dry reforming raw gas heat exchange unit (103) to obtain the relatively high temperature heat exchange propane carbon dioxide mixed gas (4) and the relatively low temperature heat exchange cooling reaction gas I (9);

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

[0020] The preheated propane-carbon dioxide mixed gas (5) passes through a propane dehydrogenation coupled dry reforming reaction unit (105) and flows through a catalyst bed to react, thereby obtaining a propane dehydrogenation coupled dry reforming reaction gas (6);

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

[0022] The relatively low-temperature heat exchange and cooling reaction gas I (9) is passed through the dehydrogenation coupled dry reforming 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) passes through the water separation unit (202) to obtain water vapor (12) product and dehydrated reaction gas (11);

[0024] The dehydrated reaction gas (11) is cooled by cooling water in a dehydrogenation coupled dry reforming reaction gas precooling unit (203) to obtain a condensed product I (13);

[0025] The condensed product I (13) is compressed by the dehydrogenation coupled dry reforming reaction gas compression unit (204) to obtain a relatively high-pressure pre-compressed reaction gas (14);

[0026] The pre-compressed reaction gas (14) and the hydrogen-carbon monoxide mixed gas (17) are coupled to the dehydrogenation dry reforming reaction gas cooling box unit (205) to obtain a relatively low-temperature condensed product II (15) and a relatively high-temperature heat exchange-heated hydrogen-carbon monoxide mixed gas (19);

[0027] The condensed product II (15) is subjected to a dehydrogenation-coupled dry reforming reaction gas cooling trap (206) to obtain a lower temperature cryogenic product (16);

[0028] The cryogenic product (16) passes through a synthesis gas hydrocarbon separation unit (207) to obtain a hydrogen and carbon monoxide mixture (17) and a C3 mixture (18);

[0029] The heat exchanged and heated hydrogen and carbon monoxide mixed gas (19) as described above passes through the hydrogen and carbon monoxide separation unit (208) to obtain a carbon monoxide mixed gas (20), a hydrogen mixed gas (21), and C2 and other light component gas products (22);

[0030] The carbon monoxide mixed gas (20) passes through the carbon monoxide extraction unit (209) to obtain the extracted carbon monoxide product (25) and the hydroformylation carbon monoxide raw gas (26);

[0031] As described above, the hydrogen mixed gas (21) enters the hydrogen extraction unit (210) to obtain extracted hydrogen (24) and hydroformylation hydrogen feed gas (23);

[0032] As described above, the C3 mixture (18) passes through the carbon oxide hydrocarbon distillation unit (301) to obtain a gaseous carbon monoxide and carbon dioxide mixed gas product (28) at the top of the tower, and a liquid carbon monoxide and carbon dioxide C3 mixture (27) is obtained in the bottom of the tower;

[0033] The carbon monoxide and carbon dioxide C3 mixture (27) is fed into the C3 mixture pumping unit (302) to obtain a pressurized pumped C3 heavy component mixture (29);

[0034] The C3 heavy component mixture (29) is pumped under pressure into the propylene propane distillation unit (303) to obtain distilled propylene I (30) and circulating propane I (31);

[0035] Circulating propane I (31) enters the circulating propane production unit (304) to obtain produced propane (32) and circulating propane II (33);

[0036] The circulating propane II (33) passes through the circulating propane preheating unit (305) to obtain preheated circulating propane (34) to participate in the propane raw material circulation;

[0037] As described above, the distilled propylene I (30) enters the propylene production unit (306) to obtain produced propylene (35) and distilled propylene II (36);

[0038] The propylene II (36) is distilled and enters the propylene secondary separation and purification unit (307) to obtain a propylene impurity-free product (38) and a hydroformylation propylene feed gas (37);

[0039] The hydroformylation hydrogen feed gas (23), the hydroformylation carbon monoxide feed gas (26) and the hydroformylation propylene feed gas (37) enter the hydroformylation feed gas mixing unit (401) to obtain a fully mixed carbon monoxide / propylene / hydrogen mixed gas (39);

[0040] The carbon monoxide / propylene / hydrogen mixed gas (39) enters the hydroformylation feed gas preheating unit I (402) to obtain a primary preheated mixed gas (40);

[0041] The primary preheated mixed gas (40) and the circulating carbon monoxide / propylene / hydrogen mixed gas II (59) enter the circulating gas mixing unit (403) and are mixed to obtain the circulating mixed gas (41);

[0042] Adding the circulating mixed gas (41) into the hydroformylation raw gas pre-compression unit (404) to obtain a compressed pre-compressed mixed gas (42);

[0043] The pre-compressed mixed gas (42) enters the hydroformylation raw gas preheating unit I (405) to obtain a secondary preheated mixed gas (43);

[0044] The secondary preheated mixed gas (43) and the preheated precompressed catalyst (53) enter the hydroformylation reaction unit (406) to undergo a hydroformylation reaction to obtain a hydroformylation reaction gas (44);

[0045] The hydroformylation reaction gas (44) passes through the hydroformylation reactant separation unit I (407) to obtain a gas phase light component reaction gas (45) and a liquid phase heavy component reaction gas (46);

[0046] The heavy component reaction gas (46) passes through the hydroformylation reactant separation unit II (408) to obtain a gas phase secondary separation light component reaction gas (47) and a liquid phase circulating catalyst I (48);

[0047] The circulating catalyst I (48) passes through the circulating catalyst extraction unit (409) to obtain the extracted homogeneous catalyst (49) and the circulating homogeneous catalyst II (50);

[0048] The circulating homogeneous catalyst II (50) 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 (51);

[0049] Fresh and recycled mixed homogeneous catalyst (51) is passed through a catalyst pumping unit (502) to obtain a pre-compressed catalyst (52);

[0050] The pre-compressed catalyst (52) passes through the catalyst preheating unit (503) to obtain the preheated pre-compressed catalyst (53) to participate in the catalyst cycle;

[0051] As described above, the light component reaction gas (45) and the secondary separated light component reaction gas (47) enter the hydroformylation reaction gas mixing unit (410) to obtain a mixed light component reaction gas (54);

[0052] The mixed light component reaction gas (54) enters the hydroformylation reaction gas compression unit (411) to obtain pre-compressed reaction gas (55);

[0053] The pre-compressed reaction gas (55) passes through the hydroformylation reaction gas preheating unit (412) to obtain preheated reaction compressed gas (56);

[0054] The preheated reaction compressed gas (56) enters the degassing and rectification unit (413) to obtain a liquid C4 product mixture (60) and a circulating carbon monoxide / propylene / hydrogen mixed gas I (57);

[0055] The circulating carbon monoxide / propylene / hydrogen mixed gas I (57) passes through the circulating raw material gas extraction unit (414) to obtain the extracted circulating raw material (58) and the circulating carbon monoxide / propylene / hydrogen mixed gas II (59) to participate in the reaction raw material circulation;

[0056] The C4 product mixture (60) is passed through a C4 product distillation unit (415) to obtain an isobutyraldehyde product (61) and a normal butyraldehyde product (62).

[0057] Furthermore, propane dehydrogenation and propane dry reforming reactions occur in a propane dehydrogenation coupled dry reforming reaction unit (105).

[0058] Furthermore, the flow ratio of the feed gas propane to carbon dioxide in the propane dehydrogenation coupled dry reforming reaction unit (105) is 0.5-10.

[0059] Furthermore, the operating conditions of the reactor in the propane dehydrogenation coupled dry reforming reaction unit (105) are a reaction temperature of 500-700°C, a reaction pressure of 0.1-0.5 MPaA, and a reaction space velocity of 100-1500 h -1 .

[0060] Furthermore, the flow ratio of carbon monoxide, propylene and hydrogen in the hydroformylation feed gas mixing unit (401), the recycle gas mixing unit (403) and the mixed flow path, such as the carbon monoxide / propylene / hydrogen mixed gas (39), the primary preheated mixed gas (40) and the recycle mixed gas (41), is any ratio.

[0061] Furthermore, the operating conditions of the reactor in the hydroformylation reaction unit (406) are a reaction temperature of 50-150°C and a reaction pressure of 1.5-2.5 MPaA.

[0062] Furthermore, the operating pressure of the degassing and rectification unit (413) is 1.5-2.5 MPaA.

[0063] Furthermore, the operating pressure of the C4 product distillation unit (415) is 0.1-0.2 MPaA.

[0064] The beneficial effects of the present invention are:

[0065] The coupled propane dehydrogenation, propane dry reforming, and hydroformylation system and process of the present invention can produce high-quality propylene and synthesis gas while simultaneously co-producing butyraldehyde. After the dehydrogenation reaction in the propane dehydrogenation and propane dry reforming systems, the hydrogen and carbon monoxide from the PSA light component separation section and the propylene from the propane-propylene separation section only need to be further purified and split before being mixed as needed before entering the hydroformylation system to produce butyraldehyde. Compared to traditional propylene hydroformylation processes, this system avoids the cumbersome production process of producing synthesis gas and propylene from fossil fuels, and also avoids the storage and transportation of propylene, hydrogen, and carbon monoxide. The hydrogen generated by the propane dehydrogenation reaction and the CO2 in the feedstock are simultaneously utilized as carbon sources. By avoiding the storage and transportation of propylene and synthesis gas required in the hydroformylation process, as well as the production process of a single product of propylene, hydrogen, and carbon monoxide, this coupled system and process reduces the costs associated with complex processes, reduces construction land, and offers a more environmentally friendly and economically efficient device. BRIEF DESCRIPTION OF THE DRAWINGS

[0066] 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.

[0067] Figure 1This is a structural schematic diagram of the propane dehydrogenation, propane dry reforming and hydroformylation coupling system and process provided by the present invention.

[0068] In the above figure, R1-propane LPG feed, 1-C4 and other heavy component products, 2-C3 component gas, R2-carbon dioxide feed, 3-propane carbon dioxide mixed gas, 4-heat exchange propane carbon dioxide mixed gas, 5-preheated propane carbon dioxide mixed gas, 6-propane dehydrogenation coupled dry reforming reaction gas, 7-carbon deposition, 8-decarbonization reaction gas, 9-heat exchange and cooling reaction gas I, 10-heat exchange and cooling reaction gas II, 11-dehydration reaction gas, 12-water vapor, 13-condensed product I, 14-precompression reaction gas, 15-condensed product II, 16 - Cryogenic products, 17- Hydrogen and carbon monoxide mixture, 18- C3 and other mixtures, 19- Heat exchange and heating hydrogen and carbon monoxide mixture, 20- Carbon monoxide mixture, 21- Hydrogen mixture, 22- C2 and other light component gases, 23- Hydroformylation hydrogen feed gas, 24- Produced hydrogen, 25- Produced carbon monoxide, 26- Hydroformylation carbon monoxide feed gas, 27- Carbon monoxide and carbon dioxide C3 mixture removed, 28- Carbon monoxide and carbon dioxide mixture, 29- Pressurized pumping of C3 heavy component mixture, 30- Distillation propylene I, 31- Circulating propane I, 32-produced propane, 33-circulating propane II, 34-preheated circulating propane, 35-produced propylene, 36-rectified propylene II, 37-hydroformylation propylene feed gas, 38-propylene impurity removal, 39-carbon monoxide / propylene / hydrogen mixed gas, 40-primary preheated mixed gas, 41-recirculating mixed gas, 42-precompressed mixed gas, 43-secondary preheated mixed gas, 44-hydroformylation reaction gas, 45-light component reaction gas, 46-heavy component reaction gas, 47-secondary separation of light component reaction gas, 48-circulating catalyst I, 49-extracted homogeneous catalyst, 50-circulated homogeneous catalyst II, R3-homogeneous catalyst feed, 51-fresh and recycled mixed homogeneous catalyst, 52-precompressed catalyst, 53-preheated precompressed catalyst, 54-mixed light component reaction gas, 55-precompressed reaction gas, 56-preheated precompressed reaction gas, 57-circulating carbon monoxide / propylene / hydrogen mixture I, 58-extracted circulating raw material, 59-circulating carbon monoxide / propylene / hydrogen mixture II, 60-C4 product mixture, 61-isobutyraldehyde product, 62-n-butyraldehyde product.

[0069] 101-C4 removal distillation unit, 102-propane and carbon dioxide premixing unit, 103-propane dehydrogenation coupled dry reforming feed gas heat exchange unit, 104-propane dehydrogenation coupled dry reforming feed gas preheating unit, 105-propane dehydrogenation coupled dry reforming reaction unit, 106-dehydrogenation coupled dry reforming reaction gas separation unit, 201-dehydrogenation coupled dry reforming reaction gas heat exchange unit, 202-water separation unit, 203-dehydrogenation coupled dry reforming reaction gas precooling unit, 20 4-dehydrogenation coupled dry reforming reaction gas compression unit, 205-dehydrogenation coupled dry reforming reaction gas cooling box unit, 206-dehydrogenation coupled dry reforming reaction gas cooling trap, 207-synthesis gas hydrocarbon separation unit, 208-hydrogen carbon monoxide separation unit, 209-carbon monoxide production unit, 210-hydrogen production unit, 301-carbon oxide hydrocarbon distillation unit, 302-C3 mixture pumping unit, 303-propylene propane distillation unit, 304-circulating propane production Output unit, 305-circulating propane preheating unit, 306-propylene extraction unit, 307-propylene secondary separation and purification unit, 401-hydroformylation feed gas mixing unit, 402-hydroformylation feed gas preheating unit I, 403-recycled gas mixing unit, 404-hydroformylation feed gas precompression unit, 405-hydroformylation feed gas preheating unit II, 406-hydroformylation reaction unit, 407-hydroformylation reactant separation unit I, 408- Hydroformylation reactant separation unit II, 409-circulating catalyst extraction unit, 410-hydroformylation reaction gas mixing unit, 411-hydroformylation reaction gas compression unit, 412-hydroformylation reaction gas preheating unit, 413-de-feed gas distillation unit, 414-circulating feed gas extraction unit, 415-C4 product distillation unit, 501-homogeneous catalyst mixing unit, 502-homogeneous catalyst pumping unit, 503-homogeneous catalyst preheating unit. DETAILED DESCRIPTION

[0070] like Figure 1As shown, this embodiment provides a propane dehydrogenation and propane dry reforming and hydroformylation coupling system, including a C4 removal distillation unit 101, a propane and carbon dioxide premixing unit 102, a propane dehydrogenation coupled dry reforming feed gas heat exchange unit 103, a propane dehydrogenation coupled dry reforming feed gas preheating unit 104, a propane dehydrogenation coupled dry reforming reaction unit 105, a dehydrogenation coupled dry reforming reaction gas separation unit 106, a dehydrogenation coupled dry reforming reaction gas heat exchange unit 201, and a moisture Separation unit 202, dehydrogenation coupled dry reforming reaction gas precooling unit 203, dehydrogenation coupled dry reforming reaction gas compression unit 204, dehydrogenation coupled dry reforming reaction gas cooling box unit 205, dehydrogenation coupled dry reforming reaction gas cold trap 206, synthesis gas hydrocarbon separation unit 207, hydrogen and carbon monoxide separation unit 208, carbon monoxide production unit 209, hydrogen production unit 210, carbon oxide hydrocarbon distillation unit 301, C3 mixture pumping unit 302, propylene Propane distillation unit 303, circulating propane extraction unit 304, circulating propane preheating unit 305, propylene extraction unit 306, propylene secondary separation and purification unit 307, hydroformylation feed gas mixing unit 401, hydroformylation feed gas preheating unit I 402, circulating gas mixing unit 403, hydroformylation feed gas precompression unit 404, hydroformylation feed gas preheating unit II 405, hydroformylation reaction unit 406, hydroformylation reactant separation unit Element 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, degassing feed gas distillation unit 413, circulating feed gas extraction unit 414, C4 product distillation unit 415, homogeneous catalyst mixing unit 501, homogeneous catalyst pumping unit 502, homogeneous catalyst preheating unit 503.

[0071] The inlet of the C4 removal distillation unit 101 is used to introduce the reaction raw material propane LPG R1, the top gas phase of the C4 removal distillation unit 101 is connected to the first inlet of the propane and carbon dioxide premixing unit 102, the second inlet of the propane and carbon dioxide premixing unit 102 is connected to the carbon dioxide feed R2, and the bottom liquid phase outlet of the C4 removal distillation unit 101 is used to obtain C4 and other heavy component products 1. The outlet of the propane and carbon dioxide premixing unit 102 is connected to the inlet of the propane dehydrogenation coupled dry reforming raw gas heat exchange unit 103, the high-temperature phase outlet of the propane dehydrogenation coupled dry reforming raw gas heat exchange unit 103 is connected to the inlet of the propane dehydrogenation coupled dry reforming raw gas preheating unit 104, the outlet of the propane dehydrogenation coupled dry reforming raw gas preheating unit 104 is connected to the inlet of the propane dehydrogenation coupled dry reforming reaction unit 105, the outlet of the propane dehydrogenation coupled dry reforming reaction unit 105 is connected to the inlet of the dehydrogenation coupled dry reforming reaction gas separation unit 106, the solid phase outlet of the dehydrogenation coupled dry reforming reaction gas separation unit 106 obtains the carbon deposit product 7, and the gas phase outlet of the dehydrogenation coupled dry reforming reaction gas separation unit 106 is connected to the inlet of the propane dehydrogenation coupled dry reforming raw gas heat exchange unit 103.

[0072] The propane dehydrogenation and propane dry reforming reactions occur in the same coupled reactor, namely the propane dehydrogenation coupled dry reforming reaction unit 105 .

[0073] As a preferred embodiment, the flow ratio of the feed gas propane to carbon dioxide in the propane dehydrogenation coupled dry reforming reaction unit 105 is 0.5-10.

[0074] As a preferred embodiment, the operating conditions of the reactor in the propane dehydrogenation coupled dry reforming reaction unit 105 are a reaction temperature of 500-700°C, a reaction pressure of 0.1-0.5 MPaA, a reaction space velocity of 100-1500 h -1 .

[0075] In this embodiment, the flow ratio of the feed gas propane to carbon dioxide in the propane dehydrogenation coupled dry reforming reaction unit 105 is 1.5; the operating conditions of the reactor in the propane dehydrogenation coupled dry reforming reaction unit 105 are a reaction temperature of 500°C, a reaction pressure of 0.1 MPaA, and a reaction space velocity of 1000 h -1 .

[0076] The low-temperature phase outlet of the propane dehydrogenation-coupled dry reforming feed gas heat exchange unit 103 is connected to the inlet of the dehydrogenation-coupled dry reforming reaction gas heat exchange unit 201, the outlet of the dehydrogenation-coupled dry reforming reaction gas heat exchange unit 201 is connected to the inlet of the water separation unit 202, the liquid phase outlet of the water separation unit 202 obtains water vapor 12 product, the gas phase outlet of the water separation unit 202 is connected to the inlet of the dehydrogenation-coupled dry reforming reaction gas precooling unit 203, the outlet of the dehydrogenation-coupled dry reforming reaction gas precooling unit 203 is connected to the inlet of the dehydrogenation-coupled dry reforming reaction gas compression unit 204, the outlet of the dehydrogenation-coupled dry reforming reaction gas compression unit 204 is connected to the compressed reaction gas inlet of the dehydrogenation-coupled dry reforming reaction gas cooling box unit 205, and the low-temperature gas outlet of the dehydrogenation-coupled dry reforming reaction gas cooling box unit 205 is connected to the inlet of the dehydrogenation-coupled dry reforming reaction gas cold trap 206. The outlet of the dehydrogenation-coupled dry reforming reaction gas cold trap 206 is connected to the inlet of the synthesis gas hydrocarbon separation unit 207, the gas phase outlet of the synthesis gas hydrocarbon separation unit 207 is connected to the deep cold gas inlet of the dehydrogenation-coupled dry reforming reaction gas cold box unit 205, the high-temperature gas outlet of the dehydrogenation-coupled dry reforming reaction gas cold box unit 205 is connected to the inlet of the hydrogen-carbon monoxide separation unit 208, the liquid phase outlet of the hydrogen-carbon monoxide separation unit 208 obtains light component gas 22 such as C2, the first gas phase outlet of the hydrogen-carbon monoxide separation unit 208 is connected to the inlet of the carbon monoxide production unit 209, the first outlet of the carbon monoxide production unit 209 obtains the produced carbon monoxide product 25, the second gas phase outlet of the hydrogen-carbon monoxide separation unit 208 is connected to the inlet of the hydrogen production unit 210, and the first outlet of the hydrogen production unit 210 obtains the produced hydrogen 24 product.

[0077] The liquid phase outlet of the synthesis gas hydrocarbon separation unit 207 is connected to the inlet of the carbon oxide hydrocarbon distillation unit 301, and the gas phase outlet of the carbon oxide hydrocarbon distillation unit 301 obtains the carbon monoxide and carbon dioxide mixed gas 28. The liquid phase outlet of the carbon oxide hydrocarbon distillation unit 301 is connected to the inlet of the C3 mixture pumping unit 302, and the outlet of the C3 mixture pumping unit 302 is connected to the inlet of the propylene propane distillation unit 303. The first outlet of the propylene propane distillation unit 303 is connected to the inlet of the circulating propane production unit 304, and the first outlet of the circulating propane production unit 304 obtains the produced propane. Propane 32, 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 third inlet of the propane and carbon dioxide premixing unit 102, the second outlet of the propylene propane distillation unit 303 is connected to the inlet of the propylene production unit 306, the first outlet of the propylene production unit 306 obtains the produced propylene 35 product, the second outlet of the propylene production unit 306 is connected to the inlet of the propylene secondary separation and purification unit 307, and the liquid phase outlet of the propylene secondary separation and purification unit 307 obtains the propylene impurity-removed 38 product.

[0078] The second outlet of the carbon monoxide extraction unit 209 is connected to the first inlet of the hydroformylation feed gas mixing unit 401, the second outlet of the hydrogen extraction unit 210 is connected to the second inlet of the hydroformylation feed gas mixing unit 401, the gas phase outlet of the propylene secondary separation and purification unit 307 is connected to the third inlet of the hydroformylation feed gas mixing unit 401, the outlet of the hydroformylation feed gas mixing unit 401 is connected to the inlet of the hydroformylation feed gas preheating unit I 402, the outlet of the hydroformylation feed gas preheating unit I 402 is connected to the first inlet of the recycle gas mixing unit 403, and the recycle gas mixing unit The outlet of element 403 is connected to the inlet of hydroformylation feed gas precompression unit 404, the outlet of hydroformylation feed gas precompression unit 404 is connected to the inlet of hydroformylation feed gas preheating unit II 405, the outlet of hydroformylation feed gas preheating unit II 405 is connected to the first inlet of hydroformylation reaction unit 406, the outlet of hydroformylation reaction unit 406 is connected to the inlet of hydroformylation reactant separation unit I 407, the liquid phase outlet of hydroformylation reactant separation unit I 407 is connected to the inlet of hydroformylation reactant separation unit II 408, and the outlet of hydroformylation reactant separation unit II 408 is connected to the inlet of hydroformylation reactant separation unit II 408. The liquid phase outlet is connected to the inlet of the circulating catalyst extraction unit 409, and the first outlet of the circulating catalyst extraction unit 409 obtains the extracted homogeneous catalyst 49. The gas phase outlets of the hydroformylation reactant separation unit I 407 and the hydroformylation reactant separation unit II 408 are connected to the inlet of the hydroformylation reaction gas mixing unit 410, and the outlet of the hydroformylation reaction gas mixing unit 410 is connected to the inlet of the hydroformylation reaction gas compression unit 411. The outlet of the hydroformylation reaction gas compression unit 411 is connected to the inlet of the hydroformylation reaction gas preheating unit 412. The outlet of the hydroformylation reaction gas preheating unit 412 is connected to the inlet of the hydroformylation reaction gas compression unit 411. The outlet is connected to the inlet of the de-raw gas distillation unit 413, the gas phase outlet of the de-raw gas distillation unit 413 is connected to the inlet of the circulating raw gas production unit 414, the first outlet of the circulating raw gas production unit 414 is connected to the second inlet of the circulating gas mixing unit 403, the second outlet of the circulating raw gas production unit 414 obtains the produced circulating raw material 58, the liquid phase outlet of the de-raw gas distillation unit 413 is connected to the inlet of the C4 product distillation unit 415, the first outlet of the C4 product distillation unit 415 obtains the isobutyraldehyde product 61, and the second outlet of the C4 product distillation unit obtains the normal butyraldehyde product 62.

[0079] As a preferred embodiment, the operating pressure of the degassing and rectification unit 413 is 1.5-2.5 MPaA.

[0080] As a preferred embodiment, the operating pressure of the C4 product distillation unit 415 is 0.1-0.2 MPaA.

[0081] In this embodiment, the operating pressure of the degassing gas distillation unit 413 is 2.0 MPaA, and the operating pressure of the C4 product distillation unit 415 is 0.2 MPaA.

[0082] The second outlet of the circulating catalyst extraction unit 409 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 406.

[0083] Based on the coupled system of propane dehydrogenation, propane dry reforming and hydroformylation of this embodiment, this embodiment also provides a coupled process of propane dehydrogenation, propane dry reforming and hydroformylation, including the following reaction process:

[0084] The propane LPG feed R1 enters the C4 removal distillation unit 101 to remove the C4 heavy component liquid. The C4 and other heavy component products 1 are obtained at the bottom liquid phase outlet of the C4 removal distillation unit 101, and the C3 component gas 2 is obtained at the top gas phase outlet of the C4 removal distillation unit 101.

[0085] C3 component gas 2, carbon dioxide feed R2, and preheated recycled propane 34 enter propane and carbon dioxide premixing unit 102 to produce propane carbon dioxide mixed gas 3. The relatively low-temperature propane carbon dioxide mixed gas 3 and the relatively high-temperature carbon removal reaction gas 8 undergo heat exchange in propane dehydrogenation-coupled dry reforming feed gas heat exchange unit 103 to produce relatively high-temperature heat-exchanged propane carbon dioxide mixed gas 4 and relatively low-temperature heat-exchanged cooling reaction gas I9. The heat-exchanged propane carbon dioxide mixed gas 4 passes through propane dehydrogenation-coupled dry reforming feed gas preheating unit 104 to produce preheated propane carbon dioxide mixed gas 5. The preheated propane carbon dioxide mixed gas 5 passes through the catalyst bed in propane dehydrogenation-coupled dry reforming reaction unit 105 for reaction to produce propane dehydrogenation-coupled dry reforming reaction gas 6. The propane dehydrogenation-coupled dry reforming reaction gas 6 passes through the dehydrogenation-coupled dry reforming reaction gas separation unit 106 to produce carbon 7 and relatively high-temperature gas-phase carbon removal reaction gas 8.

[0086] As a preferred embodiment, the flow ratio of the feed gas propane to carbon dioxide in the propane dehydrogenation coupled dry reforming reaction unit 105 is 0.5-10.

[0087] As a preferred embodiment, the operating conditions of the reactor in the propane dehydrogenation coupled dry reforming reaction unit 105 are a reaction temperature of 500-700°C, a reaction pressure of 0.1-0.5 MPaA, a reaction space velocity of 100-1500 h -1 .

[0088] In this embodiment, the flow ratio of the feed gas propane to carbon dioxide in the propane dehydrogenation coupled dry reforming reaction unit 105 is 1.5; the operating conditions of the reactor in the propane dehydrogenation coupled dry reforming reaction unit 105 are a reaction temperature of 500°C, a reaction pressure of 0.1 MPaA, and a reaction space velocity of 1000 h -1 .

[0089] The relatively low-temperature heat exchange and cooling reaction gas I9 is ​​subjected to heat exchange with circulating water in the dehydrogenation-coupled dry reforming reaction gas heat exchange unit 201 to obtain low-temperature heat exchange and cooling reaction gas II10. The heat exchange and cooling reaction gas II10 is subjected to the water separation unit 202 to obtain water vapor 12 product and dehydrated reaction gas 11. The dehydrated reaction gas 11 is subjected to cooling water in the dehydrogenation-coupled dry reforming reaction gas precooling unit 203 to obtain condensed product I13. The condensed product I13 is compressed in the dehydrogenation-coupled dry reforming reaction gas compression unit 204 to obtain relatively high-pressure pre-compressed reaction gas 14. The pre-compressed reaction gas 14 and the hydrogen-carbon monoxide mixed gas 17 are subjected to the dehydrogenation-coupled dry reforming reaction gas cooling box unit 205 to obtain a relatively low-temperature condensed product II15 and a relatively high-temperature heat exchange and heating hydrogen-carbon monoxide mixed gas 19. The condensed product II 15 is subjected to a dehydrogenation coupled dry reforming reaction gas cooling trap 206 to obtain a cryogenic product 16 at a lower temperature. The cryogenic product 16 is subjected to a synthesis gas hydrocarbon separation unit 207 to obtain a hydrogen and carbon monoxide mixed gas 17 and a C3 mixture 18.

[0090] The heat exchange-heated hydrogen-carbon monoxide mixture 19 passes through the hydrogen-carbon monoxide separation unit 208 to obtain a carbon monoxide mixture 20, a hydrogen mixture 21, and C2 and other light component gas products 22. The carbon monoxide mixture 20 passes through the carbon monoxide production unit 209 to obtain produced carbon monoxide 25 product and hydroformylation carbon monoxide raw gas 26. The hydrogen mixture 21 enters the hydrogen production unit 210 to obtain produced hydrogen 24 and hydroformylation hydrogen raw gas 23. The C3 and other mixtures 18 pass through the carbon oxide and hydrocarbon distillation unit 301 to obtain a gaseous carbon monoxide and carbon dioxide mixed gas product 28 at the top of the tower, and a liquid phase carbon monoxide and carbon dioxide C3 mixture 27 is obtained in the bottom of the tower. The carbon monoxide and carbon dioxide C3 mixture 27 enters the C3 mixture pumping unit 302 to obtain a pressurized pumped C3 heavy component mixture 29, and the pressurized pumped C3 heavy component mixture 29 enters the propylene and propane distillation unit 303 to obtain distilled propylene I 30 and circulating propane I 31. The circulating propane I 31 enters the circulating propane production unit 304 to obtain produced propane 32 and circulating propane II 33. The circulating propane II 33 passes through the circulating propane preheating unit 305 to obtain preheated circulating propane 34 to participate in the propane raw material circulation. The distilled propylene I 30 enters the propylene production unit 306 to obtain produced propylene 35 and distilled propylene II 36. The distilled propylene II 36 enters the propylene secondary separation and purification unit 307 to obtain propylene impurity-removed product 38 and hydroformylation propylene raw gas 37.

[0091] Hydroformylation hydrogen feed gas 23, hydroformylation carbon monoxide feed gas 26 and hydroformylation propylene feed gas 37 enter hydroformylation feed gas mixing unit 401 to obtain fully mixed carbon monoxide / propylene / hydrogen mixed gas 39, carbon monoxide / propylene / hydrogen mixed gas 39 enters hydroformylation feed gas preheating unit I 402 to obtain primary preheated mixed gas 40, primary preheated mixed gas 40 and recycled carbon monoxide / propylene / hydrogen mixed gas II 59 enter recycle gas mixing unit 403 to obtain recycle mixed gas 41, recycle mixed gas 42 is added. Gas 41 enters the hydroformylation feed gas pre-compression unit 404 to obtain a compressed pre-compressed mixed gas 42. The pre-compressed mixed gas 42 enters the hydroformylation feed gas preheating unit I 405 to obtain a secondary preheated mixed gas 43. The secondary preheated mixed gas 43 and the preheated pre-compressed catalyst 53 enter the hydroformylation reaction unit 406 for a hydroformylation reaction to obtain a hydroformylation reaction gas 44. The hydroformylation reaction gas 44 passes through the hydroformylation reactant separation unit I 407 to obtain a gaseous light component reaction gas 45 and a liquid heavy component reaction gas 46. The heavy component reaction gas 46 passes through the hydroformylation reactant separation unit II 408 to obtain the gas phase secondary separation light component reaction gas 47 and the liquid phase circulating catalyst I 48. The circulating catalyst I 48 passes through the circulating catalyst extraction unit 409 to obtain the extracted homogeneous catalyst 49 and the circulating homogeneous catalyst II 50. The circulating homogeneous catalyst II 50 enters the homogeneous catalyst mixing unit 501 together with the fresh homogeneous catalyst feed R3 to be fully mixed to obtain the fresh and circulating mixed homogeneous catalyst 51. The fresh and circulating mixed homogeneous catalyst 51 passes through the catalyst pumping unit 502 to obtain the pre-compressed catalyst 52. The pre-compressed catalyst 52 passes through the catalyst preheating unit 503 to obtain the preheated pre-compressed catalyst 53 to participate in the catalyst circulation.

[0092] As a preferred embodiment, the operating conditions of the reactor in the hydroformylation reaction unit 406 are a reaction temperature of 50-150° C. and a reaction pressure of 1.5-2.5 MPaA.

[0093] In this embodiment, the flow ratio of carbon monoxide, propylene, and hydrogen in the hydroformylation feed gas mixing unit 401, the recycle gas mixing unit 403, and the mixed flow paths, such as the carbon monoxide / propylene / hydrogen mixed gas 39, the primary preheated mixed gas 40, and the recycle mixed gas 41, is 1:1:1. The operating conditions of the reactor in the hydroformylation reaction unit 406 are a reaction temperature of 90° C. and a reaction pressure of 2.0 MPaA.

[0094] The light component reaction gas 45 and the secondary separated light component reaction gas 47 enter the hydroformylation reaction gas mixing unit 410 to obtain a mixed light component reaction gas 54. The mixed light component reaction gas 54 enters the hydroformylation reaction gas compression unit 411 to obtain a pre-compressed reaction gas 55. The pre-compressed reaction gas 55 passes through the hydroformylation reaction gas preheating unit 412 to obtain a preheated pre-compressed reaction gas 56. The preheated pre-compressed reaction gas 56 enters the de-feed gas distillation unit 413 to obtain a liquid C4 product mixture 60 and a circulating carbon monoxide / propylene / hydrogen mixed gas I 57. The circulating carbon monoxide / propylene / hydrogen mixed gas I 57 passes through the circulating raw material gas extraction unit 414 to obtain a produced circulating raw material 58 and a circulating carbon monoxide / propylene / hydrogen mixed gas II 59 to participate in the reaction raw material circulation. The C4 product mixture 60 passes through the C4 product distillation unit 415 to obtain an isobutyraldehyde product 61 and an n-butyraldehyde product 62.

[0095] As a preferred embodiment, the operating pressure of the degassing and rectification unit 413 is 1.5-2.5 MPaA.

[0096] As a preferred embodiment, the operating pressure of the C4 product distillation unit 415 is 0.1-0.2 MPaA.

[0097] In this embodiment, the operating pressure of the degassing gas distillation unit 413 is 2.0 MPaA, and the operating pressure of the C4 product distillation unit 415 is 0.2 MPaA.

[0098] In summary, the coupled propane dehydrogenation, propane dry reforming, and hydroformylation system and process of the present invention utilizes the characteristics of propane dehydrogenation, propane dry reforming, and propylene hydroformylation reactions to achieve this coupling. This eliminates the storage and transportation of propylene and synthesis gas required in the hydroformylation process, as well as the production of propylene, hydrogen, and carbon monoxide alone. This system reduces CO2 emissions, 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.

[0099] 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, propane dry reforming and hydroformylation coupling system, characterized in that: The invention comprises a propane dehydrogenation subsystem, a propane dry reforming subsystem, and a hydroformylation subsystem; wherein the propane dehydrogenation subsystem and the propane dry reforming subsystem are coupled via a propane dehydrogenation coupling dry reforming reaction unit (105) to co-produce propylene and synthesis gas; the propylene produced by the propane dehydrogenation subsystem and the synthesis gas produced by the propane dry reforming subsystem are coupled via a hydroformylation raw gas mixing unit (401) to the hydroformylation subsystem to co-produce n-butyraldehyde and isobutyraldehyde.

2. A propane dehydrogenation, propane dry reforming and hydroformylation coupling system according to claim 1, characterized in that: The invention comprises a de-C4 distillation unit (101), a propane and carbon dioxide premixing unit (102), a propane dehydrogenation coupled dry reforming raw gas heat exchange unit (103), a propane dehydrogenation coupled dry reforming raw gas preheating unit (104), a propane dehydrogenation coupled dry reforming reaction unit (105), a dehydrogenation coupled dry reforming reaction gas separation unit (106), a dehydrogenation coupled dry reforming reaction gas heat exchange unit (201), a water separation unit (202), a dehydrogenation coupled dry reforming reaction gas precooling unit (203), ... reaction gas preheating unit (104), a propane dehydrogenation coupled dry reforming reaction unit (105), a dehydrogenation coupled dry reforming reaction gas separation unit (106), a dehydrogenation coupled dry reforming reaction gas heat exchange unit (201), a water separation unit (202), a dehydrogenation coupled dry reforming reaction gas precooling unit (203), a de-C4 distillation unit (101), a propane and carbon dioxide premixing unit (102), a propane Hydrogen coupled dry reforming reaction gas compression unit (204), dehydrogenation coupled dry reforming reaction gas cooling box unit (205), dehydrogenation coupled dry reforming reaction gas cooling trap (206), synthesis gas hydrocarbon separation unit (207), hydrogen carbon monoxide separation unit (208), carbon monoxide production unit (209), hydrogen production unit (210), carbon oxide hydrocarbon distillation unit (301), C3 mixture pumping unit (302), propylene propane distillation unit (303), circulating propane production unit ( 304), circulating propane preheating unit (305), propylene extraction unit (306), propylene secondary separation and purification unit (307), hydroformylation feed gas mixing unit (401), hydroformylation feed gas preheating unit I (402), adding circulating gas mixing unit (403), hydroformylation feed gas precompression unit (404), hydroformylation feed gas preheating unit II (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), degassing feed gas distillation unit (413), circulating feed gas extraction unit (414), C4 product distillation unit (415), homogeneous catalyst mixing unit (501), homogeneous catalyst pumping unit (502), homogeneous catalyst preheating unit (503); The inlet of the C4 removal distillation unit (101) is used to introduce the reaction raw material propane LPG (R1), the top gas phase of the C4 removal distillation unit (101) is connected to the first inlet of the propane and carbon dioxide premixing unit (102), the second inlet of the propane and carbon dioxide premixing unit (102) is connected to the carbon dioxide feed (R2), and the bottom liquid phase outlet of the C4 removal distillation unit (101) is used to obtain C4 and other heavy component products (1); the outlet of the propane and carbon dioxide premixing unit (102) is connected to the inlet of the propane dehydrogenation coupled dry reforming raw gas heat exchange unit (103), and the outlet of the propane dehydrogenation coupled dry reforming raw gas heat exchange unit (103) is connected to the inlet of the propane dehydrogenation coupled dry reforming raw gas heat exchange unit (103). The high-temperature phase outlet is connected to the inlet of the propane dehydrogenation coupled dry reforming raw gas preheating unit (104), the outlet of the propane dehydrogenation coupled dry reforming raw gas preheating unit (104) is connected to the inlet of the propane dehydrogenation coupled dry reforming reaction unit (105), the outlet of the propane dehydrogenation coupled dry reforming reaction unit (105) is connected to the inlet of the dehydrogenation coupled dry reforming reaction gas separation unit (106), the solid phase outlet of the dehydrogenation coupled dry reforming reaction gas separation unit (106) obtains the carbon deposition product (7), and the gas phase outlet of the dehydrogenation coupled dry reforming reaction gas separation unit (106) is connected to the inlet of the propane dehydrogenation coupled dry reforming raw gas heat exchange unit (103); The low temperature phase outlet of the propane dehydrogenation coupled dry reforming feed gas heat exchange unit (103) is connected to the inlet of the dehydrogenation coupled dry reforming reaction gas heat exchange unit (201), the outlet of the dehydrogenation coupled dry reforming reaction gas heat exchange unit (201) is connected to the inlet of the water separation unit (202), the liquid phase outlet of the water separation unit (202) obtains the water vapor (12) product, the gas phase outlet of the water separation unit (202) is connected to the inlet of the dehydrogenation coupled dry reforming reaction gas precooling unit (203) The outlet of the dehydrogenation-coupled dry reforming reaction gas precooling unit (203) is connected to the inlet of the dehydrogenation-coupled dry reforming reaction gas compression unit (204), the outlet of the dehydrogenation-coupled dry reforming reaction gas compression unit (204) is connected to the compressed reaction gas inlet of the dehydrogenation-coupled dry reforming reaction gas cooling box unit (205), the low-temperature gas outlet of the dehydrogenation-coupled dry reforming reaction gas cooling box unit (205) is connected to the inlet of the dehydrogenation-coupled dry reforming reaction gas cold trap (206), and the dehydrogenation-coupled dry reforming reaction gas cooling box unit (205) is connected to the inlet of the dehydrogenation-coupled dry reforming reaction gas cold trap (206). The outlet of the hydrogen-coupled dry reforming reaction gas cold trap (206) is connected to the inlet of the synthesis gas hydrocarbon separation unit (207), the gas phase outlet of the synthesis gas hydrocarbon separation unit (207) is connected to the deep cold gas inlet of the dehydrogenation-coupled dry reforming reaction gas cold box unit (205), the high temperature gas outlet of the dehydrogenation-coupled dry reforming reaction gas cold box unit (205) is connected to the inlet of the hydrogen-carbon monoxide separation unit (208), and the liquid phase outlet of the hydrogen-carbon monoxide separation unit (208) is connected to the inlet of the hydrogen-carbon monoxide separation unit (208). to C2 and other light component gases (22), the first gas phase outlet of the hydrogen and carbon monoxide separation unit (208) is connected to the inlet of the carbon monoxide production unit (209), the first outlet of the carbon monoxide production unit (209) obtains the produced carbon monoxide product (25), the second gas phase outlet of the hydrogen and carbon monoxide separation unit (208) is connected to the inlet of the hydrogen production unit (210), and the first outlet of the hydrogen production unit (210) obtains the produced hydrogen product (24); The liquid phase outlet of the synthesis gas hydrocarbon separation unit (207) is connected to the inlet of the carbon oxide hydrocarbon distillation unit (301), the gas phase outlet of the oxide hydrocarbon distillation unit (301) obtains a carbon monoxide and carbon dioxide mixed gas (28), the liquid phase outlet of the oxide hydrocarbon 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 first outlet of the propylene propane distillation unit (303) is connected to the inlet of the circulating propane production unit (304), and the first outlet of the circulating propane production unit (304) obtains produced propane. (32), 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 and carbon dioxide premixing unit (102), the second outlet of the propylene propane distillation unit (303) is connected to the inlet of the propylene production unit (306), the first outlet of the propylene production unit (306) obtains the produced propylene product (35), the second outlet of the propylene production unit (306) is connected to the inlet of the propylene secondary separation and purification unit (307), and the liquid phase outlet of the propylene secondary separation and purification unit (307) obtains the propylene impurity-removed product (38); The second outlet of the carbon monoxide extraction unit (209) is connected to the first inlet of the hydroformylation feed gas mixing unit (401), the second outlet of the hydrogen extraction unit (210) is connected to the second inlet of the hydroformylation feed gas mixing unit (401), the gas phase outlet of the propylene secondary separation and purification unit (307) is connected to the third inlet of the hydroformylation feed gas mixing unit (401), the outlet of the hydroformylation feed gas mixing unit (401) is connected to the inlet of the hydroformylation feed gas preheating unit I (402), the outlet of the hydroformylation feed gas preheating unit I (402) is connected to the inlet of the recycle gas mixing unit (403), and the recycle gas mixing unit (403) is connected to the inlet of the hydroformylation feed gas preheating unit I (402). The outlet of the element (403) is connected to the inlet of the hydroformylation raw gas precompression unit (404), the outlet of the hydroformylation raw gas precompression unit (404) is connected to the inlet of the hydroformylation raw gas preheating unit II (405), the outlet of the hydroformylation raw gas preheating unit II (405) is connected to the first inlet of the hydroformylation reaction unit (406), the outlet of the hydroformylation reaction unit (406) is connected to the inlet of the hydroformylation reactant separation unit I (407), the liquid phase outlet of the hydroformylation reactant separation unit I (407) is connected to the inlet of the hydroformylation reactant separation unit II (408), and the hydroformylation reactant separation unit II (408) is connected to the inlet of the hydroformylation reactant separation unit II (408). ) is connected to the inlet of the circulating catalyst extraction unit (409), the first outlet of the circulating catalyst extraction unit (409) obtains the extracted homogeneous catalyst (49), the gaseous phase outlets of the hydroformylation reactant separation unit I (407) and the hydroformylation reactant separation unit II (408) are connected to the inlet of the hydroformylation reaction gas mixing unit (410), the outlet of the hydroformylation reaction gas mixing unit (410) is connected to the inlet of the hydroformylation reaction gas compression unit (411), the outlet of the hydroformylation reaction gas compression unit (411) is connected to the inlet of the hydroformylation reaction gas preheating unit (412), and the hydroformylation reaction gas preheating unit (412) is connected to the inlet of the hydroformylation reaction gas compression unit (411). The outlet of the degassing unit (413) is connected to the inlet of the degassing unit (413), the gas phase outlet of the degassing unit (413) is connected to the inlet of the circulating raw gas extraction unit (414), the first outlet of the circulating raw gas extraction unit (414) is connected to the second inlet of the adding circulating gas mixing unit (403), the second outlet of the circulating raw gas extraction unit (414) obtains the extracted circulating raw material (58), the liquid phase outlet of the degassing unit (413) is connected to the inlet of the C4 product distillation unit (415), the first outlet of the C4 product distillation unit obtains the isobutyraldehyde product (61), and the second outlet of the C4 product distillation unit obtains the normal butyraldehyde product (62); The second outlet of the circulating catalyst extraction unit (409) 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 (406).

3. A coupled process of propane dehydrogenation, propane dry reforming and hydroformylation, characterized in that: The reaction process includes the following: Propane LPG feed (R1) enters a C4 removal distillation unit (101) to remove C4 heavy component liquid, a C4 and other heavy component products (1) are obtained at the bottom liquid phase outlet of the C4 removal distillation unit (101), and a C3 component gas (2) is obtained at the top gas phase outlet of the C4 removal distillation unit (101); The C3 component gas (2), carbon dioxide feed (18) and preheated circulating propane (34) enter the propane and carbon dioxide premixing unit (102) to obtain a propane carbon dioxide 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 coupled dry reforming raw gas heat exchange unit (103) to obtain the relatively high temperature heat exchange propane carbon dioxide mixed gas (4) and the relatively low temperature heat exchange cooling reaction gas I (9); The heat exchange propane carbon dioxide mixed gas (4) passes through a propane dehydrogenation coupled dry reforming feed gas preheating unit (104) to obtain a preheated propane carbon dioxide mixed gas (5); The preheated propane-carbon dioxide mixed gas (5) passes through a propane dehydrogenation coupled dry reforming reaction unit (105) and flows through a catalyst bed to react, thereby obtaining a propane dehydrogenation coupled dry reforming reaction gas (6); The propane dehydrogenation coupled dry reforming reaction gas (6) passes through a dehydrogenation coupled dry reforming reaction gas separation unit (106) to obtain carbon deposits (7) and a gas phase relatively high temperature carbon removal reaction gas (8); The relatively low-temperature heat exchange and cooling reaction gas I (9) is passed through the dehydrogenation coupled dry reforming 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) passes through the water separation unit (202) to obtain water vapor (12) product and dehydrated reaction gas (11); The dehydrated reaction gas (11) is cooled by cooling water in a dehydrogenation coupled dry reforming reaction gas precooling unit (203) to obtain a condensed product I (13); The condensed product I (13) is compressed by the dehydrogenation coupled dry reforming reaction gas compression unit (204) to obtain a relatively high-pressure pre-compressed reaction gas (14); The pre-compressed reaction gas (14) and the hydrogen-carbon monoxide mixed gas (17) are coupled to the dehydrogenation dry reforming reaction gas cooling box unit (205) to obtain a relatively low-temperature condensed product II (15) and a relatively high-temperature heat exchange-heated hydrogen-carbon monoxide mixed gas (19); The condensed product II (15) is subjected to a dehydrogenation-coupled dry reforming reaction gas cooling trap (206) to obtain a lower temperature cryogenic product (16); The cryogenic product (16) passes through a synthesis gas hydrocarbon separation unit (207) to obtain a hydrogen and carbon monoxide mixture (17) and a C3 mixture (18); The heat exchanged and heated hydrogen and carbon monoxide mixed gas (19) as described above passes through the hydrogen and carbon monoxide separation unit (208) to obtain a carbon monoxide mixed gas (20), a hydrogen mixed gas (21), and C2 and other light component gas products (22); The carbon monoxide mixed gas (20) passes through the carbon monoxide extraction unit (209) to obtain the extracted carbon monoxide product (25) and the hydroformylation carbon monoxide raw gas (26); As described above, the hydrogen mixed gas (21) enters the hydrogen extraction unit (210) to obtain extracted hydrogen (24) and hydroformylation hydrogen feed gas (23); As described above, the C3 mixture (18) passes through the carbon oxide hydrocarbon distillation unit (301) to obtain a gaseous carbon monoxide and carbon dioxide mixed gas product (28) at the top of the tower, and a liquid carbon monoxide and carbon dioxide C3 mixture (27) is obtained in the bottom of the tower; The carbon monoxide and carbon dioxide C3 mixture (27) is fed into the C3 mixture pumping unit (302) to obtain a pressurized pumped C3 heavy component mixture (29); The C3 heavy component mixture (29) is pumped under pressure into the propylene propane distillation unit (303) to obtain distilled propylene I (30) and circulating propane I (31); Circulating propane I (31) enters the circulating propane production unit (304) to obtain produced propane (32) and circulating propane II (33); The circulating propane II (33) passes through the circulating propane preheating unit (305) to obtain preheated circulating propane (34) to participate in the propane raw material circulation; As described above, the distilled propylene I (30) enters the propylene production unit (306) to obtain produced propylene (35) and distilled propylene II (36); The propylene II (36) is distilled and enters the propylene secondary separation and purification unit (307) to obtain a propylene impurity-free product (38) and a hydroformylation propylene feed gas (37); The hydroformylation hydrogen feed gas (23), the hydroformylation carbon monoxide feed gas (26) and the hydroformylation propylene feed gas (37) enter the hydroformylation feed gas mixing unit (401) to obtain a fully mixed carbon monoxide / propylene / hydrogen mixed gas (39); The carbon monoxide / propylene / hydrogen mixed gas (39) enters the hydroformylation feed gas preheating unit I (402) to obtain a primary preheated mixed gas (40); The primary preheated mixed gas (40) and the circulating carbon monoxide / propylene / hydrogen mixed gas II (59) enter the circulating gas mixing unit (403) and are mixed to obtain the circulating mixed gas (41); Adding the circulating mixed gas (41) into the hydroformylation raw gas pre-compression unit (404) to obtain a compressed pre-compressed mixed gas (42); The pre-compressed mixed gas (42) enters the hydroformylation raw gas preheating unit I (405) to obtain a secondary preheated mixed gas (43); The secondary preheated mixed gas (43) and the preheated precompressed catalyst (53) enter the hydroformylation reaction unit (406) to undergo a hydroformylation reaction to obtain a hydroformylation reaction gas (44); The hydroformylation reaction gas (44) passes through the hydroformylation reactant separation unit I (407) to obtain a gas phase light component reaction gas (45) and a liquid phase heavy component reaction gas (46); The heavy component reaction gas (46) passes through the hydroformylation reactant separation unit II (408) to obtain a gas phase secondary separation light component reaction gas (47) and a liquid phase circulating catalyst I (48); The circulating catalyst I (48) passes through the circulating catalyst extraction unit (409) to obtain the extracted homogeneous catalyst (49) and the circulating homogeneous catalyst II (50); The circulating homogeneous catalyst II (50) 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 (51); Fresh and recycled mixed homogeneous catalyst (51) is passed through a catalyst pumping unit (502) to obtain a pre-compressed catalyst (52); The pre-compressed catalyst (52) passes through the catalyst preheating unit (503) to obtain the preheated pre-compressed catalyst (53) to participate in the catalyst cycle; As described above, the light component reaction gas (45) and the secondary separated light component reaction gas (47) enter the hydroformylation reaction gas mixing unit (410) to obtain a mixed light component reaction gas (54); The mixed light component reaction gas (54) enters the hydroformylation reaction gas compression unit (411) to obtain pre-compressed reaction gas (55); The pre-compressed reaction gas (55) passes through the hydroformylation reaction gas preheating unit (412) to obtain preheated reaction compressed gas (56); The preheated reaction compressed gas (56) enters the degassing and rectification unit (413) to obtain a liquid C4 product mixture (60) and a circulating carbon monoxide / propylene / hydrogen mixed gas I (57); The circulating carbon monoxide / propylene / hydrogen mixed gas I (57) passes through the circulating raw material gas extraction unit (414) to obtain the extracted circulating raw material (58) and the circulating carbon monoxide / propylene / hydrogen mixed gas II (59) to participate in the reaction raw material circulation; The C4 product mixture (60) is passed through a C4 product distillation unit (415) to obtain an isobutyraldehyde product (61) and a normal butyraldehyde product (62).

4. A coupled process of propane dehydrogenation, propane dry reforming and hydroformylation according to claim 3, characterized in that: The two reactions of propane dehydrogenation and propane dry reforming occur in the propane dehydrogenation coupled dry reforming reaction unit (105).

5. A coupled process of propane dehydrogenation, propane dry reforming and hydroformylation according to claim 3, characterized in that: The flow ratio of the raw gas propane to carbon dioxide in the propane dehydrogenation coupled dry reforming reaction unit (105) is 0.5-10.

6. A coupled process of propane dehydrogenation, propane dry reforming and hydroformylation according to claim 3, characterized in that: The operating conditions of the reactor in the propane dehydrogenation coupled dry reforming reaction unit (105) are a reaction temperature of 500-700°C, a reaction pressure of 0.1-0.5 MPaA, and a reaction space velocity of 100-1500 h -1 .

7. A coupled process of propane dehydrogenation, propane dry reforming and hydroformylation 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 (403) and the mixed flow path, such as the carbon monoxide / propylene / hydrogen mixed gas (39), the primary preheated mixed gas (40) and the recycle mixed gas (41), is any ratio.

8. A coupled process of propane dehydrogenation, propane dry reforming and hydroformylation according to claim 3, characterized in that: The operating conditions of the reactor in the hydroformylation reaction unit (406) are a reaction temperature of 50-150°C and a reaction pressure of 1.5-2.5 MPaA.

9. A coupled process of propane dehydrogenation, propane dry reforming and hydroformylation according to claim 3, characterized in that: The operating pressure of the degassing and rectification unit (413) is 1.5-2.5 MPaA.

10. A coupled process of propane dehydrogenation, propane dry reforming and hydroformylation according to claim 3, characterized in that: The operating pressure of the C4 product distillation unit (415) is 0.1-0.2 MPaA.

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