CN1394965A - Melt reduction iron-smelting dimethyl ether production and power generation combined production method and installation - Google Patents

Abstract

The invention belongs to the fields of metallurgy, chemical industry and energy, and particularly relates to smelting reduction ironmaking, dimethyl ether production and utilization of waste heat to generate electricity. The cogeneration method of the present invention combining smelting reduction ironmaking, dimethyl ether production and power generation is to use the coal gas produced in the smelting reduction ironmaking process, after heat exchange, dust removal, desulfurization, and pressure treatment, after adding catalyst and inert solvent DME is produced in a slurry bed reactor, and the waste heat in the process is used to generate electricity. The cogeneration unit combining smelting reduction ironmaking, dimethyl ether production and power generation includes a smelting reduction ironmaking unit, a synthesis gas purification unit, a dimethyl ether synthesis unit, a product separation unit and a power generation unit. The invention has the advantages of less investment, can effectively improve energy utilization rate, greatly reduce product energy consumption and cost, and is beneficial to environmental protection.

Description

Coproduction method and device for combining smelting reduction ironmaking dimethyl ether production and power generation

technical field

The invention belongs to the fields of metallurgy, chemical industry and energy, and particularly relates to smelting reduction ironmaking, dimethyl ether production and utilization of waste heat to generate electricity.

Background technique

Smelting reduction is an advanced ironmaking process technology. It can not only solve the two major problems of coke shortage and environmental pollution that the iron and steel industry is facing today, but also greatly shorten the process flow, increase productivity, and reduce Infrastructure investment and production costs increase the flexibility of production (ZL99122119.2, ZL99122120.6, ZL99122121.4 and ZL00238120.6). While the smelting reduction ironmaking process produces molten iron, it also by-produces a large amount of gas with high calorific value. How to use these gas and related waste heat to achieve the purpose of comprehensive joint production has always been a subject of people's exploration. While using the smelting reduction process gas to produce sponge iron, voestalpine also proposed the idea of using smelting reduction ironmaking process gas to synthesize chemical raw materials; Japan once proposed the technical idea of using smelting reduction ironmaking process gas for clean power generation. But above-mentioned two all fail to put forward specific plan and implement.

Contents of the invention

The purpose of the present invention is to provide an efficient, environment-friendly and energy-saving co-production method and device based on smelting reduction ironmaking, dimethyl ether production and power generation.

Aiming at the above-mentioned purpose, the co-production method of smelting reduction ironmaking, dimethyl ether production and power generation of the present invention is based on smelting reduction ironmaking, with the process gas of smelting reduction as the main raw material, plus relevant catalysts and inert Solvent, DME is produced in the DME synthesis device, and the water vapor generated by the heat exchange of the gas generated in the smelting reduction ironmaking process through the heat exchanger and the waste heat generated in the DME production process enter the steam drum to generate steam To generate electricity. Now with regard to this technical scheme, describe in detail,

(1) Smelting reduction ironmaking uses iron ore, iron ore powder and its pellets, lump coal and coal powder as the main raw materials, and industrial pure oxygen or low-purity oxygen, limestone, fluorite, etc. as auxiliary raw materials, using pre-reduction The two-step smelting reduction ironmaking technology of final reduction and final reduction produces molten iron. At the same time, in the process of producing molten iron, a large amount of gas with ^high calorific value is also by-produced. 6000～8500KJ/Nm ³ .

(2) The main raw material is the high calorific value gas produced in the smelting reduction ironmaking process, which is fed into the

In the slurry bed reactor of the dimethyl ether synthesis device of catalyst and inert solvent, in the catalyst

The dimethyl ether synthesis reaction is carried out under the action of dimethyl ether, and the synthetic product is obtained after absorption, decarburization and rectification

A high concentration of dimethyl ether was obtained.

In the synthetic raw material of above-mentioned dimethyl ether, the proportioning (weight %) of catalyzer and inert solvent is:

The catalyst content is 5-45%, and the inert solvent content is 55-95%.

The main composition of coal gas is: CO30～75%, H ₂ 7～8%, CO ₂ 3～32%;

Gas air velocity is 1500～10000h ^-1 ;

The hot coal gas produced in the smelting reduction ironmaking process in the raw material needs to be treated by heat exchange, dust removal, fine desulfurization and pressure treatment, and then enters the dimethyl ether synthesis unit as a raw material. The gas pressure is 2.0-8.0MPa.

The catalyst in the raw material adopts a copper-based methanol synthesis catalyst and a methanol dehydration catalyst, and the weight ratio of the two is 0.5-4.

The copper-based methanol synthesis catalyst is any one of C301, C302, C306 or C207.

The methanol dehydration catalyst is any one of molecular sieve ZSM-5 or gama-Al ₂ O ₃ .

The inert solvent in the raw material is any one of liquid paraffin, mineral oil, carboxane, alcohol or ether containing 18-35 carbon chains, chlorinated alkanes, aromatic hydrocarbons and derivatives thereof in alkane solvents.

The process parameter of dimethyl ether synthesis process is:

Working temperature is 200～320℃;

The working pressure is 2.0~8.0MPa;

The dimethyl ether synthesis process is three reaction coupling processes of water gas shift, methanol synthesis and methanol dehydration, that is, three reactions are carried out simultaneously in the slurry bed reactor, namely:

The product obtained after the synthesis reaction contains dimethyl ether (CH ₃ OCH ₃ ), methanol (CH ₃ OH), water (H ₂ O), unreacted H ₂ , CO, CO ₂ and part of the catalyst and inert Solvent, these substances enter the primary separator from the top of the slurry bed reactor of the dimethyl ether synthesis unit for separation, separate the inert solvent and catalyst from the gaseous products, and the gaseous products enter the absorption tower, dimethyl ether, methanol, water and part of CO ₂ After absorption, it becomes a liquid phase and enters the decarburization tower to remove CO ₂ , and the remaining product enters the dimethyl ether rectification tower for rectification. The unabsorbed gaseous substance returns to the compressor to join the feed gas.

The absorption parameters of the absorption tower are:

Gas inlet temperature: -10～40℃

Liquid inlet temperature: 10～60℃

Pressure inside the tower: 1.0～3.0Mpa,

Decarburization parameters of the decarburization tower

Liquid inlet temperature: 150～210℃

Outlet temperature of tower kettle: 180～220℃

Pressure inside the tower: 1.0～2.0MPa,

Then enter the dimethyl ether rectification tower for rectification, and its dimethyl ether rectification parameters

Liquid inlet temperature: 180～200℃

Outlet temperature of tower kettle: 180～220℃

Pressure inside the tower: 0.6~1.5MPa.

After rectification, a high concentration of dimethyl ether can be obtained.

In the rectification process, the distillate at the bottom of the tower is methanol and water, part of which is returned to the slurry bed reactor as raw material and the absorption tower as an absorbent, and the rest is rectified to recover methanol.

(3) The water vapor generated by the heat exchange of the coal gas through the heat exchanger in the smelting reduction ironmaking process and the water vapor generated during the synthesis of dimethyl ether enter the steam drum of the power generation device respectively, and the steam is used as power to drive the steam turbine or other power generation devices To generate electricity. The steam parameters used for power generation are:

The steam pressure is 1~7Mpa

The steam temperature is 130-300°C.

The combined production device of smelting reduction ironmaking, dimethyl ether production and power generation in the present invention is composed of a smelting reduction ironmaking device, a synthesis gas purification device, a dimethyl ether synthesis device, a product separation device and a power generation device.

The co-production device combining smelting reduction ironmaking, dimethyl ether production and power generation of the present invention will now be described in detail with reference to the accompanying drawings.

Description of drawings

Accompanying drawing 1 is the structure schematic diagram of the joint production device of the present invention combining smelting reduction ironmaking, dimethyl ether production and power generation.

As can be seen from Fig. 1, the combined production device of smelting reduction ironmaking, dimethyl ether production and power generation of the present invention is composed of smelting reduction ironmaking device S1, synthesis gas purification device S2, and dimethyl ether synthesis device S3 in each dotted line frame , Product separation device S4 and power generation device S5.

Now each device and their connection relationship are described as follows:

①Smelting reduction ironmaking device S1 consists of pre-reduction furnace 04, final reduction furnace 11, silos 01 and 02, dust collectors 06 and 15, feeding pipe 10 and related pipelines 05, 07, 08, 09, 14, 16 Composition: In the final reduction furnace 11, there are oxidation conveying pipeline 03, iron tapping outlet 13 and slag outlet 12.

The pre-reduction furnace 04 is connected to the final reduction furnace 11 through the feeding pipe 10, the pre-reduction furnace 04 is connected to the dust collector 06 through the pipeline 05, the final reduction furnace 11 is connected to the dust collector 15 through the pipeline 14, and the dust collector 15 is connected to the dust collector 15 through the pipeline 16 is connected with the pre-reduction furnace, and the dust collector 06 is also connected with the final reduction furnace 11 through the pipeline 07. The entire smelting reduction ironmaking device S1 is connected to the synthesis gas purification device S2 through a pipeline 08 .

②Synthesis gas purification device S2 is composed of heat exchanger 17, synthesis gas purification tower 19, compressor 21 and related pipelines 18, 20, 22, 23; The dust collector 06 of S1 is connected, and is connected with the synthesis gas purification tower 19 through the pipeline 18, and the synthesis gas purification tower 19 is connected with the compressor 21 through the pipeline 20, and the heat exchanger 17 is connected with the steam drum of the power generation device S5 through the pipeline 23 45 connected.

③ The dimethyl ether synthesis unit S3 is composed of a heat exchanger 24, a slurry bed reactor 26, a primary separator 28 and related pipelines 25, 27, 29, 31, 32, 43. The heat exchanger 24 is connected to the The compressor 21 in the synthesis gas purification device S2 is connected, and is connected with the slurry bed reactor 26 through the pipeline 25, and the slurry bed reactor 26 is connected with the primary separator 28 through the pipeline 27, 29, and the primary separator 28 passes through The pipeline 31 is connected with the heat exchanger 24 again, and the slurry bed reactor 26 is connected with the steam bag 45 of the power generation unit S5 through the pipeline 47, and the 30 at the top of the slurry bed reactor 26 is the inlet for catalyst and inert solvent;

④ The product separation device S4 is composed of an absorption tower 33, a decarburization tower 37, a dimethyl ether rectification tower 39, a dimethyl ether storage tank 42 and corresponding pipelines 34, 35, 36, 41, 49; Roads 36, 43 are connected to the slurry bed reactor 26 in the dimethyl ether synthesis unit S3, and are connected to each other with the decarburization tower 37 through a pipeline 35, and the absorption tower 33 is also connected to the dimethyl ether synthesis unit S3 through a pipeline 32. The heat exchanger 24 is connected to each other, and is connected to the compressor 21 of the synthesis gas purification device S2 through the pipeline 34, and the decarburization tower 37 is connected to the dimethyl ether rectification tower 39 through the pipeline 49, and the top of the decarbonization tower 37 has a non-condensable The gas outlet 38 and the top of the dimethyl ether rectification tower 39 are connected to the dimethyl ether fine storage tank 42 through a pipeline 41 , and there is an outlet 40 at the bottom of the tower, which is connected to the slurry bed reactor 26 through a pipeline 43 at the same time.

⑤The power generation device S5 is composed of a steam drum 45, a generator 48 and a pipeline 46, and the steam drum 45 also passes through the pipelines 23 and 47 and the heat exchanger 17 of the synthesis gas purification device S2 and the slurry state of the dimethyl ether synthesis device S3 respectively. Bed reactor 26 is connected;

In the entire cogeneration unit that combines smelting reduction ironmaking, dimethyl ether production and power generation, the smelting reduction ironmaking unit S1 is connected to the synthesis gas purification unit S2 through the pipeline 08, and the synthesis gas purification unit S2 is connected through the pipeline 22 and the 23 is connected with the dimethyl ether synthesis unit S3 and the power generation unit S5, and the dimethyl ether synthesis unit S3 is connected with the product separation unit S4 and the power generation unit S5 through pipelines 32 and 47 respectively.

According to the method and device of the present invention, the combined production process of smelting reduction ironmaking, dimethyl ether production and power generation is as follows:

Firstly, the smelting reduction ironmaking device S1 of the present invention is used to produce molten iron in a conventional two-step process. While producing molten iron, a large amount of gas generated in the pre-reduction furnace 04 is dedusted by the dust collector 06 and then enters the synthesis gas for purification. The heat exchanger 17 in the device S2 exchanges heat to reduce the temperature, and then enters the synthesis gas purification tower 19 for further dust removal and desulfurization. After dedusting and desulfurization, it is compressed by the compressor 21 and enters the heat exchanger 24 in the dimethyl ether synthesis unit S3. After heat exchange, the coal gas (synthesis gas) with a certain pressure enters the slurry bed reactor 26. At this time, the catalyst and The inert solvent is also added into the slurry bed reactor 26 from the inlet 30, and the three react in the slurry bed 26 reactor, and the products obtained after the reaction include dimethyl ether, methanol, water, unreacted H ₂ , CO, CO ₂ and the entrained catalyst and inert solvent, these products enter the primary separator 28 from the top of the slurry bed reactor 26 through the pipeline 27, separate the inert solvent and catalyst from the gaseous product, and return to the slurry state through the pipeline 29 In the bed reactor 26, the gaseous product enters the heat exchanger 24 through the pipeline 31 for heat exchange, and enters the absorption tower 33 through the pipeline 32. After being absorbed by the absorption tower 33, the _H2 , CO, and _CO2 in the mixed product are still in the gas phase , and return to the compressor 21 through the pipeline 34, mixed with fresh coal gas (synthesis gas) or directly used as waste heat recovery; while dimethyl ether, methanol, water and a small amount of CO ₂ are liquid phases, and enter the decarburization through the pipeline 35 In the tower 37, after decarburization, _CO2 is separated from the tower top 38, and the distillate from the bottom of the decarburization tower 38 enters the dimethyl ether rectification tower 37 through the pipeline 35 for rectification, and the high-concentration dimethyl ether after rectification The product is drawn from the outlet 41 at the top of the tower, and sent to the dimethyl ether storage tank 42 for storage after being cooled; the distillate at the bottom of the rectification tower 39 is methanol and water, and part of it is sent to the slurry bed reactor through the outlet 40 through pipelines 43 and 36 26 and absorption tower 33, all the other enter methanol rectification tower through pipeline 44 and reclaim methanol.

In addition, the water vapor produced during the ironmaking process of the smelting reduction ironmaking device S1 through the heat exchange of the heat exchanger 17 enters the steam drum 45 in the power generation device S5 through the pipeline 23, and the dimethyl ether synthesis process produces The waste heat also enters the steam drum through the pipeline 47, converts water steam, and the two streams of water steam merge into the turbo generator 48 to generate electricity.

For this reason, the joint production purpose of smelting reduction ironmaking, dimethyl ether production and power generation has been achieved.

Compared with prior art, the present invention has following advantage:

1. The coal gas produced in the smelting reduction process of the present invention is a CO-rich synthesis gas, wherein the CO content is 30-75%, and the _H content is 7-8%. The bottom of the tower after dimethyl ether rectification can be used The distillate (mainly methanol and water) re-enters the slurry bed reactor 26 through the pipeline 43 to adjust the hydrogen-to-carbon ratio and increase the production rate of dimethyl ether and the conversion rate of CO.

②In the slurry bed reactor 26, the CO/H2 _is wide, the CO content reaches 30-75%, and the _CO2 concentration range is large (3-32%), so the dimethyl ether synthesis process has great flexibility and is easy to work.

③Due to the synthesis process of dimethyl ether, when the one-pass process is adopted, the CO conversion rate reaches 85%, and when the low-cycle process is adopted, the CO conversion rate reaches 70%, which is significantly higher than the CO conversion rate in the traditional methanol synthesis process (usually lower than 10% ).

④ The present invention aims at the best conversion effect of energy and resources in the co-production process (comprehensive process), uses the primary conversion of carbon in coal to complete the reduction process of iron in iron-containing raw materials, and then uses the by-product gas to further convert and synthesize dimethyl ether process, to achieve the purpose of system optimization (minimum consumption, minimum waste discharge, etc.), not only to find a reasonable way to use the large amount of tail gas produced by the traditional smelting reduction ironmaking process, but also to solve the problems required for the synthesis of dimethyl ether The main raw material problem. The combination of the two processes achieves the effect of complementary advantages, which reduces the production cost of the product. At the same time, it provides adjustment space for the ratio of the products produced (hot metal, dimethyl ether), and the waste heat of the two processes is used for power generation. To achieve the purpose of comprehensive utilization.

⑤Low investment can effectively improve energy utilization rate, greatly reduce product energy consumption and cost, and is conducive to environmental protection.

Example

Three batches of tests were carried out by adopting the co-production method and device in which the smelting reduction ironmaking, dimethyl ether production and power generation are combined.

Firstly, the ore, flux, coal and other raw materials and oxygen are sent to the smelting reduction device according to a certain proportion from the silos 01 and 02, and the oxygen delivery pipe 03 respectively, and the molten iron is discharged from the molten iron outlet 13. At the same time, a large amount of gas is produced. The gas composition, gas generation and iron production are shown in Table 1. The produced coal gas is dedusted by dedusters 06 and 15, and after heat exchange by heat exchanger 17 and dedusting and desulfurization by synthesis gas purification tower 19, it is compressed by compressor 21 to make it have a certain pressure from the dimethyl ether synthesis unit S3. The bottom of the slurry bed reactor 26 enters, and the catalyst and the inert solvent are added from the inlet 30 in advance. The components and weight ratios of the inert solvent and the catalyst are shown in Table 2. In the slurry bed reactor 26, the coal gas is synthesized into dimethyl ether under the action of a catalyst and an inert solvent. The technical parameters of the synthesis process are listed in Table 3. The synthesized product is decarburized by the decarburization tower 33 and rectified by the dimethyl ether rectification tower 39 to obtain high-concentration dimethyl ether after rectification. Its decarburization and rectification parameters are listed in Table 4. The indicators of the obtained 3 batches of dimethyl ether are shown in Table 5.

In the above process, the gas produced by smelting reduction ironmaking passes through the heat exchanger to generate water vapor and the waste heat generated in the synthesis process of dimethyl ether enters the steam converted by the steam drum, and generates electricity through the steam turbine. The steam pressure and The steam temperatures are listed in Table 6.

Table 1 Example gas composition, gas generation and iron production batch number Iron production t/h Gas composition %vol Gas generation Nm ³ /t·Molten iron CO CO ₂ N ₂ H ₂ 1 3 62～75 8～14 2～5 7～14 1900 2 3.5 40～48 23～32 2～5 10～18 1340 3 3.3 52～59 19～25 2～5 8～15 1670

Table 2 Catalyst and inert solvent ratio (weight) in the synthetic process of embodiment dimethyl ether batch number catalyst inert solvent Copper-based Methanol Synthesis Catalyst Methanol dehydration catalyst 1 C301 20 ZSM-5 10 liquid paraffin 570 2 C302 50 gama-Al ₂ O ₃ 50 mineral oil 400 3 C207 20 ZSM-5 5 angle sandane 220

Table 3 Synthesis process parameters of embodiment dimethyl ether in synthesis device batch number Working temperature/℃ Working pressure/MPa Syngas space velocity/h ^-1 1 220 3 2500 2 270 5 6000 3 270 8 9000

Table 4 Absorption, decarburization and dimethyl ether distillation parameters of synthetic products of examples batch number Decarburization parameter Decarburization parameter Dimethyl ether distillation parameters Inlet temperature °C Outlet temperature °C pressure MPa Inlet temperature °C Outlet temperature °C pressure MPa Inlet temperature °C Outlet temperature °C pressure MPa 1 15 45 2.0 170 210 2.0 130 160 0.6 2 32 16 1.3 180 200 1.5 150 170 0.8 3 2 32 1.6 160 190 1.2 170 190 1.2

The indication of the dimethyl ether product gained in the embodiment of table 5 batch number Dimethyl ether index 1 DME content ≥99.5% 2 DME content ≥99.98% 3 Dimethyl ether content ≥ 95%

The steam pressure and steam temperature of table 6 embodiment steam bag Batch number Vapor pressure MPa Steam temperature °C 1 4.0 220 2 5.5 175 3 3.2 205

Claims (10)

1. A co-production method combining smelting reduction ironmaking, dimethyl ether production and power generation, including smelting reduction ironmaking, that is, using iron ore, iron ore powder and its pellets, lump coal and coal powder as main raw materials , using industrial pure oxygen or low-purity oxygen, limestone, fluorite, etc. as auxiliary raw materials, adopts the two-step smelting reduction ironmaking technology of pre-reduction and final reduction to produce molten iron. At the same time, in the process of smelting reduction ironmaking, also A large amount of gas with high calorific value is produced as a by-product, which is characterized by: ①Using the high calorific value gas produced in the smelting reduction ironmaking process as the main raw material, adding In the slurry bed reactor of the dimethyl ether synthesis device of catalyst and inert solvent, in the catalyst Under the action of dimethyl ether synthesis reaction, the synthesis product is absorbed, decarburized and rectified, To obtain a high concentration of dimethyl ether, The proportioning (weight %) of catalyzer and inert solvent is: Catalyst is 5～45%, inert solvent is 55～95%, The main composition of gas is CO 30-75%, H ₂ 7-8%, CO ₂ 3-32%; Gas air velocity is 1500～10000h ^-1 ; ② The technical parameters of the dimethyl ether synthesis process are: Working temperature is 200～320℃ The working pressure is 2.0~8.0MPa; ③ The parameters of further absorption, decarburization and rectification of the synthetic product obtained in the dimethyl ether synthesis unit are: The absorption parameters of its absorption tower Gas inlet temperature: -10～40℃ Liquid inlet temperature: 10～60℃ Pressure inside the tower: 1.0~3.0Mpa, decarburization parameters of the decarburization tower Liquid inlet temperature: 150～210℃ Outlet temperature of tower kettle: 180～220℃ Pressure inside the tower: 1.0~2.0MPa, then enter the dimethyl ether rectification tower for rectification, its dimethyl ether rectification parameters Liquid inlet temperature: 180～200℃ Outlet temperature of tower kettle: 180～220℃ Pressure inside the tower: 0.6~1.5MPa. 2. A co-production method combining smelting reduction ironmaking, dimethyl ether production and power generation, characterized in that: the water vapor and dimethyl ether produced by the heat exchange of the coal gas produced in the smelting reduction ironmaking process through the heat exchanger The waste heat generated during the synthesis process enters the steam drum, and the steam obtained is used as power, and enters the steam turbine to drive the generator to generate electricity. The steam parameters used for power generation are: The steam pressure is 1~7Mpa, and the steam temperature is 130~300℃. 3. The method according to claim 1, characterized in that the catalyst is a copper-based methanol synthesis catalyst and a methanol dehydration catalyst, and the weight ratio of the two is 0.5-4. 4. The method according to claim 1, 3, characterized in that the copper-based methanol synthesis catalyst is any one of C301, C302, C306 or C207. 5. The method according to claim 1, 3, characterized in that the methanol dehydration catalyst is any one of molecular sieve ZSM-5 or gama-Al ₂ O ₃ . 6. The method according to claim 1, wherein the inert solvent is liquid paraffin, mineral oil, carboxane, alcohol or ether containing 18-35 carbon chains, chlorinated alkanes, aromatic hydrocarbons and any of its derivatives. 7. The method according to claim 1, characterized in that the gas with high calorific value produced in the smelting reduction ironmaking process needs to be processed by heat exchange, dust removal, fine desulfurization, deoxidation and pressure before entering the synthesis of dimethyl ether as a raw material device. 8. The method according to claim 1, 7, characterized in that the pressure of the gas entering the dimethyl ether synthesis unit is 2.0-8.0 MPa. 9. A cogeneration unit combining smelting reduction ironmaking, dimethyl ether production and power generation, comprising a smelting reduction ironmaking unit (S1), characterized in that: The device also includes a synthesis gas purification unit (S2), a dimethyl ether synthesis unit (S3), a product separation unit (S4) and a power generation unit (S5); among them: ①The synthesis gas purification device (S2) is composed of a heat exchanger (17), a synthesis gas purification tower (19), a compressor (21) and related pipelines (18, 20, 22, 23); the heat exchanger (17) The dust collector (06) of the smelting reduction ironmaking plant (S1) is connected through the pipeline (08,09), and is connected with the synthesis gas purification tower (19) through the pipeline (18), and the synthesis gas purification tower (19) passes through The pipeline (20) is connected to the compressor (21), and the heat exchanger (17) is connected to the steam drum (45) of the power generation device (S5) through the pipeline (23); ② The dimethyl ether synthesis unit (S3) consists of a heat exchanger (24), a slurry bed reactor (26), a primary separator (28) and related pipelines (25, 27, 29, 31, 32, 43) , the heat exchanger (24) is connected to the compressor (21) in the synthesis gas purification device (S2) through the pipeline (22), and is connected to the slurry bed reactor (26) through the pipeline (25), the slurry state Bed reactor (26) links to each other with primary separator (28) through pipeline (27,29), and primary separator (28) links to each other with heat exchanger (24) again through pipeline (31), and slurry bed reactor (26) link to each other with the steam bag (45) of power generation unit (S5) by pipeline (47), (30) at the top of slurry bed reactor 26 is the inlet of catalyst and inert solvent; ③ The product separation device (S4) consists of an absorption tower (33), a decarburization tower (37), a dimethyl ether rectification tower (39), a dimethyl ether storage tank (42) and corresponding pipelines (34, 35, 36 ) composition; the absorption tower (33) links to each other with the slurry bed reactor (26) in the dimethyl ether synthesis unit (S3) by the pipeline (36,43), and links to each other with the decarburization tower (37) by the pipeline (35) ), the absorption tower (33) is also connected with the heat exchanger (24) in the dimethyl ether synthesis unit (S3) through the pipeline (32), and is connected with the synthesis gas purification unit (S2) through the pipeline (34) Compressor (21) links to each other, and decarburization tower (37) links to each other with dimethyl ether rectifying tower (39) by pipeline (49), and the top of decarburization tower (37) has non-condensable gas outlet (38), dimethyl ether The tower top of ether rectification tower (39) links to each other with dimethyl ether fine storage tank (42) through pipeline (41), and outlet (40) is arranged at the bottom of the tower, simultaneously through pipeline (43) and slurry state reactor ( 26) connected; ④The power generation device (S5) is composed of a steam drum (45), a generator (48) and a pipeline (46), and the steam drum (45) is also connected with the synthesis gas purification device (S2) through pipelines (23) and (47) respectively. ) heat exchanger (17) is connected with the slurry bed reactor (26) of dimethyl ether synthesis unit (S3); In the entire cogeneration unit that combines smelting reduction ironmaking, dimethyl ether production and power generation, the smelting reduction ironmaking unit (S1) is connected to the synthesis gas purification unit (S2) through a pipeline (08), and the synthesis gas purification unit ( S2) is connected to the dimethyl ether synthesis unit (S3) and the power generation unit (S5) through pipelines (22) and (23) respectively, and the dimethyl ether synthesis unit (S3) is connected to each other through pipelines (32) and (47) respectively The product separation unit (S4) is connected to the power generation unit (S5). 10. The device according to claim 9, characterized in that the generator (48) can be a turbo generator or other generator.

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