System and method for preparing chemical products by using blast furnace gas and coke oven gas

Abstract

The invention provides a system and a method for preparing chemical products by using blast furnace gas and coke oven gas. The system comprises a coke oven gas hydrogenation device, a coke oven gas desulfurization device, a blast furnace gas hydrolysis device, a blast furnace gas desulfurization device, a reforming device and an alcohol synthesis device, wherein a discharge port of the coke oven gas hydrogenation device is connected with a feed port of the coke oven gas desulfurization device, a discharge port of the blast furnace gas hydrolysis device is connected with a feed port of the blast furnace gas desulfurization device, and a discharge port of the coke oven gas desulfurization device and a discharge port of the blast furnace gas desulfurization device are respectively connected with a feed port of the reforming device. And a discharge port of the reforming device is connected with a feed port of the alcohol synthesis device. The system can fully and effectively utilize methane and carbon dioxide contained in blast furnace gas and coke oven gas.

Description

Technical Field

[0001] The present invention relates to a system and method for preparing chemical products using blast furnace gas and coke oven gas. Background Art

[0002] Coke oven gas is a combustible gas obtained during the coking process. Generally, about 300 - 350 m 3 , 3 of coke oven gas can be produced per ton of dry coal, and about half of it is consumed by the coke oven itself. Coke oven gas is a mixture, and its yield and composition vary depending on the quality of the coking coal and the coking process conditions. A typical coke oven gas, by volume percentage, includes 55% - 70% hydrogen, 15% - 30% methane, 5% - 9% carbon monoxide, 2% - 5% carbon dioxide, 2% - 6% nitrogen, and trace impurities (such as coal tar, benzene, naphthalene, sulfur dioxide, organic sulfur, ammonia, thiophene, HCN, etc.). Coke oven gas can be used as fuel gas for city gas or power generation, or as a raw material for synthesizing ammonia, methanol, methane, etc., and has a wide range of uses.

[0003] Blast furnace gas is a by - product generated during the iron - making process. About 1500 m 3 of blast furnace gas is produced per ton of pig iron. A typical blast furnace gas, by volume percentage, includes 40 - 65% nitrogen, 0.5 - 5% hydrogen, 0.2 - 5% oxygen, 10 - 30% carbon dioxide, 10 - 30% carbon monoxide, 0.1 - 2.0% methane, and hydrogen sulfide and carbonyl sulfide, etc. Due to problems such as more dust, high content of inert gases, slow and unstable combustion, less heat release, and large flue gas volume, it is difficult to utilize blast furnace gas. Usually, it is directly or blended with coke oven gas as fuel gas to heat boilers to generate steam for power generation or drive large - scale equipment, with low economic benefits.

[0004] Currently, steel enterprises pay more and more attention to the comprehensive utilization of gas in order to reduce environmental pollution and improve economic benefits. Blast furnace gas and coke oven gas contain a large amount of hydrogen, methane, carbon monoxide, and carbon dioxide, etc., which can be used as chemical raw materials to synthesize chemical products after purification treatment.

[0005] CN111100714A discloses a method for producing H 2 / CO feed gas by combining coke oven gas with blast furnace gas or / and converter gas. Methane and carbon dioxide in the blast furnace gas are removed, and carbon monoxide is separated. Methane and carbon dioxide in the coke oven gas are removed, and hydrogen is separated. Then, ethylene glycol is synthesized using carbon monoxide and hydrogen as raw materials. In this method, methane and carbon dioxide in blast furnace gas and coke oven gas, as effective sources of carbon and hydrogen elements, are not fully utilized.

[0006] In general, there is still a need to study technical solutions that can achieve the full and effective utilization of blast furnace gas and coke oven gas (including the methane and carbon dioxide contained therein). Summary of the Invention

[0007] The object of the present invention is to provide a technical solution that can make full and effective use of blast furnace gas and coke oven gas, including methane and carbon dioxide contained therein.

[0008] To solve the above problems, the present invention provides the following two aspects of technical solutions.

[0009] In the first aspect, the present invention provides a system for preparing chemical products using blast furnace gas and coke oven gas. Among them, the system includes:

[0010] Coke oven gas hydrogenation device, coke oven gas desulfurization device, blast furnace gas hydrolysis device, blast furnace gas desulfurization device, reforming device, alcohol synthesis device;

[0011] Among them, the outlet of the coke oven gas hydrogenation device is connected to the inlet of the coke oven gas desulfurization device, the outlet of the blast furnace gas hydrolysis device is connected to the inlet of the blast furnace gas desulfurization device, the outlets of the coke oven gas desulfurization device and the blast furnace gas desulfurization device are respectively connected to the inlet of the reforming device, and the outlet of the reforming device is connected to the inlet of the alcohol synthesis device.

[0012] In the above system for preparing chemical products using blast furnace gas and coke oven gas, the coke oven gas is desulfurized after hydrogenation reaction, and the blast furnace gas is desulfurized after hydrolysis reaction. The products after desulfurization of both are mixed and subjected to reforming reaction to obtain syngas, and the syngas is subjected to alcohol synthesis to obtain alcohol chemical products. The full and effective utilization of hydrocarbon components such as methane, carbon dioxide, hydrogen, carbon monoxide, water and other components in blast furnace gas and coke oven gas is realized. Among them, during the hydrogenation reaction of coke oven gas in the coke oven gas hydrogenation device, the unsaturated hydrocarbons in the coke oven gas react with hydrogen in the coke oven gas to be converted into saturated hydrocarbons, and the organic sulfur in the coke oven gas, mainly carbonyl sulfide, reacts with hydrogen in the coke oven gas to be converted into hydrogen sulfide; during the hydrolysis reaction of blast furnace gas in the blast furnace gas hydrolysis device, the organic sulfur in the blast furnace gas, mainly carbonyl sulfide, undergoes hydrolysis reaction with saturated water in the blast furnace gas to be converted into hydrogen sulfide. During the reforming reaction, saturated hydrocarbon components such as methane react with carbon dioxide and water to be converted into hydrogen and carbon monoxide.

[0013] According to a preferred embodiment of the first aspect, the system further includes a coke oven gas adsorption device, and the outlet of the coke oven gas adsorption device is connected to the inlet of the coke oven gas hydrogenation device. In the coke oven gas adsorption device, tar, benzene, naphthalene and most sulfides in the coke oven gas can be adsorbed and removed.

[0014] According to a preferred embodiment of the first aspect, the system further includes a TRT power generation device, which is arranged before the blast furnace gas hydrolysis device to generate electricity by utilizing the energy provided by the temperature and pressure of the blast furnace gas.

[0015] According to a preferred embodiment of the first aspect, the system further includes a blast furnace gas dust removal device, which is arranged before the TRT power generation device.

[0016] According to a preferred embodiment of the first aspect, the system further includes a gas-liquid separator and a rectification device. The feed inlet of the gas-liquid separator is connected to the discharge outlet of the alcohol synthesis device, the liquid phase outlet of the gas-liquid separator is connected to the feed inlet of the rectification device, and the rectification device is used to fractionate and obtain alcohol products.

[0017] Further, the system further includes a recycle compressor. The feed inlet of the recycle compressor is connected to the gas phase outlet of the gas-liquid separator, and the discharge outlet of the recycle compressor is connected to the reforming device.

[0018] Further, the system further includes a recycle pump. The pump inlet of the recycle pump is connected to the water outlet of the rectification device, and the pump outlet of the recycle pump is connected to the reforming device.

[0019] According to a preferred embodiment of the first aspect, the reforming device is a shell-and-tube reactor.

[0020] In a second aspect, the present invention provides a method for preparing chemical products by using blast furnace gas and coke oven gas. This method is carried out using the system for preparing chemical products by using blast furnace gas and coke oven gas provided in the first aspect. The method includes:

[0021] The coke oven gas enters the coke oven gas hydrogenation device and contacts with a hydrogenation catalyst to carry out a hydrogenation reaction. Among them, the unsaturated hydrocarbons in the coke oven gas react with the hydrogen in the coke oven gas to be converted into saturated hydrocarbons, and the organic sulfur in the coke oven gas reacts with the hydrogen in the coke oven gas to be converted into hydrogen sulfide.

[0022] The coke oven gas after the hydrogenation reaction enters the coke oven gas desulfurization device and contacts with a desulfurizing agent to carry out desulfurization to obtain the desulfurized coke oven gas.

[0023] The blast furnace gas enters the blast furnace gas hydrolysis device and contacts with a hydrolysis catalyst to carry out a hydrolysis reaction. Among them, the organic sulfur in the blast furnace gas reacts with the water in the blast furnace gas to be converted into hydrogen sulfide.

[0024] The blast furnace gas after the hydrolysis reaction enters the blast furnace gas desulfurization device and contacts with a desulfurizing agent to carry out desulfurization to obtain the desulfurized blast furnace gas.

[0025] The desulfurized coke oven gas is mixed with the desulfurized blast furnace gas and contacts with a methane reforming catalyst in a reforming unit to carry out a reforming reaction to obtain syngas; among them, saturated alkanes including methane react with carbon dioxide and water to be converted into hydrogen and carbon monoxide;

[0026] The syngas contacts with an alcohol synthesis catalyst in an alcohol synthesis unit to carry out an alcohol synthesis reaction to obtain alcohol chemical products.

[0027] According to a preferred embodiment of the second aspect, wherein, by volume, the usage ratio of the coke oven gas to the blast furnace gas is 1:1 - 1:3.

[0028] According to a preferred embodiment of the second aspect, wherein, based on the volume of the coke oven gas being 100%, the coke oven gas contains 55% - 70% of hydrogen, 15% - 30% of methane, 5% - 9% of carbon monoxide, 2% - 5% of carbon dioxide, 2% - 6% of nitrogen, and the balance of impurities; wherein, the impurities include unsaturated hydrocarbons, organic sulfur, optionally coal tar, optionally sulfur dioxide, optionally ammonia, optionally thiophene, optionally HCN, etc.

[0029] According to a preferred embodiment of the second aspect, wherein, based on the volume of the blast furnace gas being 100%, the blast furnace gas includes 40 - 65% of nitrogen, 0.5 - 5% of hydrogen, 0.2 - 5% of oxygen, 10 - 30% of carbon dioxide, 10 - 30% of carbon monoxide, 0.1 - 2.0% of methane, 0.05 - 1% of water, and the balance of impurities; wherein, the impurities include hydrogen sulfide and organic sulfur, etc.

[0030] According to a preferred embodiment of the second aspect, wherein, the volume ratio of hydrogen to carbon monoxide in the syngas is 0.5:1 - 3:1.

[0031] According to a preferred embodiment of the second aspect, wherein, the hydrogenation catalyst includes at least one of an iron - molybdenum hydrogenation catalyst and a nickel - molybdenum hydrogenation catalyst;

[0032] Further, the temperature of the hydrogenation reaction is 200 - 400°C and the pressure is 0.1 - 3 MPa.

[0033] According to a preferred embodiment of the second aspect, wherein, the hydrolysis catalyst is an alumina hydrolyzing agent;

[0034] Further, the temperature of the hydrolysis reaction is from normal temperature to 400°C and the pressure is 0.1 - 3 MPa.

[0035] According to a preferred embodiment of the second aspect, wherein, the desulfurizer in the coke oven gas desulfurization device is a desulfurizer capable of removing hydrogen sulfide in the coke oven gas after the hydrogenation reaction to below 50 ppb;

[0036] Further, the desulfurizer in the coke oven gas desulfurization device includes at least one of iron-manganese desulfurizer and zinc oxide desulfurizer;

[0037] Furthermore, the temperature for desulfurization in the coke oven gas desulfurization device is room temperature - 400 °C, and the pressure is 0.1 - 3 MPa.

[0038] According to the preferred embodiment of the second aspect, wherein the desulfurizer in the blast furnace gas desulfurization device is selected to be able to remove hydrogen sulfide in the blast furnace gas after hydrolysis reaction to below 50 ppb;

[0039] Further, the desulfurizer in the blast furnace gas desulfurization device includes at least one of iron-manganese desulfurizer and zinc oxide desulfurizer;

[0040] Furthermore, the temperature for desulfurization in the blast furnace gas desulfurization device is room temperature - 400 °C, and the pressure is 0.1 - 3 MPa.

[0041] According to the preferred embodiment of the second aspect, wherein the methane reforming catalyst includes at least one of nickel-based reforming catalyst and platinum-based noble metal catalyst;

[0042] Further, the temperature of the reforming reaction is 600 - 1000 °C, and the pressure is 0.1 - 2 MPa.

[0043] According to the preferred embodiment of the second aspect, wherein the alcohol synthesis catalyst is selected from methanol synthesis catalyst, ethanol synthesis catalyst or lower carbon mixed alcohol (lower carbon refers to C1 - C5) synthesis catalyst;

[0044] Further, the methanol synthesis catalyst is selected as a copper-based catalyst;

[0045] Further, the ethanol synthesis catalyst is selected as a rhodium-based catalyst

[0046] Further, the lower carbon mixed alcohol synthesis catalyst is selected as a molybdenum-based catalyst;

[0047] Further, the temperature of the alcohol synthesis reaction is 200 - 500 °C, and the pressure is 0.1 - 10 MPa.

[0048] According to the preferred embodiment of the second aspect, wherein the method for preparing chemical products using blast furnace gas and coke oven gas further includes:

[0049] Before the coke oven gas enters the coke oven gas hydrogenation device, it first enters the coke oven gas adsorption device, contacts with the adsorbent, and undergoes adsorption to remove tar, benzene, naphthalene, and sulfides in the coke oven gas;

[0050] Further, the adsorption device includes two parallel adsorption towers, the adsorption towers are filled with adsorbent, and the two adsorption towers can be used alternately for adsorption-regeneration cycle operation;

[0051] Further, the adsorbent is a molecular sieve adsorbent;

[0052] Furthermore, the molecular sieve adsorbent includes at least one of A-type molecular sieve, X-type molecular sieve and carbon molecular sieve;

[0053] Furthermore, the adsorption pressure is 0.1 - 0.5 MPa and the temperature is normal temperature - 50 °C;

[0054] Furthermore, the method for preparing chemical products using blast furnace gas and coke oven gas further includes: after the adsorbent in the coke oven gas adsorption device is saturated by adsorption, the adsorbent is regenerated; wherein, the regeneration treatment is achieved by purging with steam at 110 - 150 °C under normal pressure - 0.5 MPa;

[0055] In a specific embodiment, the adsorption device includes two parallel adsorption towers. The first adsorption tower adsorbs impurities at normal pressure - 0.5 MPa and normal temperature - 50 °C, and discharges the purified coke oven gas. After being saturated by adsorption, it is switched to the second adsorption tower for adsorption. At the same time, the pressure of the first adsorption tower is reduced to normal pressure - 0.5 MPa, and the first adsorption tower is purged with steam at 110 - 150 °C to regenerate the adsorbent. After the second adsorption tower is saturated by adsorption, it is switched to the first adsorption tower for adsorption, and the second adsorption tower repeats the regeneration operation of the first adsorption tower. In this way, continuous adsorption and regeneration of the adsorbent are achieved.

[0056] According to the preferred embodiment of the second aspect, wherein the method for preparing chemical products using blast furnace gas and coke oven gas further includes:

[0057] Before the blast furnace gas enters the blast furnace gas hydrolysis device, it first enters the blast furnace gas dust removal device for dust removal.

[0058] According to the preferred embodiment of the second aspect, wherein the method for preparing chemical products using blast furnace gas and coke oven gas further includes:

[0059] Before the blast furnace gas enters the blast furnace gas hydrolysis device, it first enters the TRT power generation device to recover the energy of the blast furnace gas for power generation.

[0060] According to the preferred embodiment of the second aspect, wherein the method for preparing chemical products using blast furnace gas and coke oven gas further includes:

[0061] The product after the alcohol synthesis reaction enters a gas-liquid separator for gas-liquid separation;

[0062] The liquid-phase product obtained by gas-liquid separation enters a distillation device for separation and purification to obtain a purified alcohol chemical product;

[0063] Further, the method for preparing chemical products using blast furnace gas and coke oven gas further includes:

[0064] Transporting the gas-phase product obtained from gas-liquid separation back to the reforming unit for reuse;

[0065] Further, the method for preparing chemical products using blast furnace gas and coke oven gas further includes:

[0066] Transporting the water obtained from the distillation unit back to the reforming unit for reuse.

[0067] For the technical solution provided by the present invention, the coke oven gas is desulfurized after hydrogenation reaction, and the blast furnace gas is desulfurized after hydrolysis reaction. The products after desulfurization of both are mixed for reforming reaction to obtain syngas, and the syngas is subjected to alcohol synthesis to obtain alcohol chemical products. The full and effective utilization of hydrocarbon components such as methane, carbon dioxide, hydrogen, carbon monoxide, water, etc. in blast furnace gas and coke oven gas is realized. Compared with the prior art, the technical solution provided by the present invention has the following beneficial effects:

[0068] 1. For the technical solution provided by the present invention, neither methane nor carbon dioxide in coke oven gas and blast furnace gas is removed. Instead, methane and carbon dioxide are used to undergo reforming reaction to generate carbon monoxide and hydrogen, improving the utilization rate of carbon and hydrogen elements, increasing the yield of syngas and downstream products, and at the same time reducing greenhouse gas emissions.

[0069] 2. For the technical solution provided by the present invention, coke oven gas and blast furnace gas are efficiently utilized to produce chemical products such as methanol and ethanol, improving economic benefits.

[0070] 3. For the technical solution provided by the present invention, methane in coke oven gas and carbon dioxide in blast furnace gas are effectively utilized, reducing greenhouse gas emissions and improving energy utilization efficiency.

[0071] 4. For the technical solution provided by the present invention, the solution is flexible, and the catalyst of the synthesis unit can be adjusted according to market needs to produce different alcohol products. BRIEF DESCRIPTION OF THE DRAWINGS

[0072] Figure 1 It is a schematic structural diagram of the system for preparing chemical products using blast furnace gas and coke oven gas in Example 1. DETAILED DESCRIPTION OF THE INVENTION

[0073] In order to have a clearer understanding of the technical features, objectives, and beneficial effects of the present invention, the technical solution of the present invention will be described in detail below, but it should not be construed as a limitation on the implementable scope of the present invention.

[0074] Example 1

[0075] This embodiment provides a system for preparing chemical products using blast furnace gas and coke oven gas, such as Figure 1 As shown, the system includes a coke oven gas adsorption device 1, a coke oven gas hydrogenation device 2, a coke oven gas desulfurization device 3-1, a blast furnace gas dedusting device 4, a TRT power generation device 5, a blast furnace gas hydrolysis device 6, a blast furnace gas desulfurization device 3-2, a reforming device 7, an alcohol synthesis device 8, a gas-liquid separator 8, a rectification device 10, a circulation pump 11, and a circulation compressor 12.

[0076] Among them, the coke oven gas adsorption device 1, the coke oven gas hydrogenation device 2, and the coke oven gas desulfurization device 3-1 are connected in series in sequence. The blast furnace gas dedusting device 4, the TRT power generation device 5, the blast furnace gas hydrolysis device 6, and the blast furnace gas desulfurization device 3-2 are connected in series in sequence. The discharge port of the coke oven gas desulfurization device 3-1 and the discharge port of the blast furnace gas desulfurization device 3-2 are respectively connected to the feed port of the reforming device 7. The discharge port of the reforming device 7 is connected to the feed port of the alcohol synthesis device 8. The discharge port of the alcohol synthesis device 8 is connected to the feed port of the gas-liquid separator 9. The liquid phase outlet of the gas-liquid separator 8 is connected to the feed port of the rectification device 10. The rectification device 10 is used to fractionate and produce alcohol products. The feed port of the circulation compressor 12 is connected to the gas phase outlet of the gas-liquid separator 9. The discharge port of the circulation compressor 12 is connected to the reforming device 7. The pump inlet of the circulation pump 11 is connected to the water outlet of the rectification device 10. The pump outlet of the circulation pump 11 is connected to the reforming device 7.

[0077] Among them, the reforming device 7 selects a shell-and-tube reactor.

[0078] Among them, the coke oven gas desulfurization device 3-1 consists of three series-connected desulfurization towers.

[0079] Among them, the coke oven gas hydrogenation device 2 selects one hydrogenation reactor.

[0080] Among them, the blast furnace gas dedusting device 4 selects a dry dedusting equipment.

[0081] Among them, the blast furnace gas hydrolysis device 6 consists of three series-connected hydrolysis reactors.

[0082] Among them, the blast furnace gas desulfurization device 3-2 consists of three series-connected desulfurization towers.

[0083] Among them, the coke oven gas adsorption device 1 consists of two parallel adsorption towers.

[0084] Embodiment 2

[0085] This embodiment provides a method for preparing chemical products using blast furnace gas and coke oven gas. This method is carried out using the system for preparing chemical products using blast furnace gas and coke oven gas provided in Embodiment 1. This method includes:

[0086] Step 1, the coking gas treatment step, specifically including:

[0087] 1.1. The coking gas enters the coking gas adsorption device 1 and contacts the 13X molecular sieve adsorbent filled in the coking gas adsorption device 1 to adsorb and remove impurities such as tar, benzene, naphthalene, dust, and hydrogen sulfide in the coking gas;

[0088] Among them, the flow rate of the coking gas is 30000m 3 / h;

[0089] Among them, based on the volume of the coking gas being 100%, the methane content in the coking gas is 25%, the carbon dioxide content is 4%, the hydrogen content is 55%, the carbon monoxide content is 8%, the nitrogen content is 1%, the hydrogen sulfide content is 200 ppm, the carbonyl sulfide content is 500 ppm, and the balance is unsaturated hydrocarbons (including benzene and naphthalene), tar, dust and other impurities;

[0090] Among them, the two adsorption towers are used alternately to realize the adsorption-regeneration cycle operation; specifically, the first adsorption tower adsorbs impurities at 0.5 MPa and normal temperature, discharges the purified coking gas, and after adsorption saturation, switches to the second adsorption tower for adsorption. At the same time, the pressure of the first adsorption tower is reduced to atmospheric pressure, and the first adsorption tower is purged with 150 °C steam to regenerate the adsorbent. After the second adsorption tower is adsorbed and saturated, it switches back to the first adsorption tower for adsorption, and the second adsorption tower repeats the regeneration operation of the first adsorption tower. In this way, the adsorbent continuously adsorbs and regenerates.

[0091] 1.2. The coking gas after adsorption treatment enters the coking gas hydrogenation device 2 and contacts the 30 cubic meters of nickel-molybdenum hydrogenation catalyst (produced by Shenyang Sanju Kate Co., Ltd., model T202) filled in the coking gas hydrogenation device 2 to carry out the hydrogenation reaction; among them, the unsaturated hydrocarbons in the coking gas react with the hydrogen in the coking gas to be converted into saturated hydrocarbons, and the carbonyl sulfide in the coking gas reacts with the hydrogen in the coking gas to be converted into hydrogen sulfide;

[0092] Among them, the temperature of the hydrogenation reaction is 350 °C and the pressure is 2 MPa.

[0093] 1.3. The coking gas after the hydrogenation reaction enters the coking gas desulfurization device 3-1 and contacts the 15 cubic meters of zinc oxide desulfurizer filled in the coking gas desulfurization device 3-1 to carry out desulfurization, and the hydrogen sulfide in the coking gas is removed to below 50 ppb to obtain the desulfurized coking gas;

[0094] Among them, the temperature of desulfurization is 200 °C and the pressure is 2 MPa.

[0095] Step 2, the blast furnace gas treatment step, specifically including:

[0096] 2.1. The blast furnace gas enters the blast furnace gas dust removal device 4 for dust removal;

[0097] Among them, the flow rate of the blast furnace gas is 50,000 m 3 / h;

[0098] Among them, based on the volume of the blast furnace gas being 100%, the methane content in the blast furnace gas is 1%, the carbon dioxide content is 20%, the hydrogen content is 2%, the carbon monoxide content is 25%, the nitrogen content is 50%, the water content is 0.5%, the hydrogen sulfide content is 50 ppm, the carbonyl sulfide content is 200 ppm, and the balance is dust and other impurities.

[0099] 2.2. The dust-removed blast furnace gas enters the TRT power generation device 5 to recover the energy of the blast furnace gas for power generation.

[0100] 2.3. The blast furnace gas discharged from the TRT power generation device 5 enters the blast furnace gas hydrolysis device 6 and contacts the 60 cubic meters of alumina hydrolysis catalyst loaded in the blast furnace gas hydrolysis device 6 for hydrolysis reaction; among them, the carbonyl sulfide in the blast furnace gas reacts with the water in the blast furnace gas to be converted into hydrogen sulfide;

[0101] The temperature of the hydrolysis reaction is 200 °C and the pressure is 2 MPa.

[0102] 2.4. The blast furnace gas after the hydrolysis reaction enters the blast furnace gas desulfurization device 3-2 and contacts the 30 cubic meters of zinc oxide desulfurization agent loaded in the blast furnace gas desulfurization device 3-2 for desulfurization, and the hydrogen sulfide in the blast furnace gas is removed to below 50 ppb to obtain the desulfurized blast furnace gas;

[0103] Among them, the temperature of the desulfurization is 200 °C and the pressure is 2 MPa.

[0104] 3. The desulfurized coke oven gas is mixed with the desulfurized blast furnace gas and contacts the 16 cubic meters of nickel-based methane reforming catalyst (the active component nickel oxide accounts for about 30%) in the reforming device 7 for reforming reaction to obtain syngas; among them, the saturated alkanes including methane react with carbon dioxide and water to be converted into hydrogen and carbon monoxide;

[0105] Among them, the temperature of the reforming reaction is 800 °C and the pressure is 0.5 MPa;

[0106] Among them, the ratio of hydrogen to carbon monoxide in the syngas is 1.08:1.

[0107] 4. The syngas contacts the 16 cubic meters of copper-based methanol synthesis catalyst (Sinopec Nanjing Research Institute of Chemical Industry, model C308) loaded in the alcohol synthesis device 8 in the alcohol synthesis device 8 for alcohol synthesis reaction;

[0108] Among them, the temperature of the alcohol synthesis reaction is 220 °C and the pressure is 5 MPa.

[0109] 5. The product after the alcohol synthesis reaction enters the gas-liquid separator 9 for gas-liquid separation. The liquid-phase product enters the rectification device 10 for subsequent treatment, and the gas-phase product is transported back to the reforming device for reuse.

[0110] 6. The liquid-phase product obtained by gas-liquid separation enters the rectification device for separation and purification to obtain purified methanol and water. The methanol is used as an alcohol chemical product, with a methanol purity of over 99%, a production rate of approximately 68 tons per hour, and the water is transported back to the reforming device for reuse.

[0111] The above are only the preferred embodiments of the present invention and are not intended to limit the present invention. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention shall be included within the protection scope of the present invention.

Claims

1. A system for preparing chemical products using blast furnace gas and coke oven gas, wherein, the system includes: a coke oven gas hydrogenation unit, a coke oven gas desulfurization unit, a blast furnace gas hydrolysis unit, a blast furnace gas desulfurization unit, a reforming unit, and an alcohol synthesis unit; wherein, the outlet of the coke oven gas hydrogenation unit is connected to the inlet of the coke oven gas desulfurization unit, the outlet of the blast furnace gas hydrolysis unit is connected to the inlet of the blast furnace gas desulfurization unit, the outlets of the coke oven gas desulfurization unit and the blast furnace gas desulfurization unit are respectively connected to the inlet of the reforming unit, and the outlet of the reforming unit is connected to the inlet of the alcohol synthesis unit.

2. The system according to claim 1, wherein, the system further includes a coke oven gas adsorption unit, and the outlet of the coke oven gas adsorption unit is connected to the inlet of the coke oven gas hydrogenation unit.

3. The system according to claim 1, wherein, the system further includes a TRT power generation unit, which is arranged before the blast furnace gas hydrolysis unit to generate electricity by utilizing the energy provided by the temperature and pressure of the blast furnace gas; the system further includes a blast furnace gas dust removal unit, which is arranged before the TRT power generation unit.

4. The system according to claim 1, wherein, the system further includes a gas-liquid separator and a rectification unit. The inlet of the gas-liquid separator is connected to the outlet of the alcohol synthesis unit, the liquid phase outlet of the gas-liquid separator is connected to the inlet of the rectification unit, and the rectification unit is used to fractionate and produce alcohol products.

5. The system according to claim 4, wherein, the system further includes a recycle compressor, the inlet of the recycle compressor is connected to the gas phase outlet of the gas-liquid separator, and the outlet of the recycle compressor is connected to the reforming unit; and / or the system further includes a recycle pump, the pump inlet of the recycle pump is connected to the water outlet of the rectification unit, and the pump outlet of the recycle pump is connected to the reforming unit.

6. A method for preparing chemical products using blast furnace gas and coke oven gas, which uses the system for preparing chemical products using blast furnace gas and coke oven gas according to any one of claims 1-5, and the method includes: The coke oven gas enters the coke oven gas hydrogenation unit and contacts with a hydrogenation catalyst for a hydrogenation reaction; wherein, the unsaturated hydrocarbons in the coke oven gas react with the hydrogen in the coke oven gas to be converted into saturated hydrocarbons, and the organic sulfur in the coke oven gas reacts with the hydrogen in the coke oven gas to be converted into hydrogen sulfide; The coke oven gas after the hydrogenation reaction enters the coke oven gas desulfurization unit and contacts with a desulfurizing agent for desulfurization to obtain desulfurized coke oven gas; The blast furnace gas enters the blast furnace gas hydrolysis unit and contacts with a hydrolysis catalyst for a hydrolysis reaction; wherein, the organic sulfur in the blast furnace gas reacts with the water in the blast furnace gas to be converted into hydrogen sulfide; The blast furnace gas after the hydrolysis reaction enters the blast furnace gas desulfurization unit and contacts with a desulfurizing agent for desulfurization to obtain desulfurized blast furnace gas; The desulfurized coke oven gas is mixed with the desulfurized blast furnace gas and contacts a methane reforming catalyst in a reforming unit to carry out a reforming reaction to obtain syngas; wherein, saturated alkanes including methane react with carbon dioxide and water to be converted into hydrogen and carbon monoxide. The syngas contacts an alcohol synthesis catalyst in an alcohol synthesis unit to carry out an alcohol synthesis reaction to obtain alcohol chemical products.

7. The method according to claim 6, wherein, Based on the volume of the coke oven gas being 100%, the coke oven gas contains 55%-70% hydrogen, 15%-30% methane, 5%-9% carbon monoxide, 2%-5% carbon dioxide, 2%-6% nitrogen, and the balance of impurities; wherein, the impurities include unsaturated hydrocarbons, organic sulfur, optionally coal tar, optionally sulfur dioxide, optionally ammonia, optionally thiophene, optionally HCN. Based on the volume of the blast furnace gas being 100%, the blast furnace gas includes 40-65% nitrogen, 0.5-5% hydrogen, 0.2-5% oxygen, 10-30% carbon dioxide, 10-30% carbon monoxide, 0.1-2.0% methane, 0.05-1% water, and the balance of impurities; wherein, the impurities include hydrogen sulfide and organic sulfur, etc. By volume, the usage ratio of the coke oven gas to the blast furnace gas is 1:1-1:

3.

8. The method according to claim 6, wherein, The volume ratio of hydrogen to carbon monoxide in the syngas is 0.5:1-3:

1.

9. The method according to claim 6, wherein, The hydrogenation catalyst includes at least one of an iron-molybdenum hydrogenation catalyst and a nickel-molybdenum hydrogenation catalyst; and / or The hydrolysis catalyst is selected from an alumina hydrolysis agent; and / or The methane reforming catalyst includes at least one of a nickel-based reforming catalyst and a platinum-based noble metal catalyst; and / or The alcohol synthesis catalyst is selected from a methanol synthesis catalyst, an ethanol synthesis catalyst or a lower-carbon mixed alcohol synthesis catalyst; wherein, the methanol synthesis catalyst is selected from a copper-based catalyst; wherein, the ethanol synthesis catalyst is selected from a rhodium-based catalyst; wherein, the lower-carbon mixed alcohol synthesis catalyst is selected from a molybdenum-based catalyst; and / or The desulfurizer in the coke oven gas desulfurization unit includes at least one of an iron-manganese desulfurizer and a zinc oxide desulfurizer; and / or The desulfurizer in the blast furnace gas desulfurization unit includes at least one of an iron-manganese desulfurizer and a zinc oxide desulfurizer.

10. The method according to claim 9, wherein, The temperature of the hydrogenation reaction is 200-400°C and the pressure is 0.1-3 MPa; and / or The temperature of the hydrolysis reaction is from room temperature to 400°C and the pressure is 0.1-3 MPa; and / or The temperature of the reforming reaction is 600-1000°C and the pressure is 0.1-2 MPa; and / or The temperature of the alcohol synthesis reaction is 200-500°C and the pressure is 0.1-10 MPa; and / or The temperature for desulfurization in the coke oven gas desulfurization unit is from room temperature to 400°C and the pressure is 0.1-3 MPa; and / or The temperature for desulfurization in the blast furnace gas desulfurization unit is from room temperature to 400°C and the pressure is 0.1-3 MPa.

11. The method according to claim 6, wherein, The method for preparing chemical products using blast furnace gas and coke oven gas further includes: Before the coke oven gas enters the coke oven gas hydrogenation unit, it first enters the coke oven gas adsorption unit, contacts with the adsorbent, and undergoes adsorption to remove tar, benzene, naphthalene, and sulfides in the coke oven gas.

12. The method according to claim 11, wherein, the adsorbent is selected as a molecular sieve adsorbent; the molecular sieve adsorbent includes at least one of A-type molecular sieve, X-type molecular sieve, and carbon molecular sieve.

13. The method according to claim 6, wherein, the method for preparing chemical products using blast furnace gas and coke oven gas further includes: Before the blast furnace gas enters the blast furnace gas hydrolysis unit, it first enters the blast furnace gas dust removal unit for dust removal; and / or Before the blast furnace gas enters the blast furnace gas hydrolysis unit, it first enters the TRT power generation unit to recover the energy of the blast furnace gas for power generation.

14. The method according to claim 6, wherein, the method for preparing chemical products using blast furnace gas and coke oven gas further includes: The product after the alcohol synthesis reaction enters a gas-liquid separator for gas-liquid separation; The liquid-phase product obtained from the gas-liquid separation enters a rectification unit for separation and purification to obtain a purified alcohol chemical product.

15. The method according to claim 14, wherein, the method for preparing chemical products using blast furnace gas and coke oven gas further includes: The gas-phase product obtained from the gas-liquid separation is transported back to the reforming unit for reuse; and / or The water obtained from the rectification unit is transported back to the reforming unit for reuse.

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