CN103160294B - Omnibearing coproduction system and method by utilizing coal grading - Google Patents
Omnibearing coproduction system and method by utilizing coal grading Download PDFInfo
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- CN103160294B CN103160294B CN201310109786.6A CN201310109786A CN103160294B CN 103160294 B CN103160294 B CN 103160294B CN 201310109786 A CN201310109786 A CN 201310109786A CN 103160294 B CN103160294 B CN 103160294B
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The invention provides an omnibearing coproduction system and method by utilizing coal grading. A standby coal system is respectively connected with a lump coal pyrolysis system and a pea coal pyrolysis system; a gasification system uses air as an input, semicoke generated by the pea coal pyrolysis system as a raw material, and generated gasified coal gas as a heat carrier of the lump coal pyrolysis system; lump coal pyrolysis oil gas generated by the lump coal pyrolysis system is used as a heat carrier of the pea coal pyrolysis system, part of generated lump coke is output as metallurgical coke, and the rest lump coke is used as a raw material for preparing carbide; pyrolysis coal gas generated by the pea coal pyrolysis system enters a crude gas treatment system, generated pyrolysis tar is used for hydrogenation grading, and generated semicoke is respectively used as semicoke for power generation and semicoke for gasification; and the crude gas treatment system uses pyrolysis coal gas generated by the pea coal pyrolysis system as a raw material, generated recovery waste heat is applied to a waste heat boiler of a power generation system, and generated carbon dioxide enters a carbon dioxide displaced coal gas system.
Description
Technical field
The present invention relates to technical field of coal chemical industry, thereby relate in particular to the field of realizing oil, gas, change, electric Poly-generation take wholegrain footpath coal as raw material.
Background technology
China is maximum in the world coal production state and country of consumption, from Energy resources and the level of economic development of China, within considerable time, coal will be the topmost energy of China, but the direct utilization of coal also exists a series of pollution problems except coal utilization efficiency is low.
Compared with the directions such as the leading sub-prime clean conversion technology of pyrolytic technique and other coal combustion generatings, gelatin liquefaction, gasification and gasification downstream, at aspects such as investment intensity, Technical Economy, energy conversion efficiency, all having obvious advantage, is the optimum way of coal comprehensive utilization.The high-efficiency cleaning pyrolytic process of coal is divided into lump coal pyrolysis and pulverized coal pyrolysis technique according to raw material particle size difference at present.
In the pyrolytic process for take fine coal as raw material, exist generation granularity of dust little, content is high, the problems such as the solid separating effect of pyrolysis coke breeze and pyrolysis oil gas High Temperature Gas is undesirable, finally cause in coal tar ash oontent high, second-rate, cannot reach the quality index of the further deep processing of coal tar; And pyrolytic process take lump coal as raw material requires height to raw material particle size, cannot be applicable to a large amount of fine coal that produce in existing exploitation situation.
Meanwhile, the Poly-generation technology take coal as raw material is gas head mainly with Single gas or pyrolysis of coal technology at present.The technology that turns to gas head with Single gas relies on merely CO transformationreation to adjust ratio of carbon-hydrogen in raw gas to meet the demand of further part, thereby has increased the complicacy of system and technology, and has increased CO
2discharge.And the reasonable utilization of a large amount of semicokes that produce in the single pyrolytic technique process take pyrolysis of coal technology as gas head becomes the principal element of restriction pyrolysis of coal scale development.
Summary of the invention
Low in order to solve coal utilizaton rate, Single gas or poor, the specific pyrolysis system Suitability of Coals of coal pyrolysis gas head Poly-generation adjustability oil-gas high-temperature weak and pulverized coal pyrolysis separates the problems such as undesirable, the invention provides a kind of comprehensive coal sub-prime and utilize the system and method for Poly-generation.
For solving above technical problem, the present invention by the following technical solutions:
Comprehensive coal sub-prime is utilized a system for Poly-generation, comprises standby coal measures system, lump coal pyrolysis system, beans pyrolysis system, raw gas treatment system, and gasification system; Wherein, the outlet of standby coal measures system is connected with beans pyrolysis system with lump coal pyrolysis system respectively; Gasification system is take air as input, and the semicoke producing take beans pyrolysis system is as raw material, and the gasification gas of generation is as the thermal barrier of lump coal pyrolysis system; The lump coal pyrolysis oil gas that lump coal pyrolysis system produces is as the thermal barrier of beans pyrolysis system, and a lump coke part for generation is exported as metallurgical coke, and a part of lump coke is as the raw material of calcium carbide processed in addition; The pyrolysis coal gas that beans pyrolysis system produces enters raw gas treatment system and does further processing, and the pyrolytic tar of generation is for hydrogenation upgrading, and the semicoke of generation is respectively as semicoke and gasification semicoke for generating; The pyrolysis coal gas that raw gas treatment system produces take beans pyrolysis system is as raw material, the sulphur of its generation is as output of products, the recovery waste heat producing is for the waste heat boiler of power generation system, the carbonic acid gas producing enters carbonic acid gas displacement coal gas gas train, and the purification coal gas of generation is respectively as synthetic gas, synthetic gas used for Fischer-Tropsch synthesis, synthetic gas and hydrogen manufacturing coal gas for alkylation for Sweet natural gas.
Described system further comprises hydrogen recovery system, the purification coal gas that described hydrogen recovery system produces take raw gas treatment system is as raw material, produce after treatment hydrogen and dehydrogenation coal gas, wherein, hydrogen is divided into three parts, a part is output directly, a part is sent in hydrofining oil system with hydrogen as oil product upgrading, a part is sent in chemical synthesis system with hydrogen as MEG processed, dehydrogenation coal gas is divided into two portions, a part is as coal for power generation gas, and another part is sent in chemical synthesis system with coal gas as MEG processed.
Described system further includes hydrofining oil system, the hydrogen that the pyrolytic tar that this hydrofining oil system produces take beans pyrolysis system and hydrogen recovery system produce carries out oil product upgrading as raw material, obtain hydrogenation processed oil and petroleum naphtha, wherein, described petroleum naphtha is as the raw material of chemical synthesis system.
The hydrogen that described chemical synthesis system produces take hydrogen recovery system and dehydrogenation coal gas are raw material generation MEG; The petroleum naphtha that the purification coal gas producing take raw gas treatment system and hydrofining oil system produce is raw material generation PX, PX obtains PTA through oxidation, produces PET, wherein take PTA and MEG as raw material, PTA is as output of products for a part, and a part of PTA enters into calcium carbide industrial system in addition.
Described beans pyrolysis system comprises beans pyrolysis oven, separator, and condenser, wherein, the import of described beans pyrolysis oven and standby coal system outlet, the outlet of lump coal decomposing system is connected, beans forms beans pyrolysis oil gas and half breeze through beans pyrolysis oven, wherein, beans pyrolysis oil gas is separated into half breeze and de-dirt oil gas through separator, de-dirt oil gas obtains pyrolysis coal gas through condenser condenses, recovery waste heat, and pyrolytic tar, wherein, half breeze that the semicoke grain that beans decomposing furnace produces and separator are separated is merged into semicoke as gasification semicoke and generating semicoke.
Described raw gas treatment system comprises converter unit, acid gas removal body device, and sulfur recovery unit, and wherein, the entrance of converter unit is connected with the pyrolysis gas exit of condenser; Described condenser pyrolysis coal gas is out divided into two-way, one road enters into converter unit and forms conversion coal gas, one tunnel is that bypass coal gas is mixed to form mixed gas and enters in acid gas removal body device with conversion coal gas, after acid gas removal body device is processed, obtain carbonic acid gas and depickling coal gas, depickling coal gas is purified coal gas after sulfur recovery unit is processed.
Described chemical synthesis system comprises methyl alcohol-naphtha reforming device, oxidation unit, ethylene glycol synthesizer, and PET synthesizer; The import of ethylene glycol synthesizer is connected for the synthesis of MEG with dehydrogenation gas exit with the hydrogen of hydrogen recovery system, the import of described methyl alcohol-naphtha reforming device is connected for generation of PX with the purification gas exit of raw gas treatment system and the outlet of the petroleum naphtha of hydrofining system respectively, the outlet of described methyl alcohol-naphtha reforming device is connected with the entrance of oxidation unit, and the entrance of described PET synthesizer is connected with the outlet of ethylene glycol synthesizer with the outlet of oxidation unit respectively.
Described system further includes power generation system, described power generation system comprises combustion gas steam turbine, waste heat boiler, pulverized coal boiler, and steam turbine, the import of described combustion gas steam turbine is connected with the dehydrogenation gas exit of hydrogen recovery system, the outlet of described combustion gas steam turbine is connected with the import of waste heat boiler, the import of described waste heat boiler is connected with the waste heat recovery outlet of beans pyrolysis system, the outlet of described waste heat boiler is connected with the entrance of steam turbine with the outlet of pulverized coal boiler, and the import of described pulverized coal boiler is connected with the semicoke outlet of beans pyrolysis system.
A kind of co-production based on said system, feed coal is divided into lump coal and beans through standby coal measures system, the gasification gas that lump coal produces take gasification system is as thermal barrier, in lump coal pyrolysis system, there is pyrolytic reaction, generate lump coal pyrolysis oil gas and lump coke, the lump coal pyrolysis oil gas that beans pyrolysis system produces take lump coal pyrolysis system is as thermal barrier, there is pyrolytic reaction, obtain pyrolysis coal gas, pyrolytic tar and semicoke, wherein, pyrolysis coal gas enters raw gas treatment system and is further processed, pyrolytic tar is as hydrogenation upgrading, semicoke is as semicoke and gasification semicoke for generating, described pyrolysis coal gas is in raw gas treatment system, through transforming, depickling, desulfurization obtains sulphur, carbonic acid gas, purify coal gas and recovery waste heat, wherein, sulphur is directly exported as product, carbonic acid gas enters into carbonic acid gas and gets for coal-bed gas system displacement coal seam gas, described recovery waste heat is sent in power generation system, purify coal gas as Sweet natural gas synthetic gas, synthetic gas used for Fischer-Tropsch synthesis, synthetic gas and hydrogen manufacturing coal gas for alkylation.
Purification coal gas as hydrogen manufacturing coal gas is isolated to hydrogen and dehydrogenation coal gas in hydrogen recovery system, wherein, part hydrogen is directly exported, part hydrogen is sent in hydrofining oil system with hydrogen as oil product upgrading, a part is sent in chemical synthesis system and is prepared MEG, a part for dehydrogenation coal gas is generated electricity as fuel used to generate electricity, and another part is sent into synthetic MEG in chemical synthesis system; The oil product upgrading that the pyrolytic tar that described beans pyrolysis system produces and hydrogen recovery system produce is carried out oil product upgrading with hydrogen at hydrofining oil system, obtains hydrogenation processed oil and petroleum naphtha, and wherein, petroleum naphtha is sent in chemical synthesis system H.
Compared with prior art, the comprehensive coal sub-prime of the present invention utilizes the system and method for Poly-generation at least to have the following advantages:
1. adaptability to raw materials is strong: in the present invention using wholegrain footpath coal as raw material.
2. heat self-balancing: adopt in the present invention gasification gas and the pyrolysis coal gas thermal barrier as pyrolytic process, can realize the heat balance in embodiment.
3. gas self-purification function: the effect that takes into account granular-bed separator at lump coal pyrolysis oven of the present invention can be played to gasification gas and pyrolysis coal gas the effect of dedusting, effectively improves the high temperature gas-solid separation problem of pulverized coal pyrolysis.
Accompanying drawing explanation
Fig. 1 is integrated artistic system schematic of the present invention;
Fig. 2 is the process for refining composition schematic diagram of Fig. 1.
In Fig. 1, A is standby coal measures system, and B is lump coal pyrolysis system, and C is beans pyrolysis system, D is raw gas treatment system, and E is synthetic natural gas system, and F is Fischer-Tropsch synthesis system, and G is carbonic acid gas displacement coal-bed gas system, H is chemical synthesis system, and I is hydrofining oil system, and J is H
2recovery system, K is power generation system, L is calcium carbide industrial system, M is gasification system, 101 is feed coal, 107 is lump coal pyrolysis oil gas, 110 is pyrolysis coal gas, 112 is lump coke, 113 is metallurgical coke, 114 is carbonic acid gas, 116 is recovery waste heat, 117 is pyrolytic tar, 118 is semicoke, 119 is gasification semicoke, 120 is generating semicoke, 121 is gasification gas, 123 for calcium carbide is with burnt, 124 is air, 126 is sulphur, 127 is hydrogen manufacturing coal gas, 130 is alkylation synthetic gas, 131 is synthetic gas used for Fischer-Tropsch synthesis, 132 is preparing natural gas synthetic gas, 133 is hydrogen, 134 is product hydrogen, 135 is dehydrogenation coal gas, 136 is oil product upgrading hydrogen, 143 is lime, 148 is product acetylene, 149 is formaldehyde, 151 is product B DO, 153 is that outer transmission of electricity can, 154 is product P BT, 155 is hydrogenation processed oil, 156 is petroleum naphtha, 159 is product P X, 160 is PBT PTA processed, 161 is PTA, 162 is product P TA, 164 is product P ET, 166 is Fischer-Tropsch processed oil, 168 is product methane, 173 is coal for power generation gas, 174 is MEG coal gas processed, 175 is MEG hydrogen processed, 176 is product ethylene glycol, 178 is generating carbonic acid gas, 179 is beans, 180 is lump coal, 181 is methane in coal seam, 184 for purifying coal gas.
In Fig. 2, A is standby coal measures system, and B is lump coal pyrolysis system, and C is beans pyrolysis system, D is raw gas treatment system, and E is synthetic natural gas system, and F is Fischer-Tropsch synthesis system, and G is carbonic acid gas displacement coal-bed gas system, H is chemical synthesis system, and I is hydrofining oil system, and J is H
2recovery system, K is power generation system, L is calcium carbide industrial system, M is gasification system, 1 is cleaning unit, 2 is type coal equipment, 3 is air separation plant, 4 is vapourizing furnace, 5 is beans pyrolysis oven, 6 is lump coal pyrolysis oven, 7 is separator, 8 is condenser, 9 is converter unit, 10 is acid gas removal device, 11 is sulfur recovery unit, 12 is pressure-swing absorber, 13 is hydrofining reactor, 14 is knockout tower, 15 is synthesis of natural device of air, 16 is methyl alcohol-naphtha reforming device, 17 is rectifying tower, 18 is combustion gas steam turbine, 19 is waste heat boiler, 20 is pulverized coal boiler, 21 is steam turbine, 22 is furnace of calcium carbide, 23 is cooling tower, 24 is carbide-feed generator, 25 is Fischer-Tropsch synthetic tower, 26 is water-and-oil separator, 27 is PET synthesizer, 28 is oxidation unit, 29 is peace and quiet tower, 30 is BDO synthesizer, 31 is PBT synthetic tower, 32 is carbonic acid gas displacement coal-bed gas unit, 33 is ethylene glycol synthesizer, 101 is feed coal, 102 is raw material beans, 103 is raw material lump coal, 104 is raw material fine coal, 105 is moulding beans, 106 is moulding lump coal, 107 is lump coal pyrolysis oil gas, 108 is beans pyrolysis oil gas, 109 is de-dirt oil gas, 110 is pyrolysis coal gas, 111 is mixed gas, 112 is lump coke, 113 is metallurgical coke, 114 is carbonic acid gas, 115 is depickling coal gas, 116 is recovery waste heat, 117 is pyrolytic tar, 118 is semicoke, 119 is gasification semicoke, 120 is generating semicoke, 121 is gasification gas, 122 is oxygen, 123 for calcium carbide is with burnt, 124 is air, 125 is nitrogen, 126 is sulphur, 127 is hydrogen manufacturing coal gas, 128 is ethylene glycol, 129 is PET spent glycol processed, 130 is alkylation synthetic gas, 131 is synthetic gas used for Fischer-Tropsch synthesis, 132 is preparing natural gas synthetic gas, 133 is hydrogen, 134 is product hydrogen, 135 is dehydrogenation coal gas, 136 is oil product upgrading hydrogen, 137 is hydrogenation synthetic oil, 138 for purifying back end hydrogenation synthetic oil, 139 is combustion gas flue gas, 140 is superheated vapour, 141 is coal-fired superheated vapour, 142 is calcium carbide, 143 is lime, 144 is cooling calcium carbide, 145 is acetylene, 146 for purifying acetylene, 147 is BDO acetylene processed, 148 is product acetylene, 149 is formaldehyde, 150 is PBT BDO processed, 151 is product B DO, 152 is BDO, 153 is that outer transmission of electricity can, 154 is product P BT, 155 is hydrogenation processed oil, 156 is petroleum naphtha, 157 is PX, 158 is PTA PX processed, 159 is product P X, 160 is PBT PTA processed, 161 is PTA, 162 product P TA, 163 PET PTA processed, 164 is product P ET, 165 is Fischer-Tropsch synthesis oil, 166 is Fischer-Tropsch processed oil, 167 is combustion gas electric energy, 168 is product methane, 169 is half breeze, 170 is bypass coal gas, 171 is conversion coal gas, 172 is coal gas after conversion, 173 is coal for power generation gas, 174 is MEG coal gas processed, 175 is MEG hydrogen processed, 176 is product ethylene glycol, 177 is steam electric energy, 178 is generating carbonic acid gas, 179 is beans, 180 is lump coal, 181 is methane in coal seam, 182 purify coal gas for combustion gas carbonic acid gas 183 for coal-fired carbonic acid gas 184.
Embodiment
Entire system of the present invention forms structure as shown in Figure 1:
Standby coal measures system A, take feed coal 101 as raw material, is provided with 180 two outlets of beans 179 and lump coal, and lump coal 180 outlets are connected with the material inlet of lump coal pyrolysis system B, and beans 179 outlets are connected with the material inlet of beans pyrolysis system C.
The thermal barrier of lump coal pyrolysis system B is provided by the gasification gas 121 producing in gasification system M, lump coal pyrolysis system B is provided with 107 outlets of lump coal pyrolysis oil gas and lump coke 112 exports, 107 outlets of lump coal pyrolysis oil gas are connected with the thermal barrier import of beans pyrolysis system C, lump coke 112 outlets of lump coal pyrolysis system B are divided into two-way, directly export as metallurgical coke 113 on one tunnel, and a road is connected with the carbide raw material import processed of calcium carbide industrial system L with burnt 123 branch roads as calcium carbide.
Beans pyrolysis system C is provided with that pyrolysis coal gas 110 exports, pyrolytic tar 117 exports and semicoke 118 exports, semicoke 118 outlets are divided into generating semicoke 120 and gasification semicoke 119 two-way, be connected with gasification system M material inlet with power generation system K material inlet respectively, pyrolytic tar 117 outlets of beans pyrolysis system C are connected with hydrofining oil system I import, and 110 outlets of pyrolysis coal gas are connected with raw gas treatment system D import.
Raw gas treatment system D is provided with that sulphur 126 exports, carbonic acid gas 114 exports, recovery waste heat 116 exports and purifies coal gas 184 and exports, sulphur 126 is directly exported as product, recovery waste heat 116 is inputted in power generation system K, carbonic acid gas 114 outlet is connected with carbonic acid gas displacement coal-bed gas system G carbon dioxide inlet, through the purification coal gas 184 of raw gas treatment system D depickling desulfurization export be divided into four tunnels respectively with synthetic natural gas system E, Fischer-Tropsch synthesis system F, chemical synthesis system H and H
2the synthetic gas import of recovery system J is connected.
Preparing natural gas synthetic gas 132 branch roads that the purification coal gas 184 of raw gas treatment system D exports are connected with the import of synthetic natural gas E, and synthetic natural gas system E is provided with methane 168 and exports; Synthetic gas used for Fischer-Tropsch synthesis 131 branch roads that the purification coal gas 184 of raw gas treatment system D exports are connected with the import of Fischer-Tropsch synthesis system F, and Fischer-Tropsch synthesis system F is provided with Fischer-Tropsch synthesis oil 166 and exports.
Hydrogen manufacturing coal gas 127 branch roads and H that the purification coal gas 184 of raw gas treatment system D exports
2the import of recovery system J is connected, H
2recovery system J is provided with hydrogen 133 outlets and dehydrogenation coal gas 135 exports, H
2133 outlets are divided into three tunnels, and a road is that oil product upgrading hydrogen 136 branch roads are connected with the import of hydrofining oil system I hydrogen source, and a road is that MEG processed hydrogen 175 is connected with the hydrogen source import of the MEG processed of chemical synthesis system H, and a road is product H
2134 directly outputs, H
2 dehydrogenation coal gas 135 outlets of recovery system J are divided into two-way, and a road is that coal for power generation gas 173 branch roads are connected with the fuel gas inlet of power generation system, and another portion is that MEG processed coal gas 174 branch roads are connected with the carbon source import of the MEG processed of chemical synthesis system H.
Alkylation synthetic gas 130 branch roads that the purification coal gas 184 of raw gas treatment system D exports are connected with the import of chemical synthesis system H, chemical synthesis system H is provided with product P X159 outlet, product P ET164 outlet, PTA161 outlet and product MEG176 outlet, wherein PTA161 outlet is provided with two branch roads, one tunnel is product P TA162 output branch road, and a road is that PBT processed PTA160 branch road is connected with the PBT material inlet processed of calcium carbide industrial system L; Hydrofining oil system I is provided with 155 outlets of hydrogenation processed oil and petroleum naphtha 156 exports, and petroleum naphtha 156 outlets are connected with the import of chemical synthesis system H petroleum naphtha; Calcium carbide industrial system L is provided with that product acetylene 148 exports, product B DO151 outlet and product P BT154 outlet.
Power generation system K is provided with outer transmission of electricity energy 153 and generating carbonic acid gas 178 exports, and 178 outlets of generating carbonic acid gas are connected with the import of carbonic acid gas displacement coal-bed gas system G; Carbonic acid gas displacement coal-bed gas system G is provided with methane 181 in coal seam and exports.
The concrete technology route of scheme shown in Fig. 1 is as described below:
Feed coal 101 is sent in standby coal measures system A and through screening and processing, the beans of (6-20mm) 179 and lump coal 180 (>20mm) is sent into respectively in beans pyrolysis system C and lump coal pyrolysis system B;
In beans pyrolysis system C, the lump coal pyrolysis oil gas 107 providing take lump coal pyrolysis system B is as thermal barrier, in the time of 500-800 ℃, there is pyrolytic reaction in beans 179, through pyrolysis and separating technology, obtain pyrolysis coal gas 110, pyrolytic tar 117 and semicoke 118, pyrolysis coal gas 110(V/V%, CO47.14%, H
234.35%, CO
217.6%, CH
40.117%, Deng) send into and in raw gas treatment system D, carry out subsequent disposal, pyrolytic tar 117 is sent in hydrofining oil system I and is carried out hydrogenation upgrading, semicoke 118 is divided into two portions, a part is sent in power generation system K with semicoke 120 as generating, and another part is sent in gasification system M with semicoke 119 as gasification;
In gasification system M, the semicoke 119 gasification gas 121(V/V% that generating gasification reaction generates under the hot conditions of 1300 ℃ for gasification, H
221.90%, CH
439.91%, CO19.89%, CO
213.71%, etc.) pass in lump coal pyrolysis system B as lump coal pyrolysis thermal barrier;
Pyrolysis coal gas 110 is in raw gas treatment system D, through steps such as conversion, depickling, desulfurization, obtain sulphur 126, carbonic acid gas 114, purify coal gas 184 and recovery waste heat 116, sulphur 126 is directly exported as product, carbonic acid gas 114 is sent in carbonic acid gas displacement coal-bed gas system G gas in displacement coal seam, recovery waste heat 116 is sent in power generation system K, purifies 184 of coal gas and is divided into synthetic gas 132 for preparing natural gas, synthetic gas used for Fischer-Tropsch synthesis 131, alkylation synthetic gas 130 and hydrogen manufacturing coal gas 127 4 parts;
Preparing natural gas synthetic gas 132 is sent into and in synthetic natural gas system E, is converted into methane and discharges; Synthetic gas 131 used for Fischer-Tropsch synthesis is sent in Fischer-Tropsch synthesis system F and is made product Fischer-Tropsch synthesis oil 166 through processes such as synthetic, purification, separation;
Hydrogen manufacturing coal gas 127 is sent into H
2in recovery system J, separate and obtain hydrogen 133 and dehydrogenation coal gas 135, hydrogen 133 is divided into three parts, a part is directly exported as product hydrogen 134, a part is sent in hydrofining oil system I with hydrogen 136 as oil product upgrading, a part is sent in chemical synthesis system H with hydrogen 175 as MEG processed, dehydrogenation coal gas 135 is divided into two portions, and a part is sent in power generation system K as coal for power generation gas 173, and another part is sent in chemical synthesis system H with coal gas 174 as MEG processed;
In chemical synthesis system H, MEG processed makes MEG with hydrogen 175 and MEG processed coal gas 174, alkylation makes PX with synthetic gas 130 and petroleum naphtha 156, PX obtains PTA through peroxidation, PTA and MEG make PET, and PTA161 is two portions respectively, directly export for one for product P TA162, another part PBT processed sends in calcium carbide industrial system L with PTA160, and remaining product P X159, product P ET164, product MEG176 directly export;
In calcium carbide industrial system L, take calcium carbide with burnt 123 and lime 143 prepare calcium carbide, take calcium carbide as raw material, prepare acetylene as raw material, acetylene and the synthetic BDO of formaldehyde 149, BDO and PBT processed obtain PBT with PTA160 reaction, can obtain product acetylene 148, product B DO151 and product P BT154 and supply outward;
Carbonic acid gas 114 and generating carbonic acid gas 178 in carbonic acid gas displacement coal-bed gas system G in displacement coal output layer gas obtain coal seam in methane 181, the methane obtaining with synthetic natural gas system E is together as the outer confession of product methane 168.
Below in conjunction with Fig. 2, Fig. 1 of the present invention is carried out to refinement description, dotted line frame has been divided the concrete equipment in each system, and the present invention is described in further detail:
In accompanying drawing 2, the concrete composition structural relation of each system is as described below:
Standby coal measures system A comprises cleaning unit 01 and type coal equipment 02; Lump coal pyrolysis system B comprises lump coal pyrolysis oven 06; Beans pyrolysis system C is comprised of beans pyrolysis oven 05, separator 07 and condenser 08; Raw gas treatment system D is comprised of converter unit 09, acid gas removal device 10 and sulfur recovery unit 11; Synthetic natural gas system E consists of synthesis of natural device of air 15; Fischer-Tropsch synthesis system F comprises Fischer-Tropsch synthetic tower 25 and water-and-oil separator 26; Carbonic acid gas displacement coal-bed gas system G is comprised of carbonic acid gas displacement coal-bed gas unit 32, and chemical synthesis system H comprises methyl alcohol-naphtha reforming device 16, oxidation unit 28, ethylene glycol synthesis device 33 and PET synthesizer 27; Hydrofining oil system I is comprised of hydrofining reactor 13, knockout tower 14 and rectifying tower 17; H
2recovery system J is comprised of transformation system tower 12; Power generation system K is comprised of combustion gas steam turbine 18, waste heat boiler 19, pulverized coal boiler 20, steam turbine 21; Calcium carbide industrial system L comprises furnace of calcium carbide 22, cooling tower 23, carbide-feed generator 24, peace and quiet tower 29, BDO synthesizer 30 and PBT synthetic tower 31; Gasification system M is comprised of air separation plant 03 and vapourizing furnace 04.
Below the annexation between each devices in system in Fig. 2 is described in further detail.
For coal measures system, A comprises cleaning unit 01 and exports with cleaning unit 01 fine coal the type coal equipment 02 being connected, and cleaning unit 01 and type coal equipment 02 are equipped with beans outlet and lump coal outlet.
Lump coal pyrolysis system B comprises: export with the standby coal measures system cleaning unit 01 of A and the lump coal of type coal equipment 02 the lump coal pyrolysis oven 06 being connected, the thermal barrier import of lump coal pyrolysis oven 06 is connected with the gasification gas outlet of vapourizing furnace 04 in gasification system M, lump coal pyrolysis oven 06 is provided with lump coal pyrolysis oil gas vent and lump coke outlet, lump coke outlet is divided into two-way, one tunnel is that metallurgical coke is directly exported, and a road is the burnt branch road of calcium carbide.
Beans pyrolysis system C comprises that material inlet is connected with the standby coal measures system cleaning unit 01 of A and the outlet of the beans of type coal equipment 02, the beans pyrolysis oven 05 that thermal barrier import is connected with the lump coal pyrolysis oil gas vent of lump coal pyrolysis system B, beans pyrolysis oven 05 is provided with beans pyrolysis oil gas vent and the outlet of semicoke grain, its chews pyrolysis oil gas outlet is connected with separator 07 gas inlet, separator 07 is provided with half breeze outlet and takes off dirt oil gas vent, de-dirt oil gas vent is connected with the import of condensing tower 08, condensing tower 08 offers pyrolysis gas exit, recovery waste heat outlet and pyrolytic tar outlet, half breeze outlet of the semicoke grain outlet of beans pyrolysis oven 05 and separator 07 is merged into semicoke and is further divided into gasification semicoke and generating semicoke two-way.
Raw gas treatment system D comprises the converter unit 09 being connected with the conversion gas pipe branch road of the pyrolysis gas exit of beans pyrolysis system C condensing tower 08 and the acid gas removal device 10 being connected with the mixed mixed gas pipeline of another branch road bypass coal gas of pyrolysis gas exit of coal gas after converter unit 09 conversion and beans pyrolysis system C condensing tower 08, acid gas removal device 10 is provided with carbonic acid gas outlet and depickling gas exit, depickling gas exit is connected with sulfur recovery unit 11, sulfur recovery unit 11 is provided with sulphur outlet and purifies gas exit, purify gas exit and be divided into four branch roads, be respectively hydrogen manufacturing coal gas branch road, alkylation synthetic gas branch road, synthetic gas branch road used for Fischer-Tropsch synthesis and preparing natural gas synthetic gas branch road.
Synthetic natural gas system E is the synthesis of natural device of air 15 being connected with the preparing natural gas synthetic gas branch road of sulfur recovery unit 11 in raw gas treatment system D, and synthesis of natural device of air 15 is provided with methane outlet.
Fischer-Tropsch synthesis system F comprises the Fischer-Tropsch synthetic tower 25 being connected with the synthetic gas branch road used for Fischer-Tropsch synthesis of sulfur recovery unit 11 in raw gas treatment system D and exports with Fischer-Tropsch synthetic tower 25 Fischer-Tropsch synthesis oils the water-and-oil separator 26 being connected, and water-and-oil separator 26 is provided with Fischer-Tropsch export of finished oil.
Carbonic acid gas displacement coal gas gas train G exports and exports with the generating carbonic acid gas of power generation system K the carbonic acid gas displacement coal-bed gas unit 32 being connected with the carbonic acid gas of acid gas removal device 10 in raw gas treatment system D, and carbonic acid gas displacement coal-bed gas unit 32 is provided with methane outlet in coal seam.
Chemical synthesis system H comprises with the alkylation synthetic gas branch road of sulfur recovery unit 11 in raw gas treatment system D and with 17 petroleum naphthas of rectifying tower in hydrofining oil system I and exports the methyl alcohol-naphtha reforming device 16 and the ethylene glycol synthesizer 33 that are connected, hydrogen source import and the H of ethylene glycol synthesizer 33
2in recovery system J, the MEG processed of pressure-swing absorber 12 hydrogen outlets is connected with hydrogen branch road, carbon source import and the H of ethylene glycol synthesizer 33
2in recovery system J, the MEG processed of pressure-swing absorber 12 dehydrogenation gas exits is connected with coal gas branch road, and ethylene glycol synthesizer 33 is provided with ethylene glycol outlet, ethylene glycol outlet is divided into two-way, one tunnel is that product ethylene glycol is directly exported, one tunnel is PET spent glycol branch road processed, the PX outlet of methyl alcohol-naphtha reforming device 16 is divided into two-way, one branch road is output products PX pipeline, another branch road is connected with oxidation unit 28 with PX pipeline for PTA processed, oxidation unit 28 is provided with PTA outlet, PTA outlet is divided into three tunnels, the one direct output products PTA in tunnel, one tunnel is that PBT processed PTA branch road is connected with the PBT synthetic tower 31 in calcium carbide industrial system K, one tunnel is connected with PET synthesizer 27 with PTA branch road for PET processed, PET synthesizer 27 is provided with PET outlet.
Hydrofining oil system I comprises with the 08 pyrolytic tar outlet of condensing tower in beans pyrolysis system C and being connected, and and H
2the hydrofining reactor 13 that in recovery system J, the oil product upgrading of pressure-swing absorber 12 hydrogen outlets is connected with hydrogen branch road, the hydrogenation synthetic oil outlet of hydrofining reactor 13 is connected with knockout tower 14 imports, the purification back end hydrogenation synthetic oil outlet of knockout tower 14 is connected with rectifying tower 17 imports, and rectifying tower 17 is provided with the petroleum naphtha outlet at top and the hydrogenation export of finished oil of bottom.
H
2recovery system J is the pressure-swing absorber 12 being connected with the hydrogen manufacturing gas exit of sulfur recovery unit 11 in raw gas treatment system D, pressure-swing absorber 12 is provided with hydrogen outlet and dehydrogenation gas exit, hydrogen outlet is divided into three tunnels, one tunnel is the direct output channel of product hydrogen, one tunnel is oil product upgrading hydrogen branch road, and a road is MEG processed hydrogen branch road, and dehydrogenation gas exit is divided into two-way, one tunnel is coal for power generation gas branch road, and another road is MEG processed hydrogen branch road.
Power generation system K comprises and H
2the combustion gas steam turbine 18 that in recovery system J, the coal for power generation gas branch road of the dehydrogenation gas exit of pressure-swing absorber 12 is connected and the pulverized coal boiler 20 being connected with semicoke with the generating of beans pyrolysis system C, combustion gas steam turbine 18 is provided with the outlet of combustion gas carbonic acid gas, the outlet of combustion gas electric energy and combustion gas exhanst gas outlet, combustion gas exhanst gas outlet is connected with waste heat boiler 19, and waste heat boiler 19 is connected with the recovery waste heat outlet of the condensing tower 08 in beans pyrolysis system C, the coal-fired superheated vapour outlet of the superheated vapour outlet of waste heat boiler 19 and pulverized coal boiler 20 is connected with steam turbine 21, steam turbine 21 is provided with the outlet of steam electric energy.
Calcium carbide industrial system L comprises the PBT synthetic tower 31 that the furnace of calcium carbide 22 being connected with burnt branch road with the calcium carbide of the lump coke outlet of lump coal pyrolysis system B medium-sized coal pyrolysis oven 06 and the PBT processed PTA branch road exporting with the PTA of oxidation unit 28 in chemical synthesis system H are connected, the calcium carbide outlet of furnace of calcium carbide 22 is connected with the import of cooling tower 23, the cooling calcium carbide outlet of cooling tower 23 is connected with the import of carbide-feed generator 24, the acetylene outlet of carbide-feed generator 24 is connected with the import of peace and quiet tower 29, the purification acetylene outlet of peace and quiet tower 29 is divided into two-way, one tunnel is that product acetylene is directly exported, one tunnel is BDO processed acetylene branch road, BDO processed is connected with BDO synthesizer 30 with acetylene branch road, BDO synthesizer 30 is provided with BDO outlet, BDO outlet is divided into two-way, one tunnel is that product B DO directly exports, another road is PBT processed BDO branch road, PBT processed is connected with PBT synthetic tower 31 with BDO branch road, PBT synthetic tower 31 is provided with PBT outlet.
The vapourizing furnace 04 that gasification system M comprises air separation plant 03 and is connected with air separation plant 03 oxygen outlet, and the material inlet of vapourizing furnace 04 is connected with semicoke branch road with the gasification that semicoke grain in beans pyrolysis system C and half breeze merge semicoke outlet, and vapourizing furnace 04 is provided with gasification gas and exports.
Describe the concrete technology route of scheme shown in Fig. 2 below in detail:
Feed coal 101 can sieve as raw material fine coal 104(0-6mm through cleaning unit 01), raw material beans 102(6-20mm) and raw material lump coal 103(>20mm), raw material fine coal 104 is sent into the moulding beans 105 that in type coal equipment 02, reshaping is (6-20mm) and is greater than the moulding lump coal 106 of 20mm, moulding beans 105 and raw material beans 102 are merged into beans 179 and are sent into beans pyrolysis oven 05 and at 500-800 ℃, carry out pyrolysis, moulding lump coal 106 and raw material lump coal 103 are merged into lump coal 180 and are sent into lump coal pyrolysis oven 06 and at 500-800 ℃, carry out lump coal pyrolysis.
Beans pyrolysis oven 05 is produced beans pyrolysis oil gas 108 and semicoke grain, pyrolysis of coal oil gas 108 passes into separator 07 and obtains de-dirt oil gas 109 and half breeze 169, after being mixed into semicoke 118, half breeze 169 and semicoke grain be divided into two portions, a part is sent into oxygen 122 1 that vapourizing furnace 04 makes with air separation plant 03 generating gasification under the hot conditions of 1300 ℃ that coexists in vapourizing furnace 04 for gasification with semicoke 119 and is reacted generation gasification gas 121(V/V%, H221.90%, CH439.91%, CO19.89%, CO213.71%, Deng), and pass in lump coal pyrolysis oven 06 with the form of thermal barrier, another part semicoke is sent in pulverized coal boiler 20 as fuel with semicoke 120 as generating, the de-dirt oil gas 109 obtaining in separator 07 passes into condenser 08 and obtains pyrolysis coal gas 110(V/V%, CO47.14%, H234.35%, CO217.6%, CH40.117%, Deng), pyrolytic tar 117 and recovery waste heat 116, and pyrolytic tar 117 is passed into and in hydrofining reactor 13, carries out hydrogenation upgrading, recovery waste heat 116 passes in waste heat boiler 19 as generating thermal source,
Lump coal pyrolytic reaction in lump coal pyrolysis oven 06 generates lump coal pyrolysis oil gas 107 and lump coke 112, lump coal pyrolysis oil gas 107 passes in beans pyrolysis oven 05 as thermal barrier, lump coke 112 parts are as the outer confession of metallurgical coke 113, and a part is sent into furnace of calcium carbide 22 with Jiao 123 for calcium carbide;
It is bypass coal gas 170 that pyrolysis coal gas 110 is divided into two-way one tunnel, another road is conversion coal gas 171, conversion coal gas 171 passes into change unit 09 and is converted into the rear coal gas 172 of conversion, and be mixed into mixed gas 111 with bypass coal gas 170, mixed gas 111 is isolated carbonic acid gas 114 more successively in acid gas removal device 10, in sulfur recovery unit 11, isolate sulphur 126 and be purified coal gas 184, carbonic acid gas 114 and generating carbonic acid gas 178 all pass in carbonic acid gas displacement coal-bed gas unit 32 and obtain methane 181 in coal seam, and sulphur 126 is directly exported as product;
Purify coal gas 184 and according to different purposes, be divided into four tunnels, hydrogen manufacturing coal gas 127, synthetic gas 130, synthetic gas used for Fischer-Tropsch synthesis 131 and synthetic gas 132 for preparing natural gas for alkylation;
Hydrogen manufacturing coal gas 127 passes into pressure-swing absorber 12 and makes hydrogen 133 and dehydrogenation coal gas 135, hydrogen 133 is divided into three tunnels, part hydrogen passes into ethylene glycol synthesizer 33 as hydrogen source as MEG processed with hydrogen 175, a part is exported external application as product hydrogen 134, another part hydrogen passes into hydrofining reactor 13 and pyrolytic tar 117 as oil product upgrading with hydrogen 136 and hydrogenation reaction occurs makes hydrogenation synthetic oil 137 and pass into successively knockout tower 14 and rectifying tower 17 makes petroleum naphtha 156 and hydrogenation processed oil 155, petroleum naphtha 156 passes into methyl alcohol-naphtha reforming device 16 and carries out reforming reaction, the dehydrogenation coal gas 135 that pressure-swing absorber 12 is discharged is divided into two portions, a part passes into combustion gas steam turbine 18 production combustion gas electric energy 167 as coal for power generation gas 173, another part passes into ethylene glycol synthesizer 33 and the synthetic ethylene glycol 128 that makes of MEG processed hydrogen 175 as MEG processed with coal gas 174, ethylene glycol 128 parts are directly exported as product ethylene glycol 176, and another part is sent in PET synthesizer 27 with MEG129 as PET processed,
Alkylation passes into methyl alcohol-naphtha reforming device 16 with synthetic gas 130 and reacts and generate p-Xylol (PX) 157 with petroleum naphtha 156, PX is divided into two portions, a part supplies outward as product P X159, another part is that PTA processed PX158 is oxidized to obtain terephthalic acid (PTA) 161 through oxidation unit 28, PTA downstream is divided into three approach, one is directly exported as product P TA162, it two passes in PBT synthetic tower 31 with PTA160 as PBT processed, its three as PET processed with PTA163 pass into PET synthesizer 27 and with the synthetic product P ET164 that makes of PET processed MEG129,
Synthetic gas 131 used for Fischer-Tropsch synthesis passes into Fischer-Tropsch synthetic tower 25 and makes Fischer-Tropsch synthesis oil 165 and obtain Fischer-Tropsch processed oil 166 through water-and-oil separator 26; Preparing natural gas with synthetic gas 132 pass into synthesis of natural device of air 15 synthesizing methane gases and with the coal seam of carbonic acid gas displacement gained in methane 181 as product methane 168, export in the lump;
The calcium carbide Jiao 123 and the outer calcium carbide of producing in furnace of calcium carbide 22 for lime 143 142 that pass into furnace of calcium carbide 22 also pass into cooling tower 23 successively, carbide-feed generator 24 and peace and quiet tower 29 are purified acetylene 146, part acetylene is exported as product acetylene 148, another part as BDO processed, with acetylene 147, pass into BDO synthesizer 30 and pass into formaldehyde 149 synthetic 1, 4-butyleneglycol (BDO) 152, and BDO is divided into two-way, part product B DO151 supplies outward, a part passes into PBT synthetic tower 31 as synthetic PBT with BDO150, with PTA, synthesize to obtain product polybutylene terephthalate (PBT) 154 with PBT processed,
Coal for power generation gas 173 passes into combustion gas steam turbine 18 production combustion gas electric energy 167, and discharge combustion gas flue gas 139, combustion gas flue gas 139 passes into waste heat boiler 19 and produces superheated vapour 140 and pass into steam turbine 21 together with the recovery waste heat 116 obtaining in condensing tower 08, generating is burnt in pulverized coal boiler 20 with semicoke 120 and is obtained coal-fired superheated vapour 141 and also pass into steam turbine 21, steam turbine 21 produces steam electric energy 177 under superheated vapour 140 and the common effect of coal-fired superheated vapour 141, steam electric energy 177 and heating power electric energy 167 are grid-connected as outer transmission of electricity energy 153 outputs, the coal-fired carbonic acid gas 183 producing in the combustion gas carbonic acid gas 182 producing in combustion gas steam turbine 18 and pulverized coal boiler 20 is merged into generating carbonic acid gas 178 and is passed into carbonic acid gas displacement coal-bed gas unit 32.
The foregoing is only one embodiment of the present invention, it not whole or unique embodiment, the conversion of any equivalence that those of ordinary skills take technical solution of the present invention by reading specification sheets of the present invention, is claim of the present invention and contains.
Claims (10)
1. comprehensive coal sub-prime is utilized a system for Poly-generation, it is characterized in that: comprise standby coal measures system (A), lump coal pyrolysis system (B), beans pyrolysis system (C), raw gas treatment system (D), and gasification system (M); Wherein, the outlet of standby coal measures system is connected with beans pyrolysis system (C) with lump coal pyrolysis system (B) respectively; Gasification system is take air as input, and the semicoke producing take beans pyrolysis system (C) is as raw material, and the gasification gas of generation is as the thermal barrier of lump coal pyrolysis system (B); The lump coal pyrolysis oil gas that lump coal pyrolysis system (B) produces is as the thermal barrier of beans pyrolysis system, and a lump coke part for generation is exported as metallurgical coke, and a part of lump coke is as the raw material of calcium carbide processed in addition; The pyrolysis coal gas that beans pyrolysis system (C) produces enters raw gas treatment system and does further processing, and the pyrolytic tar of generation is for hydrogenation upgrading, and the semicoke of generation is respectively as semicoke and gasification semicoke for generating; The pyrolysis coal gas that raw gas treatment system (D) produces take beans pyrolysis system (C) is as raw material, the sulphur of its generation is as output of products, the recovery waste heat producing is for the waste heat boiler of power generation system, the carbonic acid gas producing enters carbonic acid gas displacement coal gas gas train (G), and the purification coal gas of generation is respectively as synthetic gas, synthetic gas used for Fischer-Tropsch synthesis, synthetic gas and hydrogen manufacturing coal gas for alkylation for Sweet natural gas.
2. the system as claimed in claim 1, it is characterized in that: described system further comprises hydrogen recovery system (J), the purification coal gas that described hydrogen recovery system produces take raw gas treatment system (D) is as raw material, produce after treatment hydrogen and dehydrogenation coal gas, wherein, hydrogen is divided into three parts, a part is output directly, a part is sent in hydrofining oil system (I) with hydrogen as oil product upgrading, a part is sent in chemical synthesis system (H) with hydrogen as MEG processed, dehydrogenation coal gas is divided into two portions, a part is as coal for power generation gas, another part is sent in chemical synthesis system (H) with coal gas as MEG processed.
3. the system as claimed in claim 1, it is characterized in that: described system further includes hydrofining oil system (I), the hydrogen that the pyrolytic tar that this hydrofining oil system (I) produces take beans pyrolysis system (C) and hydrogen recovery system (J) produce carries out oil product upgrading as raw material, obtain hydrogenation processed oil and petroleum naphtha, wherein, described petroleum naphtha is as the raw material of chemical synthesis system.
4. system as claimed in claim 2, is characterized in that: the hydrogen that described chemical synthesis system (H) produces take hydrogen recovery system (J) and dehydrogenation coal gas are raw material generation MEG; The petroleum naphtha that the purification coal gas producing take raw gas treatment system and hydrofining oil system (I) produce is raw material generation PX, PX obtains PTA through oxidation, produces PET, wherein take PTA and MEG as raw material, PTA is as output of products for a part, and a part of PTA enters into calcium carbide industrial system in addition.
5. the system as claimed in claim 1, it is characterized in that: described beans pyrolysis system comprises beans pyrolysis oven (05), separator (07), and condenser (08), wherein, the import of described beans pyrolysis oven is connected with the outlet of lump coal pyrolysis system with the outlet of standby coal measures system, beans forms beans pyrolysis oil gas and half breeze through beans pyrolysis oven, wherein, beans pyrolysis oil gas is separated into half breeze and de-dirt oil gas through separator, de-dirt oil gas obtains pyrolysis coal gas through condenser condenses, recovery waste heat, and pyrolytic tar, wherein, half breeze that the semicoke grain that beans pyrolysis oven produces and separator are separated is merged into semicoke as gasification semicoke and generating semicoke.
6. the system as claimed in claim 1, it is characterized in that: described raw gas treatment system (D) comprises converter unit (09), acid gas removal body device (10), and sulfur recovery unit (11), wherein, the entrance of converter unit (09) is connected with the pyrolysis gas exit of condenser; Described condenser pyrolysis coal gas is out divided into two-way, one road enters into converter unit and forms conversion coal gas, one tunnel is that bypass coal gas is mixed to form mixed gas and enters in acid gas removal body device with conversion coal gas, after acid gas removal body device is processed, obtain carbonic acid gas and depickling coal gas, depickling coal gas is purified coal gas after sulfur recovery unit is processed.
7. system as claimed in claim 4, is characterized in that: described chemical synthesis system (H) comprises methyl alcohol-naphtha reforming device (16), oxidation unit (28), ethylene glycol synthesizer (33), and PET synthesizer (27); The import of ethylene glycol synthesizer is connected for the synthesis of MEG with dehydrogenation gas exit with the hydrogen of hydrogen recovery system, the import of described methyl alcohol-naphtha reforming device is connected for generation of PX with the purification gas exit of raw gas treatment system and the outlet of the petroleum naphtha of hydrofining system respectively, the outlet of described methyl alcohol-naphtha reforming device is connected with the entrance of oxidation unit, and the entrance of described PET synthesizer is connected with the outlet of ethylene glycol synthesizer with the outlet of oxidation unit respectively.
8. the system as claimed in claim 1, it is characterized in that: described system further includes power generation system, described power generation system comprises combustion gas steam turbine (18), waste heat boiler (19), pulverized coal boiler (20), and steam turbine (21), the import of described combustion gas steam turbine is connected with the dehydrogenation gas exit of hydrogen recovery system, the outlet of described combustion gas steam turbine is connected with the import of waste heat boiler, the import of described waste heat boiler is connected with the waste heat recovery outlet of beans pyrolysis system, the outlet of described waste heat boiler is connected with the entrance of steam turbine with the outlet of pulverized coal boiler, the import of described pulverized coal boiler is connected with the semicoke outlet of beans pyrolysis system.
9. the co-production based on system described in claim 1, it is characterized in that: feed coal is divided into lump coal and beans through standby coal measures system, the gasification gas that lump coal produces take gasification system is as thermal barrier, in lump coal pyrolysis system, there is pyrolytic reaction, generate lump coal pyrolysis oil gas and lump coke, the lump coal pyrolysis oil gas that beans pyrolysis system produces take lump coal pyrolysis system is as thermal barrier, there is pyrolytic reaction, obtain pyrolysis coal gas, pyrolytic tar and semicoke, wherein, pyrolysis coal gas enters raw gas treatment system and is further processed, pyrolytic tar is as hydrogenation upgrading, semicoke is as semicoke and gasification semicoke for generating, described pyrolysis coal gas is in raw gas treatment system, through transforming, depickling, desulfurization obtains sulphur, carbonic acid gas, purify coal gas and recovery waste heat, wherein, sulphur is directly exported as product, carbonic acid gas enters into carbonic acid gas and gets for coal-bed gas system displacement coal seam gas, described recovery waste heat is sent in power generation system, purify coal gas as Sweet natural gas synthetic gas, synthetic gas used for Fischer-Tropsch synthesis, synthetic gas and hydrogen manufacturing coal gas for alkylation.
10. method as claimed in claim 9, it is characterized in that: the purification coal gas as hydrogen manufacturing coal gas is isolated to hydrogen and dehydrogenation coal gas in hydrogen recovery system, wherein, part hydrogen is directly exported, part hydrogen is sent in hydrofining oil system with hydrogen as oil product upgrading, a part is sent in chemical synthesis system and is prepared MEG, and a part for dehydrogenation coal gas is generated electricity as fuel used to generate electricity, and another part is sent into synthetic MEG in chemical synthesis system; The oil product upgrading that the pyrolytic tar that described beans pyrolysis system produces and hydrogen recovery system produce is carried out oil product upgrading with hydrogen at hydrofining oil system, obtains hydrogenation processed oil and petroleum naphtha, and wherein, petroleum naphtha is sent in chemical synthesis system H.
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