CN100584924C

CN100584924C - Method of coproducing oil product, methanol and electric energy using carbon containing combustible solid as raw material

Info

Publication number: CN100584924C
Application number: CN 200610025456
Authority: CN
Inventors: 孙启文; 朱继承; 庞利峰; 张宗森; 岳建平
Original assignee: SHANGHAI YANKUANG ENERGY SOURCE SCIENCE AND TECHNOLOGY RESEARCH DEVELOPMENT Co
Current assignee: SHANGHAI YANKUANG ENERGY SOURCE SCIENCE AND TECHNOLOGY RESEARCH DEVELOPMENT Co
Priority date: 2006-04-05
Filing date: 2006-04-05
Publication date: 2010-01-27
Anticipated expiration: 2026-04-05
Also published as: CN1948436A

Abstract

This invention relates to a combined preparation of ail, methanol and electric energy with flammable carbonic solid being material. This method needs at least gasification stage, synthesis stage, end gas processing stage, deep processing of products stage and generating electricity stage. Flammable carbonic solid is used for preparing synthetic gas at gasification stage, and methanol synthesis and fischer-tropsch Synthesis are conducted with synthetic gas at synthesis stage, and at least parts of end gas from synthesis stage is processed at end gas processing stage and part of components from gas are recycled, and crude fischer-tropsch is processed into refined oil and crude methanol is processed into refined methanol, and the steam of end gas, as well as para-gas from synthesis stage is used to generate electricity.

Description

A kind of is the method for raw material coproducing oil product, methyl alcohol and electric energy with the carbon containing combustible solid

Technical field

The present invention relates to a kind of is the method for raw material coproducing oil product, methyl alcohol and electric energy with the carbon containing combustible solid.

Background technology

With carbon containing combustible solids such as coals is that the Poly-generation technology of electricity, fuel and other chemical of raw material is the important development direction of 21 century clean energy.As coal-based polygenerations systeme, promptly be that the synthetic gas of producing with gasification is a core, produce the integrated process of chemical and electric energy simultaneously.Energy part in the feed coal is converted into electric energy, and it is in the chemical of representative that a part is stored into the liquid fuel.

In the application of Poly-generation technology, except that coal, all the other carbon containing combustible solids also can be used as the source of preparation synthetic gas at present, as residual oil, waste wood, refinery coke and rubbish etc., but generally how to carry out multifuel combustion with coal.Promptly adopt coal and the gasification of municipal wastes multifuel combustion as the German black water pump works, obtain synthetic gas and be used for generating; The IGCC flow process of the Tampa power plant of the U.S. is then used coal and the gasification of refinery coke multifuel combustion to obtain synthetic gas and is generated electricity, and these factories have all obtained favorable economic benefit by the mixing gasifying of multiple carbon containing combustiblesubstance.

The disclosed general polygenerations systeme of disclosed patent and document comprises following step:

(1) gasification of carbonaceous material.Carbonaceous material at gasifying reactor and oxygen-containing gas and steam reaction to obtain synthetic gas.

(2) purification of synthetic gas.In typical gasification, synthetic gas is by available gas component H ₂, CO and small amount of impurities such as H ₂O, CO ₂, COS and H ₂Compositions such as S.Synthetic gas generally carries out purifying treatment when entering the downstream flow process, to remove or significantly to reduce wherein H ₂O, H ₂S, COS and CO ₂Deng impurity.

(3) synthetic gas is used for synthesis of chemicals.Main line of products has following several:

A. oil product is synthetic.

Fischer-Tropsch synthesis takes place in synthetic gas on fischer-tropsch synthetic catalyst.Depend on a lot of conditions by synthetic product kind and the quantity that obtains of Fischer-Tropsch, as processing condition, catalyzer etc.Commercialized running at present mainly contain four kinds of reactor patterns: tubular fixed-bed reactor, circulating fluid bed reactor, fixed fluidized-bed reactor and slurry attitude bubbling bed reactor.And fischer-tropsch synthetic catalyst generally has two kinds: cobalt-base catalyst and ferrum-based catalyst.The product of Fischer-Tropsch synthesis device is generally by water vapour, carbonic acid gas, nitrogen, unreacted synthesis gas (H ₂And CO), carburet hydrogen (C1-C5), oxygenatedchemicalss such as liquid hydrocarbon (C5+) and alcohol, aldehyde, ketone, acid, ester are formed; Most of water vapour, liquid hydrocarbon product withdrawn is condensed with oxygenatedchemicals and separate, and final reacting product generally can be divided into the several streams thighs of tail gas, liquid hydrocarbon and reaction water.Liquid hydrocarbon is processed in derived product upgrading workshop section obtains processed oil, and reaction water is delivered to the processing of water treatment workshop section.Fischer-Tropsch process exhaust is mainly by CO ₂, unreacted synthesis gas (H ₂+ CO), a small amount of gaseous hydrocarbon products and other components form.This tail gas can have part to loop back gasification unit, perhaps loops back Fischer-Tropsch synthesis device inlet, and burning perhaps acts as a fuel.

B. methyl alcohol is synthetic.

Synthetic gas carries out the methyl alcohol building-up reactions on methanol synthesis catalyst.Its building-up process has high-pressure process, middle-pressure process and low-pressure process, and the major reactor pattern has gas solid reactor and three phase slurry bed bioreactor.The product that the methyl alcohol building-up reactions obtains mainly is a methyl alcohol, and by product kind and amount then depend primarily on used synthesis condition and catalyzer.As it is more as dme and isopropylcarbinol to adopt high-pressure process zinc chrome catalyzer to generate; The by product that adopts the low-pressure process Cu-series catalyst to obtain is less.

(4) integrated coal gasification combined cycle (IGCC).

So-called combined cycle is exactly by will be in the Rankine cycle of the steam turbine of middle cold zone work and stacked at the Bradenton round-robin of the internal combustion turbine of high-temperature zone work, form a supply system circulation, because it has eventually warm (30～40 ℃) very low after very high combustion gas initial temperature (1200 ℃～1500 ℃) and the steam work done, realized the cascade utilization of heat energy, made total cycle efficiency very high.The IGCC system then is that the synthetic gas that utilizes the carbonaceous material gasification to obtain carries out combined cycle generation as combustion gas.For polygenerations systeme, to remove outside the part that is used for synthetic oil product or chemical, synthetic gas is mainly as fuel combustion, the body turbine system of degassing electrogenesis.The turbine off-gas of heat is by the heat recovery system by-product high-pressure steam, and this high pressure steam can expand and come drive-motor to produce extra electric power by steam turbine.

There are two subject matters in conventional coal fired power generation: high sulphur emissions and coal are difficult to handle as solid.Therefore, gasification being converted into IGCC system tool aspect environment protection that synthetic gas carries out combined cycle generation again has an enormous advantage.In addition, can effectively from gas, remove and collect CO by the IGCC process ₂, if in addition collection and treatment, as inject underground storage or adopt the chemically stable method to generate the carbonic acid mineral substance, can reduce the greenhouse gases CO2 emissions, in the future that CO2 emissions is required more and more stricter control, be significant economically.

Because Utilities Electric Co. is a utility company, need satisfy public's need for electricity as much as possible.And the need for electricity variation is comparatively violent, and peak load may be up to about 3 times of normal load.For one of treatment process of satisfying peak demand is exactly to build the parallel generating sets of many covers, can move abundant equipment required electric power is provided.But, often need to carry out the storage of geseous fuel if will improve or reduce gas production rates rapidly.

Under this background, adopt the IGCC and the chemical plant of the Poly-generation technology of chemical and electricity can utilize the synthetic chemical to satisfy the peak value power generation needs as deposit fuel, both realized the clean utilization of the energy, realized the variation of downstream energy product again, can adjust the product mix flexibly according to market demand, the market competitiveness is very strong.Compare with simple coal generating, gelatin liquefaction, IGCC, other chemicals production, can satisfy the requirement of each side such as efficient, cost, environment simultaneously.

Following several patents relates to existing main amalgamation factory/IGCC power plant operative technique.

United States Patent (USP) 4,092,825 to disclose a kind of gasification solid carbon raw material be synthetic gas, a part of synthetic gas and fischer-tropsch synthetic catalyst form can coagulate hydrocarbon, the process of a part of in addition synthetic gas combustion power generation.And the coagulated hydrocarbon that is obtained can be used as fuel and satisfies peak load to produce more electric energy.

United States Patent (USP) 5,543,437 disclose a kind of method for preparing Fischer-Tropsch synthetic and generating from coal based synthetic gas.Productive rate with a variation is produced Fischer-Tropsch synthetic, to satisfy the variation of synthetic gas as the fuel used to generate electricity demand.

United States Patent (USP) 5,179,129 disclose the integrated system of a multistage liquid phase methanol plant and standard GCC system.The waste heat of methanol reactor is used for reactor heating feeding gas and oiler feed, and perhaps byproduct steam is to produce extra electric power.

United States Patent (USP) 4,676,063 discloses the methyl alcohol with flexible operation of parallel module synthesizes/the GCC system.Deliver to methanol plant before water gas shift reaction, to use steam-laden synthetic gas incoming flow thigh, to increase the amount of hydrogen in the gas streams of advancing methanol sythesis reactor from the heat of acid gas removal system recoveries.In the GCC system, do not use the heat of methyl alcohol system recoveries.

United States Patent (USP) 4,273,743 disclose a chemical reaction system (mainly being synthetic ammonia), provide heat to half-closed Bradenton circulation power plant, realize coproduction electricity and chemical.It is synthetic that this patent has also been mentioned methyl alcohol especially.

English Patent 2,075,124 disclose a GCC/ methanol plant, and wherein methyl alcohol can be used as auxiliary material burning and drives fast and possess superior power load tracking power realizing.Utilize the synthetic byproduct steam of methyl alcohol in steam turbine, to generate electricity simultaneously.

United States Patent (USP) 20050150820 provides a kind of gasification, hydrocarbon is synthetic and the mutually integrated process of refining of petroleum, it mainly is the utilization of the heavy product of refining of petroleum, and adopting membrane separation apparatus that a part of synthetic gas is divided into poor hydrogen and hydrogen-rich stream thigh, the hydrogen-rich stream thigh mixes with synthetic gas regulates H ₂/ CO ratio goes Fischer-Tropsch synthetic, goes general facilities unit byproduct steam and generating as second strand of poor hydrogen stream thigh and aforementioned poor hydrogen stream thigh after another part hydrogen-rich stream stock-traders' know-how PSA dehydrogenation.

United States Patent (USP) 20030083391 provides a kind of process of generating electricity simultaneously and producing liquid hydrocarbon, after gasification obtains synthetic gas, a synthetic gas part is removed the synthetic liquid hydrocarbon that generates of Fischer-Tropsch, and Fischer-Tropsch synthetic tail gas mixes the generating of gas-steam combined circulating generation unit with another part synthetic gas.

The process that United States Patent (USP) 20020120017 proposes is a kind of generating, produce carbonic acid gas and hydrocarbon produces H/C than greater than 2 hydrocarbon from H/C less than 2 raw material.Its characteristics are that Fischer-Tropsch synthetic is separated into petroleum naphtha, diesel oil and paraffinic components, and the heat byproduct steam of vapourizing furnace and Fischer-Tropsch synthesis device by-product removes the steam turbine generation of combined cycle factory, and tail gas removes the gas turbine power generation of combined cycle factory.

United States Patent (USP) 4,549,396 provide a process with coal power generation, generate electricity with the burning synthetic gas by coal gas being turned to synthetic gas, its characteristics are to use air to gasify, and synthetic gas is converted into liquid hydrocarbon mixture and the following gas of C4, and the following gas of C4 is used for combustion power generation, and liquid hydrocarbon mixture is used for the peak value generating.

United States Patent (USP) 4,092,825 provide a process by the solid carbonaceous substance generating, obtain synthetic gas by gasification, part synthetic gas generates mixture under catalyst action, oxygenatedchemicals hydrogenation wherein is converted to hydro carbons, and the above hydrocarbon of the C3 of acquisition and another part synthetic gas are used for generating.

United States Patent (USP) 3,986,349 processes that provide a gasification solid carbon fuel to generate electricity, obtain synthetic gas by gasification, part synthetic gas generates mixture under catalyst action, mixture is divided into three-phase, and gas phase, water and oil phase generate electricity with another part synthetic gas, synthesis tail gas and liquid hydrocarbon product withdrawn.

Summary of the invention

Purpose of the present invention be exactly provide in order to overcome the defective that above-mentioned prior art exists a kind of more efficient, economical, be the method for raw material coproducing oil product, methyl alcohol and electric energy with the carbon containing combustible solid flexibly.

Purpose of the present invention can be achieved through the following technical solutions: a kind of is the method for raw material coproducing oil product, methyl alcohol and electric energy with the carbon containing combustible solid, and this method realizes by following workshop section at least: gasification workshop section, synthesizing section, vent gas treatment workshop section, product deep processing workshop section, generating workshop section; Realize that this method may further comprise the steps at least:

(1) in gasification workshop section, carbon containing combustible solid raw material and oxygen-containing gas, vapor generation reaction generate crude synthesis gas, with all or part of carbonic acid gas that is converted into of carbon monoxide, all crude synthesis gas all go to next workshop section at least a portion crude synthesis gas after purifying treatment is removed desulfuration, moisture and most of carbonic acid gas by the water vapor transformationreation;

(2) synthesizing section comprises a Fischer-Tropsch synthesis device and a methanol sythesis reactor at least, and the unstripped gas of each reactor can use synthetic gas, also can use the tail gas of other reactor outlets, can also use the gas mixture of synthetic gas and tail gas;

(3) in the Fischer-Tropsch synthesis device of synthesizing section, unstripped gas reacts under the effect of catalyzer, reaction product by follow-up cooling with operation such as separate and obtain liquid hydrocarbon mixture, the reaction water that contains organic oxygen-containing compound and tail gas, a part of tail gas gas disposal workshop section that truncates;

(4) in the methanol sythesis reactor of synthesizing section, unstripped gas obtains thick methyl alcohol and tail gas under the effect of catalyzer, a part of tail gas gas disposal workshop section that truncates;

(5) in vent gas treatment workshop section, go to the workshop section that generates electricity after the tail gas recycle portion gas component from synthesizing section;

(6) in product deep processing workshop section, synthesizing section, perhaps the liquid hydrocarbon mixture that obtains together of synthesizing section and vent gas treatment workshop section gives the hydrogenation upgrading with hydrogen, and is separated into processed oil under catalyst action;

(7) in product deep processing workshop section, the thick methyl alcohol that obtains from the synthesizing section methanol sythesis reactor obtains the refined methanol product through separating;

(8) in product deep processing workshop section, non-sour organic oxygen-containing compound such as wherein alcohol of the reaction water Separation and Recovery that contains organic oxygen-containing compound that is generated from synthesizing section Fischer-Tropsch synthesis device, aldehyde, ketone, ester, ether;

(9) generating workshop section comprises fuel gas-steam turbine combined cycle generation unit and steam turbine generation unit; The fuel used gas of fuel gas-steam turbine combined cycle generation unit is mainly the tail gas of each workshop section noted earlier, when peak of power consumption value and improper operating mode, can make the product of stand-by storage and the byproduct fuel that acts as a supplement; The steam turbine generation unit uses the steam of each workshop section's by-product noted earlier to drive generating.

Described carbon containing combustible solid is coal or refinery coke or the higher solid matter of other any combustible carbon content, or the combination of several materials.

Described oxidizing gas is generally oxygen or air, perhaps other oxygen rich gass.

The ratio of described synthetic gas conversion and not conversion, the degree of synthetic gas conversion depends on the proportion of production of required oil product, methyl alcohol and electric energy, and the combining and configuring of methanol sythesis reactor that is adopted and Fischer-Tropsch synthesis device.

Described Fischer-Tropsch synthesis device and methanol sythesis reactor can be connected for one or more levels, adopt when multistage all or part of unstripped gas as next stage of the tail gas of previous stage.

Described one or more levels placed in-line Fischer-Tropsch synthesis device and methanol sythesis reactor, each grade is made up of the synthesis reactor of one or more parallel connections.

The described conversion and the synthetic gas of conversion not are made into the mixed synthesis gas of definite composition according to the needs of different reactors at different levels, send to the inlet of each reactor.

The gaseous fraction that described vent gas treatment workshop section reclaims comprises a part of hydrogen at least, can also reclaim wherein lower carbon number hydrocarbons and the required useful component of other production processes by deep cooling simultaneously.

A part of hydrogen of described recovery can according to the needs of different reactors at different levels as a supplement gas send to reactor inlet, to regulate the composition of inlet gas.

Described vent gas treatment workshop section, the lower carbon number hydrocarbons component that freezing recovery obtains is sent to product deep processing workshop section as the part of liquid hydrocarbon mixture and is produced oil product, perhaps continues to separate and produces various derived product.

Described generating workshop section can also use a part of synthetic gas to generate electricity, and also can obtain more to be used to the synthetic gas that generates electricity in case of necessity by the method that reduces methyl alcohol and oil product output.

All oil products and the organic chemicals of described acquisition all can be used as the deposit fuel of generating.

In the described purifying treatment, water need remove as far as possible, and removes CO ₂Amount depend on the requirement of methyl alcohol synthetic.

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

(1) be that material gasification generation synthetic gas is a starting point with the carbon containing flammable solid, with the combined cycle generation is core, Fischer-Tropsch is synthetic to synthesize main product line with methyl alcohol, reaches a balance between the throughput of oil product, methyl alcohol, electric energy, has realized the efficient utilization of the energy and resource;

(2) by the conversion of gasification back gas with various and the comprehensive utilization of tail gas, in same system, to adjust synthetic gas flexibly and carry out the synthetic and Fischer-Tropsch synthetic ratio of methyl alcohol, product restructuring is convenient.

(3) by exhaust heat recovery power generation, many means such as exhaust combustion generating realize that energy reclaims to greatest extent.

(4) satisfy normally and the demand of peak value power load by the adjustment of the fuel reserve of number of chemical product and the load of chemicals production in case of necessity.

Description of drawings

Fig. 1 is the main-process stream block diagram of general coproducing oil product, methyl alcohol and electric energy.

Fig. 2 is each workshop section's schema of embodiment 1 to Fig. 6.

Fig. 2 is the gasification workshop section schema of embodiment 1.

Fig. 3 is the synthesizing section schema of embodiment 1.

Fig. 4 is the vent gas treatment workshop section schema of embodiment 1.

Fig. 5 is the product deep processing workshop section schema of embodiment 1,

Fig. 6 is the generating workshop section schema of embodiment 1.

Fig. 7 is the schema of several workshop sections of embodiment 2 to Figure 11.

Fig. 7 is the gasification workshop section schema of embodiment 2.

Fig. 8 is the synthesizing section schema of embodiment 2.

Fig. 9 is the vent gas treatment workshop section schema of embodiment 2.

Figure 10 is the product deep processing workshop section schema of embodiment 2,

Figure 11 is the generating workshop section schema of embodiment 2.

Figure 12 is the schema of several workshop sections of embodiment 3 to Figure 15.

Figure 12 is the gasification workshop section schema of embodiment 3.

Figure 13 is the synthesizing section schema of embodiment 3.

Figure 14 is the vent gas treatment workshop section schema of embodiment 3.

Figure 15 is the generating workshop section schema of embodiment 3.

Embodiment

The main-process stream block diagram of general coproducing oil product, methyl alcohol and electric energy as shown in Figure 1.

In gasification workshop section, carbon containing combustible solid raw material 1 gasifies in vapourizing furnace 2 and generates crude synthesis gas, the crude synthesis gas that is obtained is divided into stream thigh 3 and stream thigh 4, wherein stream thigh 3 carries out conversion by water gas shift reaction to CO in converter unit 5, flow thigh 4 and do not carry out conversion, stream thigh 4,6 is handled except that behind desulfuration, carbonic acid gas and the moisture through

purifying treatment unit

7 and 8 respectively and is removed synthesizing section.

In synthesizing section, the purification synthetic gas 10 of conversion is not divided into stream thigh 11 and stream thigh 12, and the purification synthetic gas 9 after the conversion is divided into stream thigh 13 and stream thigh 14.Wherein, a stream thigh 11 and stream strand 13 methyl methanol syngas that are made into definite composition enter methyl alcohol synthesis unit 15, generate thick methyl alcohol 17 and tail gas 18, and shift out the methyl alcohol synthesising reacting heat by oiler feed 34 byproduct steam modes, and byproduct steam stream thigh is 35; A stream thigh 12 and stream strand 14 Fischer-Tropsch synthetic gas that are made into definite composition enter Fischer-Tropsch synthesis unit 16, generate liquid hydrocarbon mixture 20, tail gas 21 and contain the reaction water 19 of oxygenatedchemicals, and shifting out Fischer-Tropsch synthesis heat by oiler feed 33 byproduct steams, byproduct steam stream strand is 36.Tail gas 18 from methanol sythesis reactor is divided into two portions, the stream strands 44 gas disposal workshop section that truncates, and stream strands 38 goes to the workshop section that generates electricity; Tail gas 21 from the Fischer-Tropsch synthesis device also is divided into two portions, the stream strands 43 gas disposal workshop section that truncates, and stream strands 37 goes to the workshop section that generates electricity.

In vent gas treatment workshop section, from the tail gas stream thigh 44 of methanol sythesis reactor in tail gas treating unit 23 recover hydrogen, and from the tail gas stream thigh 43 of Fischer-Tropsch synthesis device in tail gas treating unit 23 recover hydrogen and reclaim lower carbon number hydrocarbons.Tail gas treating unit 23 outlet stream thighs comprise recover hydrogen stream thigh 28 and reclaim low-carbon (LC) hydrocarbon stream thigh 32 that the tail gas 22 after the processing can be used as fuel gas or reduces internal heat the torch system.

In product deep processing workshop section, in hydrogenation upgrading unit 27, give the hydrogenation upgrading, and be separated into processed oil 30 with hydrogen stream thigh 28 from the liquid hydrocarbon mixture 20 of the synthetic acquisition of synthesizing section Fischer-Tropsch, the lower carbon number hydrocarbons 32 that reclaims; In refining methanol unit 26, isolate refined methanol 25 as product from the synthetic thick methyl alcohol that obtains of synthesizing section methyl alcohol; In the reaction water separating unit, isolate oxygenatedchemicalss 29 such as alcohol, aldehyde, ketone, acid, ester from the synthetic oxygen organic reaction water that contains that is generated of synthesizing section Fischer-Tropsch.

In generating workshop section, comprise gas-steam combined circulating generation unit 39 and steam-electric power unit 41.In gas-steam combined circulating generation unit 39, utilize

tail gas

37 and 38 to drive the generating of combustion gas turbine generator group as combustion gas, and utilize the high-temperature flue gas by-product high-pressure steam driving steam turbine generation unit behind the fuel gas buring further to generate electricity output electric energy 40; In steam-electric power unit 41, generally comprise a plurality of different pressures grade steam turbine generation units, can utilize the steam of generating to comprise that methyl alcohol synthesizes byproduct steam 35, the synthetic byproduct steam 36 of Fischer-Tropsch, can also use the steam-electric power of other workshop section's by-products, output electric energy 42.

Main-process stream block diagram shown in Figure 1 does not comprise all possible embodiment, and concrete embodiment will be illustrated in conjunction with the following examples.

Embodiment 1

Figure 2 shows that gasification workshop section.Coal 50 as gasified raw material is 486t/h, the water 51 that grinds back and 321t/h is made into coal water slurry, send into one group of coal slurry gasifier 52, and the 430t/h high pressure oxygen 53 that divides from sky carries out partial oxidation reaction between 1350-1400 ℃, obtains the crude synthesis gas 54 based on carbon monoxide and hydrogen.Crude synthesis gas 54 reclaims heats through waste heat boiler unit 55, with gas cooling to 660 ℃, enters water wash column 57 washings then and by the saturated battery limit (BL) of sending of water vapor.This process by-product 1110t/h, 9.8MPa, 540 ℃ steam 56, the steam of by-product is used for the acting of air separation facility air compressor machine and supercharger turbine; Obtained 4.0MPa and from air compressor machine, supercharger turbine, take out condensing again, 390 ℃ 127t/h steam, offer the acting of Fischer-Tropsch synthetic compressor turbine and methanol loop compressor turbine respectively, the about 51t/h of steam more than needed sends to steam pipe system and uses for each workshop section.Crude synthesis gas 58 flows that obtain are 1312945Nm ³/ h consists of N ₂: 0.41%, CO ₂: 17.89%, CO:30.54%, H ₂: 28.31%, CH ₄: 0.08%; H ₂S:0.54%; COS:0.02%; H ₂O:22.21%.

Crude synthesis gas 58 is divided into two strands, and wherein half crude synthesis gas 59 enters shift converter 61 behind heat temperature raising, issues the unboiled water gas shift reaction in the effect of transformation catalyst, makes portion C O be converted into CO ₂, interconversion rate is 57%.The gas purification units 63 that gas 62 after the conversion enters low-temperature rectisol removes CO wherein ₂, sulfide, other impurity and water, obtain to purify synthetic gas 64, flow is 403820Nm ³/ h, carbon-drop rate 93%; Half crude synthesis gas directly enters clean unit 65 and removes CO in addition ₂, sulfide, other impurity and water, obtain in addition that one purifies synthetic gas 66, flow is 388649Nm ³/ h, carbon-drop rate 99.5%.Purification synthetic gas gas 64 after the conversion consists of H ₂: 0.739, CO:0.212, CO ₂: 0.04, CH ₄: 0.001, N ₂: 0.005, Ar:0.002, H ₂O:0.001; Purification synthetic gas 66 gas compositions of conversion are not H ₂: 0.476, CO:0.513, CO ₂: 0.002, CH ₄: 0.001, N ₂: 0.004, AR:0.002, H ₂O:0.002.Conversion process by-product 4.0MPa, 390 ℃ of steam 27t/h send to generating workshop section.

Purification synthetic gas after the conversion is divided into two strands, and stream thigh 67 directly uses as methanol feedstock gas, and flow is 121146Nm ³/ h; Stream strand 68 flows are 282674Nm ³/ h, with a part not conversion purify synthetic air thigh 69 and mix, mixed flow thigh 71 is as the Fischer-Tropsch synthetic raw gas.

The purification synthetic gas of conversion is not divided into two strands, and stream strand 69 flows are 330352Nm ³H mixes with synthetic air thigh 68 after the conversion, and mixed stream strand 71 flows are 613026Nm ³/ h is as the Fischer-Tropsch synthetic raw gas; An other plume thigh 70 flows are 58297Nm ³/ h sends to generating.

The Fischer-Tropsch synthetic raw gas that is obtained consists of: H ₂: 0.597, CO:0.374, CO ₂: 0.019; CH ₄: 0.001; N ₂: 0.005; AR:0.002; H ₂O:0.001.

Figure 3 shows that synthesizing section, be divided into Fischer-Tropsch synthesis unit and methyl alcohol synthesis unit.

Fresh synthesis gas stream burst 71 temperature that obtain from synthesis gas preparation workshop section are 40 ℃, pressure 2.9MPa.Mix with reaction cycle tail gas 72, mixing back stream strand priority process two-stage interchanger 73 and 74 two-stages are preheating to 140 ℃ and enter paste state bed reactor 75, under the effect of low temperature fischer-tropsch synthetic catalyst, and 2.8MPa, 235 ℃ Fischer-Tropsch synthesis takes place down.Paste state bed reactor 75 is made up of the reactor of two parallel connections, and synthetic gas part in reactor 75 is converted into the hydrocarbons of liquid phase and gas phase: isolated liquid-phase product 76 obtains paraffin wax product 78 after interchanger 77 coolings, output is 45.74t/h.Gaseous products 79 enters quenching column 80 cooling washings, and the quenching column a part of liquid phase discharging 81 in bottom obtains 18.28t/h high temperature condensation product product 83 after water cooler 82 coolings; A part of in addition liquid phase discharging 84 usefulness recycle pumps 85 circulation backs and 86 heat exchange of reactor inlet gas, working off one's feeling vent one's spleen 87 further is cooled to 110 ℃ through interchanger 88 again and enters cat head, and making tower top outlet gas 89 temperature is 130 ℃; Cat head uncondensed gas 89 is earlier after after hot de-salted water water cooler 90 and water recirculator 91 be cooled to 40 ℃, enter high-pressure separator 92, the cryogenic condensation produce product 93 that isolated oil phase hydrocarbons is output 15.50t/h, the water product is the reaction water 94 that is rich in oxygenatedchemicals, output 94.51t/h.

Tail gas 98 about 596225Nm that high-pressure separator is separated ³/ h is divided into two portions, and wherein the flow of stream thigh 99 is 367587Nm ³/ h, compressed machine 100 compression back Returning reactor inlets; Stream thigh 101 is 228638Nm ³/ h, the gas-steam combined circulating generation unit of sending to generating workshop section is as fuel gas generation.Tail gas consists of H ₂O:0.003, H ₂: 0.498; CO:0.275; CO ₂: 0.164; Ar:0.005; CH ₄: 0.026; C ₂H ₄: 0.002; C ₂H ₆: 0.001; C ₃H ₆: 0.002; C ₃H ₈: 0.001; C ₄H ₈: 0.002; C ₄H ₁₀: 0.001; C ₅H ₁₀: 0.002; C ₅H ₁₂: 0.001; C ₆H ₁₂: 0.001; C ₇: 0.001; Ethanol: 0.001; Acetone: 0.001; N ₂: 0.013.

The heat that Fischer-Tropsch synthesis produces is removed in the mode of feedwater byproduct steam by reactor 75 inner cool tubes 102, by-product saturation steam 104 in gas bag 103, pressure are 1.6Mpa, about 425t/h, be divided into two portions: stream thigh 105,287t/h are sent to the steam-electric power unit generating of generating workshop section; Stream thigh 106,138t/h sends to steam pipe system and uses for each workshop section.

Methanol feedstock air-flow thigh 67 flows are 121146Nm ³/ h, mix with loop tail air-flow thigh 107 from gas-liquid separator, with enter fixed bed methanol sythesis reactor 109 after reactor outlet gas 108 heat exchange, at 5MPa pressure, it is synthetic to carry out methyl alcohol under 220 ℃ the temperature in, about 240 ℃ of temperature out, exit gas is cooled to 40 ℃ through reactor inlet preheater 110 and recirculated cooling water water cooler 111 two-stages, enters gas-liquid separator 112, isolates thick methyl alcohol stream thigh 113, flow is 41.72t/h, contains the water of 7.78wt%; Isolated tail gas stream thigh 114 flow 581190Nm ³/ h, wherein stream burst 115 circulations are 545163Nm ³/ h; Stream gang 116 flow 36027Nm ³/ h is divided into two portions, stream thigh 117,20797Nm ³/ h sends to vent gas treatment workshop section recover hydrogen; Stream thigh 118,15230Nm ³/ h goes to the workshop section that generates electricity.

The methyl alcohol synthesis tail gas consists of H ₂: 0.868, CO:0.074, CO ₂: 0.02, CH ₄: 0.004; Methyl alcohol: 0.01, N ₂: 0.016, AR:0.006, H ₂O:0.002.

The temperature of methanol sythesis reactor 109 reclaims heat by feedwater, and by-product 2.5MPa, the steam 119 of 38t/h, the steam of by-product send to combined cycle power plant's generating.

Figure 4 shows that vent gas treatment workshop section.

Methanol-fueled exhaust stream thigh 117 is 20797Nm ³/ h enters pressure-swing absorption apparatus 120 and isolates wherein hydrogen, obtains 99.5% hydrogen stream thigh, 121 about 18051Nm ³/ h, this hydrogen stream stock is two portions, wherein stream thigh 122 is 14802Nm ³/ h is used for the hydrotreatment and the cracking of Fischer-Tropsch synthetic crude product, and stream thigh 123 is 3249Nm ³/ h is used for the fischer-tropsch synthetic catalyst reduction.Isolate the tail gas 124 behind the hydrogen, about 2746Nm ³/ h goes the fuel gas system use that acts as a fuel.This tail gas consists of: H ₂: 0.033, CO:0.54; CO ₂: 0.15; CH ₄: 0.031; Methyl alcohol: 0.071; N ₂: 0.118; AR:0.043; H ₂O:0.013.

Figure 5 shows that product deep processing workshop section.

As shown in Figure 5, it is 79.52t/h that the synthetic three kinds of liquid-phase products (cryogenic condensation thing 93, high temperature condensation product 83 and paraffin 78) that generate of Fischer-Tropsch mix back stream strand 130 flows, at first mix, after interchanger 132 preheatings, enter hydrotreating reactor 133 with hydrogen stream thigh 131.Wherein hydrogen stream thigh 131 is made up of a hydrotreatment recycle hydrogen stream thigh 134 and burst 135 mixing of hydrotreatment supply hydrogen stream, and the hydrogen stream thigh 122 that hydrotreatment supply hydrogen stream thigh 135 obtains from tail gas recycle.

In hydrotreating reactor 133, under the effect of catalyzer, mainly carry out the hydrogenation saturated reaction of alkene and the hydrogenation and removing of impurity.Outlet liquid hydrocarbon mixture 136 is isolated hot phase logistics 138 and hydrothermal solution logistics 139 mutually through high pressure hot separator 137 earlier, and hot phase logistics 138 enters cold high pressure separator 141 after water cooler 140 coolings.The high pressure vapor stream thigh of isolating in cold high pressure separator 141 based on hydrogen 142 loops back the reactor inlet use by recycle compressor 143, isolated cold liquid phase stream thigh 144 is mixed into cold low separator 145 with the hot liquid phase stream thigh 139 of high pressure hot separator, the gas 146 that obtains after the vacuum flashing is sent to flare system, and liquid 147 is introduced stripping tower 148.The gas phase 149 of stripping tower 148 is sent to the fuel gas pipe network, separation column 152 is sent to, fractionation in separation column 152, cat head output naphtha stream thigh 153 after drawing 151 heating of liquid phase 150 heater vias in the bottom, side line is extracted diesel stream thigh 154 out, and output tail oil 155 goes the isomery hydrocracking at the bottom of the tower.

The tail oil 156 of tail oil 155 after the isomery hydrocracking through after the stable hydrogenation processing mixes with hydrogen stream thigh 157, after heater via 158 preheatings, enters isocracking reactor 159.Wherein hydrogen stream thigh 157 is made up of a hydrotreatment recycle hydrogen stream thigh 160 and burst 161 mixing of hydrotreatment supply hydrogen stream, and hydrotreatment supply hydrogen stream thigh 161 is from the hydrogen stream thigh 122 of tail gas recycle.

In isocracking reactor 159, what carry out mainly is the hydrocracking and the isomerization reaction of hydro carbons, and macromolecule hydrocarbon is converted into the small molecules hydro carbons.Isolate hot phase logistics 164 and hydrothermal solution logistics 165 mutually through high pressure hot separator 163 earlier through the outlet liquid hydrocarbon mixture after the hydrocracking 162, hot phase logistics 164 enters cold high pressure separator 167 after interchanger 166 coolings.The high pressure vapor stream thigh of isolating in cold high pressure separator 167 based on hydrogen 168 loops back the 159 inlet uses of isocracking reactor through recycle compressor 169, and isolated cold liquid phase stream thigh 170 is gone into cold low separator 171 with the hot liquid phase stream thigh 165 of high pressure hot separator 163.The gas 172 that obtains after the vacuum flashing is sent to flare system, and liquid 173 is introduced stripping tower 174, and the gas phase 175 of stripping tower 174 is sent to the fuel gas pipe network, and separation column 178 is sent to, fractionation in separation column 178 after drawing 177 heating of liquid phase 176 heater vias in the bottom.Cat head output petroleum naphtha 179, side line is extracted diesel oil 180 out, 156 times isomery hydrocracking reactors of output tail oil, 159 inlets at the bottom of the tower.

Through symbiosis output petroleum naphtha 17.39t/h and diesel oil 61.54t/h after hydrotreatment and the isocracking.In year service hours 8000 hours, produce 63.14 ten thousand tons of oil products per year.Common property is given birth to tail gas 1.09t/h, because pressure is lower and amount is few, so do not bother to see me out as fuel gas generation but send to flare system.

Fischer-Tropsch synthesizer reaction water 94 enters rectifying tower 95, what cat head obtained 5.14t/h contains oxygenatedchemicalss (based on alcohol) such as alcohol, aldehyde, ketone strands 96, contain 30wt% moisture, act as a fuel, the flow 89.37t/h of waste water 97 at the bottom of the tower, contain methyl alcohol less than 100ppm, send to and be used for the vapourizing furnace gasification after the wastewater treatment.

Thick methyl alcohol stream thigh 113 is sent to methanol rectifying tower 182 rectifying and is reclaimed methyl alcohol, and cat head obtains the refined methanol product 183 of 37.80t/h, and waste water 184 is used for the vapourizing furnace gasification after sending to wastewater treatment at the bottom of the tower.In year service hours 8000 hours, produce 30.24 ten thousand tons of refined methanols per year.

Figure 6 shows that generating workshop section, this generating workshop section comprises steam-gas Combined circulating generation unit and steam-electric power unit.

Steam-gas Combined circulating generation unit is made up of combustion gas turbine generator group and supporting steam turbine generation unit.

The fuel gas stream thigh that combined cycle generation combustion gas unit uses has: gasification workshop section is the purification synthetic air thigh 70 of conversion not, Fischer-Tropsch process exhaust stream thigh 101, methyl alcohol synthesis tail gas stream thigh 118, the gas 200 that acts as a fuel after these three strands of gases mix enters the unitary internal combustion turbine 202 of gas-steam combined circulating generation after preheater 201 preheatings combustion chambers burn, the high-temperature high-pressure fuel gas that the combustion chamber produces drives generating set 203 works done generating.The high-temperature high-pressure fuel gas 204 of internal combustion turbine unit outlet enters waste heat boiler 205, and by-product goes out the high pressure superheated steam 206 of 6MPa, enters the steam turbine 207 of gas-steam combined Cycle Unit, drives generating set 208 works done generating.

Selected for use 2 210MW gas-steam combined Cycle Unit to generate electricity.During driving and during accidental state, can use methanol product that part stores fuel 209 as a supplement.

In the steam-electric power unit, for steam and the heat that makes full use of the process by-product, the saturation steam of the synthetic by-product of a small amount of 4.0MPa steam more than needed and the methyl alcohol 1.6MPa that all reduces pressure, saturation steam with the synthetic by-product of Fischer-Tropsch mixes again, mixed vapour stream thigh 210 flows are 372t/h, after in preheater 211, being superheated to 280 ℃, enter the steam turbine generating set 212 of low pressure steam generating set workshop section, drive generating set 213 generatings.The steam turbine generating set is configured to the unit of 2 30MW.

Embodiment 2

The maximum difference of embodiment 2 and embodiment 1 is that Fischer-Tropsch is synthetic and has adopted the two-stage series structure that all the other each unit are similar to last embodiment.

The gasification workshop section of embodiment 2 as shown in Figure 7.The preparation flow of crude synthesis gas, operating parameters, raw material consumption and thick gas output are formed identical with embodiment 1.Be that it is synthetic that the synthetic gas of whole not conversion and the synthetic gas one after the part conversion are used from Fischer-Tropsch with embodiment 1 main difference part.

In vapourizing furnace 223, as gasified raw material, be made into coal water slurry with coal 220 with water 221, carry out coal gasification reaction with high pressure oxygen 222, obtain crude synthesis gas 224 based on carbon monoxide and hydrogen.The coal amount that consumes is 486t/h, and the water yield is 321t/h, and high pressure oxygen is 430t/h.

Crude synthesis gas 224 reclaims heats through waste heat boiler unit 225, enters water wash column 227 washings then and by the saturated battery limit (BL) of sending of water vapor.Final crude synthesis gas 228 flows that obtain are 1312945Nm ³/ h forms identical with embodiment 1.This process by-product 1110t/h, 9.8Mpa, 540 ℃ steam 226, the steam of by-product is used for the acting of air separation facility air compressor machine and supercharger turbine; Obtain 4.0Mpa and take out condensing from air compressor machine, supercharger turbine, 390 ℃, the steam of 127t/h offers the acting of Fischer-Tropsch synthetic compressor turbine and methanol loop compressor turbine respectively, and the about 51t/h of steam more than needed sends to steam pipe system and uses for each workshop section.

Crude synthesis gas 228 is divided into two strands, and wherein 54% crude synthesis gas stream strands 229 enters shift converter 230 behind heat temperature raising, under the effect of transformation catalyst in the generation transformationreation, make portion C O be converted into CO ₂, interconversion rate is 57%.Gas 231 after the conversion removes CO wherein in clean unit 232 ₂, sulfide, other impurity and water, obtain to purify synthetic gas 233, flow is 436104Nm ³/ h, carbon-drop rate 93%; Other 46% crude synthesis gas stream thigh 236 directly removes CO at clean unit 237 ₂, sulfide, other impurity and water, obtain in addition that one purifies synthetic gas 238, flow is 356941Nm ³/ h, carbon-drop rate 99.5%.

Conversion process by-product 4.0MPa, 390 ℃ of steam 29t/h also send to steam pipe system and use for each workshop section.

Because crude synthesis gas is formed, the CO interconversion rate is all identical with last embodiment, therefore the gas composition of purification synthetic gas, the purification synthetic gas gas composition after the conversion of conversion are not identical with embodiment 1.

Purification synthetic gas 233 after the conversion is divided into two strands, and stream thigh 234 directly uses as methanol feedstock gas, and flow is 130831Nm ³/ h, stream thigh 235, flow is 305273Nm ³/ h purifies synthetic air thigh 238 with conversion not and mixes, and mixed stream plume amount is 662216Nm ³/ h is as Fischer-Tropsch synthetic raw gas 239.

The Fischer-Tropsch synthetic raw gas 239 that is obtained consists of H ₂: 0.597; CO:0.375; CO ₂: 0.019; CH ₄: 0.001; N ₂: 0.005; AR:0.002.

The synthesizing section of embodiment 2 is divided into Fischer-Tropsch synthesis unit and methyl alcohol synthesis unit two major parts as shown in Figure 8 equally.

Come the Fischer-Tropsch synthetic raw gas 239 of autopneumatolysis workshop section to mix, be preheating to 140 ℃, enter into one-level synthesis reactor 253 through interchanger 251 and interchanger 252 secondary heat exchange with one-level recycled offgas 250.One-level synthesis reactor 253 is two reactor parallel connections, and each reactor all is a paste state bed reactor, and working pressure is 30bar, and service temperature is 235 ℃, and two reactors of one-level are isolated paraffin stream thigh 254, and flow is 49.41t/h.Gas 255 from reactor head enters into one-level quenching column 256, quenching column 256 bottom products part stream thigh 258 is as circulation Quench liquid, carry through pump 259,, and in interchanger 260, further be cooled to 110 ℃ and enter cat head with the heat exchange in interchanger 252 of reactor inlet gas; Quenching column bottom product another part stream thigh 257 is as high temperature condensation product product, and output is 19.75 tons/hour.Quenching column top exit gas 261 enters high-pressure separator 264 after supercooler 262 and 263 two-stages are cooled to 40 ℃.264 li of high-pressure separator, mixture is separated into gas-liquid two-phase.Oil reservoir in the liquid phase is a cryogenic condensation thing 265, and output is 16.74 tons/hour; Water 266 is a reaction water in the liquid phase, and output is 101.69 tons/hour.Separator top tail gas 267 is divided into two portions, and wherein stream thigh 268 is 389200Nm ³/ h, as recycled offgas through compressor 269 compression back with return one-level synthesis reactor 253 after one-level virgin gas 239 is mixed, a remaining part flows thigh 270, enters second stage F-T synthesis reaction device as the virgin gas of second order reaction.

The second stage fischer-tropsch synthesis technique and first segment base are originally similar.Virgin gas 270 is heated to 140 ℃ through two sections preheaters 272 and 273 preheatings after mixing with recycled offgas 271, enter secondary F-T synthesis reaction device 274, second reactor is formed in parallel by two paste state bed reactors equally, reactor operating pressure is 25bar, service temperature still is 235 ℃, and the paraffin of output stream strands 275 is 9.79t/h in two reactors.Reactor head gas 276 enters secondary quenching column 277: a quenching column bottoms part, stream thigh 279, after being cooled to 110 ℃ through two sections preheaters 273 of second reactor and secondary quenching column cycle heat exchange device 280 as Quench liquid 278, power by pump 281 is sent into quenching column 277 cats head, and making the top tray temperature is 130 ℃; Another part, promptly the stream thigh 282, and as secondary high temperature condensation product product, output is 7.45 tons/hour.Quenching column top output gas 283 enters secondary high-pressure separator 286 after being cooled to 40 ℃ through two water coolers 284 and 285.In secondary high-pressure separator 286, isolate liquid and gas.Oil reservoir in the liquid phase is secondary cryogenic condensation produce product 287, and output is 11.59 tons/hour; Water layer is a reaction water 288, and output is 35.85 tons/hour.This moment, the flow from the gas streams 289 that the secondary high-pressure separator is come out was 399013Nm ³/ h is divided into two portions: stream thigh 290, flow is 281957Nm ³/ h passes through back the mixing with secondary virgin gas 270 of compressor 291 compressions and returns second reactor 274; Rest part is stream thigh 292, flow 117056Nm ³/ h all enters vent gas treatment workshop section.

Tail gas consists of H ₂O:0.004; H ₂: 0.292; CO:0.125; CO ₂: 0.409; Ar:0.012; CH ₄: 0.081; C2H ₄: 0.008; C ₂H ₆: 0.002; C ₃H ₆: 0.009; C ₃H ₈: 0.002; C ₄H ₈: 0.006; C ₄H ₁₀: 0.003; C ₅H ₁₀: 0.005; C ₅H ₁₂: 0.002; C ₆H ₁₂: 0.003; C ₆H ₁₄: 0.001; C ₇: 0.001; Ethanol: 0.001; Acetone: 0.003; Nitrogen: 0.030.

The heat that Fischer-Tropsch synthesis produces is removed in the mode of drum 295 and 296 byproduct steams by firsts and seconds reactor 253 and 274 inner cool tubes 293 and 294.The saturation steam 297 of by-product and 298 pressure are 1.6MPa, and flow is respectively 457t/h and 152t/h, stream gang 299 total 609t/h after mixing, and be divided into two strands: wherein stream thigh 300 is sent to the steam turbine unit generation of generating workshop section for 453t/h; Stream thigh 301 is 156t/h, sends to steam pipe system and uses for each workshop section.

Methanol feedstock air-flow thigh 234 flows are 130831Nm ³/ h, mix with loop tail air-flow thigh 302 from gas-liquid separator, with enter fixed bed methanol sythesis reactor 304 after reactor outlet gas 303 heat exchange, at 5MPa pressure, it is synthetic to carry out methyl alcohol under 220 ℃ the temperature in, about 240 ℃ of temperature out, exit gas 303 is cooled to 40 ℃ through inlet gas interchanger 306 and recirculated cooling water water cooler 307 two-stages, enter gas-liquid separator 308, isolate thick methyl alcohol stream thigh 309, flow 45.05t/h contains the water of 7.78wt%. isolated tail gas 310 flow 627653Nm ³/ h, wherein stream burst 311 circulations, flow is 588741Nm ³/ h; Stream thigh 312 is divided into two portions, stream thigh 313, flow 22787Nm ³/ h sends to vent gas treatment workshop section recover hydrogen; Stream thigh 314,16125Nm ³/ h goes to the workshop section that generates electricity.

Tail gas consists of H ₂: 0.868; CO:0.074; CO ₂: 0.02; CH ₄: 0.004; Methyl alcohol: 0.01; N ₂: 0.016; AR:0.006; H ₂O:0.002.

The temperature of methanol sythesis reactor reclaims heat by feedwater, and by-product 2.5MPa, the steam 315 of 41t/h, the steam of by-product send to the generating of generating workshop section.

First stage reactor paraffin 254 and second stage reactor paraffin 275 mixed paraffin stream thighs 316, first stage reactor high temperature condensation product 257 and second stage reactor high temperature condensation product 282 mixed high temperature condensate flow thighs 317, first stage reactor cryogenic condensation thing 265 and second stage reactor cryogenic condensation thing 287 mixed streams strands 318 are sent to the hydrogenation upgrading workshop section oil that manufactures a finished product.

First order reaction water 266 and second order reaction water 288 mixed reaction water stream thighs 319, flow is 137.54t/h, removes product deep processing workshop section recovery oxygenatedchemicals wherein.

Figure 9 shows that vent gas treatment workshop section.Be divided into recovery of Fischer-Tropsch process exhaust lower carbon number hydrocarbons and methyl alcohol synthesis tail gas hydrogen and reclaim the two parts.

Fischer-Tropsch process exhaust stream thigh 292, enter dewatering unit 320 dehydrations, dehydration back stream strands 321 is cooled to about-40 ℃ through water cooler 322 and 323 two-stages, the above component of most C3 and contained a small amount of oxygenatedchemicals are cooled and get off to become liquid in the tail gas, form gas-liquid mixed logistics 324, separate by gas-liquid separator 325, liquid portion 326 enters gas stripping column 327, emit as stream thigh 329 with most carbonic acid gas that nitrogen gas stream thigh 328 gas propose in the liquid, wherein CO ₂Can further be collected; Its residual current thigh 330 is the lower carbon number hydrocarbons product, and 5.21t/h is arranged, and comes along product purification workshop section as raw material and Fischer-Tropsch synthetic crude product.

The stream thigh 332 of gas-liquid separator 325 top gas after interchanger 331 re-heats goes to generate electricity workshop section as fuel gas generation.This tail gas consists of H ₂: 0.484; AR:0.016; N ₂: 0.044; CO:0.265; CO ₂: 0.002; CH ₄: 0.151; C ₂H ₄: 0.015; C ₂H ₆: 0.004; C ₃H ₆: 0.011; C ₃H ₈: 0.003; C ₄H ₈: 0.003; C ₄H ₁₀: 0.002; C ₅H ₁₀: 0.001.

Methanol-fueled exhaust stream thigh 313, flow is 22466Nm ³/ h sends to dehydrogenation unit 334 separating hydrogen gas, obtains 99.5% hydrogen stream thigh, 335 about 19499Nm ³/ h, this hydrogen stream stock is two portions, wherein stream thigh 336 is 15985Nm ³/ h is used for the hydrotreatment and the cracking of thick product, and stream thigh 337 is 3514Nm ³/ h is used for catalyst reduction.Isolate the tail gas 338 behind the hydrogen, about 2967Nm ³/ h goes the fuel gas system use that acts as a fuel.This tail gas consists of H ₂: 0.033; CO:0.535; CO ₂: 0.149; CH ₄: 0.032; Methyl alcohol: 0.072; N ₂: 0.121; AR:0.044; H ₂O:0.014.

Figure 10 shows that the product deep processing workshop section of embodiment 2.

The material 340 that is merged together by the synthetic paraffin stream that produces of fischer-tropsch strands 316, high temperature condensate flow thigh 317, cryogenic condensation thing 318 and the lower carbon number hydrocarbons product 330 that reclaims, at first enter a gas stripping column 341, carry out gas with 342 pairs of liquid of hot nitrogen and carry, overhead gas 343 contains more CO ₂And nitrogen, and a small amount of lower carbon number hydrocarbons, the torch system of reducing internal heat; Remove most CO ₂After liquid flow thigh 344 mix with circulation tail oil 345 and hydrogen, hydrogen source is fresh hydrogen 346 and circulating hydrogen 347.Reactions such as successively by hydrotreating reactor 349 and hydrocracking reactor 350, the process hydrogenation is saturated after preheater 348 preheatings for mixed material, cracking, isomerization obtain mixing liquid hydrocarbon product stream thigh 351.Stream strands 351 enters high pressure hot separator 352 through carry out heat exchange with hydrotreating reactor 349 inlet gass in interchanger 348 after, be separated into thermal high vapor phase stream thigh 353 and thermal high liquid phase stream thigh 354.Thermal high vapor phase stream thigh 353 is cooled to 40 ℃ through water cooler 355, and being separated in cold high pressure separator 356 with hydrogen is the cold anticyclone vapor phase stream thigh 347 of main component, as the circulation hydrogen make-up; The isolated liquid phase stream thigh 357 of cold high pressure separator mixes with thermal high liquid phase stream thigh 354, enters one-level cold low separator 358 after the decompression.The vapor phase stream thigh 359 of one-level cold low separator 358 is cooled to 40 ℃ through water cooler 360 and isolates gas-liquid two-phase in secondary cold low separator 361, and gas phase 362 is gone fuel gas system, and liquid phase 363 is removed petroleum naphtha stabilizer tower 364.The liquid phase stream thigh 365 of one-level cold low separator 358 enters separation column 367 after interchanger 366 re-heats.

In separation column 367, tower middle and lower part output diesel oil distillate 368, output is 88.75t/h; Tower top output light constituent 369 separates liquid phase 363 and mixes with secondary cold low separator, enter petroleum naphtha stabilizer tower 364 after interchanger 371 re-heats; Cat head gas phase 370 enters fuel gas system; And tail oil 372 loops back hydrotreating reactor 349 inlets at the bottom of the tower after interchanger 373 heating.

In petroleum naphtha stabilizer tower 364, output petroleum naphtha 374 at the bottom of the tower, output 25.08t/h; From tower middle and upper part output liquefied petroleum gas (LPG) 375, output 4.91t/h, cat head emit light constituent 376 and send to fuel gas system.

In year service hours 8000 hours, above oil product is produced per year can reach 950,000 tons altogether.

Thick methyl alcohol 309 separates through methanol rectifying tower 380, and cat head obtains the refined methanol stream thigh 381 of 99.5wt%, and flow is 41.49t/h.In year operation 8000 hours, can produce 33.19 ten thousand tons of methyl alcohol per year.

Fischer-Tropsch synthesizer reaction water 319 enters rectifying tower 400, the oxygenatedchemicalss (based on alcohol) such as alcohol, aldehyde, ketone that contain that cat head obtains 7.48t/h flow thigh 401, contain 30wt% moisture, act as a fuel, the flow 130.06t/h of waste water 402 at the bottom of the tower, contain methyl alcohol less than 100ppm, send to and be used for the vapourizing furnace gasification after the wastewater treatment.

Generating workshop section flow process disposes as shown in figure 11, and this generating workshop section is similar to embodiment 1, comprises steam-gas Combined circulating generation unit and steam-electric power unit equally.

The fuel gas stream thigh that combustion gas unit in the combined cycle generation unit uses comprises the Fischer-Tropsch process exhaust stream that takes off behind the lower carbon number hydrocarbons strands 332 and methyl alcohol synthesis tail gas stream strands 314, the gas 410 that acts as a fuel after these two strands of gases mix enters the unitary internal combustion turbine 412 of gas-steam combined circulating generation after preheater 411 preheatings combustion chambers burn, the high-temperature high-pressure fuel gas that the combustion chamber produces drives generating set 413 works done generating.The high-temperature high-pressure fuel gas 414 of internal combustion turbine unit outlet enters waste heat boiler 415, and by-product goes out the high pressure superheated steam 416 of 6MPa, enters the steam turbine 417 of gas-steam combined Cycle Unit, drives generating set 418 works done generating.

Selected for use 1 150MW gas-steam combined Cycle Unit to generate electricity.During driving and during accidental state, can use oxygenatedchemicals product that part stores and methanol product fuel 419 as a supplement.

In the steam-electric power unit, for steam and the heat that makes full use of the process by-product, the saturation steam of the synthetic by-product of the methyl alcohol 1.6MPa that all reduces pressure, saturation steam with the synthetic by-product of Fischer-Tropsch mixes again, mixed vapour stream thigh 420 flows are 514t/h, after in preheater 421, being superheated to 280 ℃, enter the steam turbine generating set 422 of low-pressure steam generating set workshop section, drive generating set 423 generatings.The steam turbine generating set is configured to the unit of 1 75MW.

Embodiment 3

Embodiment 3 distinguishes the structure that has been to adopt Fischer-Tropsch synthesis device and methanol sythesis reactor two-stage series with the maximum of embodiment 1, and all the other each unit are similar to last embodiment.

Gasification workshop section as shown in figure 12.The preparation flow of crude synthesis gas, operating parameters, raw material consumption and thick gas output are formed with

embodiment

1 and 2 identical.With last embodiment main difference part be that synthetic gas all carries out the unstripped gas of conversion as the Fischer-Tropsch synthesis device.

In vapourizing furnace 433, as gasified raw material, be made into coal water slurry with coal 430 with water 431, carry out coal gasification reaction with high pressure oxygen 432, obtain crude synthesis gas 434 based on carbon monoxide and hydrogen.The coal amount that consumes is 486t/h, and the water yield is 321t/h, and high pressure oxygen is 430t/h.

Crude synthesis gas 434 reclaims heats through waste heat boiler unit 435, enters water wash column 437 washings then and by the saturated battery limit (BL) of sending of water vapor.Final crude synthesis gas 438 flows that obtain are 1312945Nm ³/ h forms identical with embodiment 1.This process by-product 1110t/h, 9.8MPa, 540 ℃ steam 436, the steam of by-product is used for the acting of air separation facility air compressor machine and supercharger turbine; Obtain 4.0MPa and take out condensing from air compressor machine, supercharger turbine, 390 ℃, the steam of 127t/h offers the acting of Fischer-Tropsch synthetic compressor turbine and methanol loop compressor turbine respectively, and the about 51t/h of steam more than needed sends to steam pipe system and uses for each workshop section.

Crude synthesis gas 438 enters shift converter 440 behind heat temperature raising, transformationreation takes place under the effect of transformation catalyst, makes portion C O be converted into CO ₂, interconversion rate is 24.5%.Gas 441 after the conversion removes CO wherein in clean unit 442 ₂, sulfide, other impurity and water, obtain to purify synthetic gas 443, flow is 780000Nm ³/ h, carbon-drop rate 99%.Purifying the synthetic gas gas composition is H ₂: 0.600, CO:0.390, CO ₂: 0.004, Ar:0.001, CH ₄: 0.001, N ₂: 0.004.

Conversion process can by-product 4.0MPa, and 390 ℃ of steam 23t/h send to steam pipe system and use for each workshop section.

Synthesizing section is the two-stage tandem of Fischer-Tropsch synthesis device and methanol sythesis reactor as shown in figure 13.

Fresh synthesis gas stream burst 443 temperature that obtain from synthesis gas preparation workshop section are 40 ℃, pressure 2.9MPa.This gas mixes with reaction cycle tail gas 452, mix a back stream burst priority and carry out preheating through two-stage interchanger 453 and 454, be preheating to 140 ℃ of paste state bed reactors 455 that enter two parallel connections, under the effect of fischer-tropsch synthetic catalyst, 2.8MPa, 235 ℃ Fischer-Tropsch synthesis takes place down, and synthetic gas part in reactor 455 is converted into the hydrocarbons of liquid phase and gas phase: isolated liquid-phase product 456 obtains paraffin wax product 458 after interchanger 457 coolings, output is 58.64t/h.Gaseous products 459 enters quenching column 460 cooling washings, the quenching column a part of liquid phase discharging 461 in bottom obtains 22.86t/h high temperature condensation product product 463 after water cooler 462 coolings, a part of in addition liquid phase discharging 464 usefulness recycle pumps 465 circulation backs and 466 heat exchange of reactor inlet gas, working off one's feeling vent one's spleen 467 further is cooled to 110 ℃ through interchanger 468 again and enters cat head, and making tower top outlet gas 469 temperature is 130 ℃; Tower top outlet gas 469 is earlier after after hot de-salted water water cooler 470 and water recirculator 471 be cooled to 40 ℃, enter high-pressure separator 472, the cryogenic condensation produce product 473 that isolated oil phase hydrocarbons is output 19.25t/h, the water product is the reaction water 474 that is rich in oxygenatedchemicals, output 119.63t/h.

Tail gas 478 about 747088Nm that high-pressure separator is separated ³/ h is divided into two portions, and wherein the flow of stream thigh 479 is 467990Nm ³/ h, compressed machine 480 compression back Returning reactor inlets; Stream thigh 481 is 279098Nm ³/ h is divided into three parts: the stream strands 497 workshop section's generating of going to generate electricity, flow is 111569Nm ³/ h; Stream thigh 498 removes to reclaim lower carbon number hydrocarbons and hydrogen, and flow is 97798Nm ³/ h; Stream thigh 499 is sent to the methanol sythesis reactor inlet, and flow is 69731Nm ³/ h.Tail gas consists of H ₂O:0.003, H ₂: 0.500, CO:0.300, CO ₂: 0.140, Ar:0.004, CH ₄: 0.026, C ₂H ₄: 0.003, C ₂H ₆: 0.001, C ₃H ₆: 0.002, C ₃H ₈: 0.001, C ₄H ₈: 0.002, C ₄H ₁₀: 0.001, C ₅H ₁₀: 0.002, C ₅H ₁₂: 0.001, C ₆H ₁₂: 0.001, C7:0.001, ethanol: 0.001, acetone: 0.001, N ₂: 0.010.

The heat that Fischer-Tropsch synthesis produces is by reactor 455 inner cool tubes 482, mode with the feedwater byproduct steam is removed, by-product saturation steam 484 in gas bag 483, pressure is 1.6MPa, about 538t/h, be divided into two portions: stream thigh 485, flow 363t/h sends to the low-pressure steam generating set generating of generating workshop section; Stream thigh 486, flow 175t/h sends to steam pipe system and uses for each workshop section.

Stream strands 499 with from vent gas treatment workshop section hydrogen stream thigh 475 (99.5%, flow 48939Nm ³/ h) mixing, the flow of mixed flow thigh 476 is 118670Nm ³/ h consists of H ₂O:0.002, H ₂: 0.704, CO:0.178, CO ₂: 0.083, Ar:0.002, CH ₄: 0.015, C ₂H ₄: 0.002, C ₃H ₆: 0.001, C ₄H ₈: 0.001, C ₄H ₁₀: 0.001, C ₅H ₁₀: 0.001, C ₆H ₁₂: 0.001, ethanol: 0.001, acetone: 0.001, N ₂: 0.006.This stream thigh is as methanol feedstock air-flow thigh.

Methanol feedstock air-flow thigh 476 mixes with loop tail air-flow thigh 487 from gas-liquid separator, with enter fixed bed methanol sythesis reactor 489 after reactor outlet gas 488 heat exchange, at 5MPa pressure, it is synthetic to carry out methyl alcohol under 220 ℃ the temperature in, about 240 ℃ of temperature out, exit gas is cooled to 40 ℃ through reactor inlet preheater 490 and recirculated cooling water water cooler 491 two-stages, enter gas-liquid separator 492, isolate thick methyl alcohol stream thigh 493, flow is 47.68t/h, contains the water of 14.09wt%; Isolated tail gas stream thigh 494 flow 560882Nm ³/ h, wherein stream burst 495 circulations are 533616Nm ³/ h; Stream strand 496 flows are 27270Nm ³/ h all sends to vent gas treatment workshop section recover hydrogen.

The methyl alcohol synthesis tail gas consists of H ₂O:0.003, H ₂: 0.745, CO:0.067, CO ₂: 0.051, Ar:0.01, CH ₄: 0.065, C ₂H ₄: 0.006, C ₃H ₆: 0.004, C ₄H ₈: 0.001, C ₄H ₁₀: 0.001, C ₅H ₁₀: 0.001, C ₆H ₁₂: 0.001, methyl alcohol: 0.013, N ₂: 0.032.

The temperature of methanol sythesis reactor reclaims heat by feedwater, and by-product 2.5MPa, the steam 500 of 39t/h, the steam of by-product send to combined cycle power plant's generating.

Figure 14 is a vent gas treatment workshop section.Be divided into Fischer-Tropsch process exhaust processing and methanol-fueled exhaust and handle the two parts.

Fischer-Tropsch process exhaust stream thigh 498, enter dewatering unit 502 dehydrations, dehydration back stream strands 503 is cooled to about-40 ℃ through water cooler 504 and 505 two-stages, the above component of most C3 is cooled and gets off to become liquid in the tail gas, form gas-liquid mixed logistics 506, separate by gas-liquid separator 507, liquid portion 510 enters gas stripping column 512, emits as stream thigh 511 with most carbonic acid gas that nitrogen gas stream thigh 513 gas propose in the liquid; Its residual current thigh 514 is the lower carbon number hydrocarbons product, and 2.28t/h is arranged, as generating deposit raw material.

The stream thigh 509 of gas-liquid separator 507 top gas after interchanger 508 re-heats enters dehydrogenation unit 516 and goes recover hydrogen, obtains 99.5% hydrogen stream thigh, 475 about 48939Nm ³/ h sends to synthesizing section methanol sythesis reactor inlet compounding methanol synthetic gas.Isolate the tail gas 520 behind the hydrogen, about 47430Nm ³/ h, the workshop section that goes to generate electricity is as fuel gas generation.This tail gas consists of H ₂: 0.005, AR:0.008, N ₂: 0.022, CO:0.615, CO ₂: 0.282, CH ₄: 0.053, C ₂H ₄: 0.005, C ₂H ₆: 0.001, C ₃H ₆: 0.004, C ₃H ₈: 0.001, C ₄H ₈: 0.001, C ₄H ₁₀: 0.001, C ₅H ₁₀: 0.001.

Methanol-fueled exhaust stream thigh 496, flow is 27267Nm ³/ h sends to dehydrogenation unit 522 separating hydrogen gas, obtains 99.5% hydrogen stream thigh, 523 about 20211Nm ³/ h, this hydrogen stream stock is two portions, wherein stream thigh 524 is 16077Nm ³/ h is used for the hydrotreatment and the cracking of thick product, and stream thigh 525 is 4134Nm ³/ h is used for catalyst reduction.Isolate the tail gas 526 behind the hydrogen, about 7049Nm ³/ h goes to the workshop section that generates electricity.This tail gas consists of H ₂O:0.010; H ₂: 0.029; CO:0.254; CO ₂: 0.195; AR:0.037; CH ₄: 0.249; C ₂H ₄: 0.023; C ₂H ₆: 0.005; C ₃H ₆: 0.016; C ₃H ₈: 0.004; C ₄H ₈: 0.005; C ₄H ₁₀: 0.006; C ₅H ₁₀: 0.006; C ₅H ₁₂: 0.002; C ₆H ₁₂: 0.002; C ₆H ₁₄: 0.001; C ₇: 0.001; METHANOL:0.05, N ₂: 0.104.

The product deep processing workshop section of embodiment 3 is with flow process shown in the embodiment 1.Can produce diesel oil 78.80t/h altogether, petroleum naphtha 20.05t/h reclaims oxygenatedchemicals (based on alcohol) 6.29t/h such as alcohol, aldehyde, ketone, ester, ether, the return-air chemical industry section reuse after wastewater treatment of the 113.34t/h acid-bearing wastewater of generation; Reclaim refined methanol 39.19t/h, the 8.49t/h methanol waste water of generation is also return-air chemical industry section reuse after wastewater treatment.According to 8000 hours meters of year operation, can produce 790,000 tons of oil products and 310,000 tons of methyl alcohol altogether.

The generating workshop section flow process of embodiment 3 disposes as shown in figure 15, and this generating workshop section is similar to

embodiment

1,2, comprises steam-gas Combined circulating generation unit and steam-electric power unit.

The fuel gas stream thigh that combustion gas unit in the combined cycle generation unit uses comprises Fischer-Tropsch process exhaust stream strands 497, and Fischer-Tropsch process exhaust takes off behind lower carbon number hydrocarbons 520 and the hydrogen after the stream burst methyl alcohol synthesis tail gas dehydrogenation stream strands 526.The gas 540 that acts as a fuel after these three strands of gases mix enters the unitary internal combustion turbine 543 of gas-steam combined circulating generation after preheater 541 preheatings combustion chambers burn, the high-temperature high-pressure fuel gas that the combustion chamber produces drives generating set 544 works done generating.The high-temperature high-pressure fuel gas 545 of internal combustion turbine unit outlet enters waste heat boiler 546, and by-product goes out the high pressure superheated steam 547 of 6MPa, enters the steam turbine 548 of gas-steam combined Cycle Unit, drives generating set 549 works done generating.

The gas-steam combined circulating generation unit of configuration be configured to 2 150MW units, the electricity consumption every day underload period (22:00-6:00) is pressed 80% load operation, only use fuel gas generation, power generation capacity 240MW contains the oxygenatedchemicals of alcohol, aldehyde, ketone, ester, ether and lower carbon number hydrocarbons liquid fuel as deposit; The electricity consumption every day high loading period (6:00-22:00) then adopts gas and liquid fuel to mix as fuel used to generate electricity, the maximum 300MW that can generate electricity.And during synthesizing section start-stop car and during accidental state, can use the fuel generating that acts as a supplement of oil product that part stores and methyl alcohol.

In the steam-electric power unit, for steam and the heat that makes full use of the process by-product, the saturation steam of the synthetic by-product of the methyl alcohol 1.6MPaG that reduces pressure mixes with the saturation steam of the synthetic by-product of Fischer-Tropsch again, mixed vapour stream thigh 550 flows are 402t/h, after in preheater 551, being superheated to 280 ℃, enter the steam turbine generating set 552 of low-pressure steam generating set workshop section, drive generating set 553 generatings.The steam turbine generating set is configured to the unit of 2 30MW.

Foregoing has been described the preferred embodiments of the invention, but should be understood to also have many adjustable places, various factorss such as technology, total system material and the energy balance that these concrete selections of improving one's methods and synthetic gas gas making are adopted, the product structure of hope and composition are directly related, all should be in scope of the present invention.

Claims

1. one kind is the method for raw material coproducing oil product, methyl alcohol and electric energy with the carbon containing combustible solid, and this method realizes by following workshop section at least: gasification workshop section, synthesizing section, vent gas treatment workshop section, product deep processing workshop section and generating workshop section; Realize that this method may further comprise the steps at least:

(1) in gasification workshop section, carbon containing combustible solid raw material and oxygen-containing gas and vapor generation reaction generate crude synthesis gas, with all or part of carbonic acid gas that is converted into of carbon monoxide, all crude synthesis gas all go to next workshop section at least a portion crude synthesis gas after purifying treatment is removed desulfuration, moisture and most of carbonic acid gas by the water vapor transformationreation;

(2) synthesizing section comprises a Fischer-Tropsch synthesis device and a methanol sythesis reactor at least, and the unstripped gas of each reactor uses synthetic gas, or uses the tail gas of other reactor outlets, or uses the gas mixture of synthetic gas and tail gas;

(3) in the Fischer-Tropsch synthesis device of synthesizing section, unstripped gas reacts under the effect of catalyzer, reaction product obtains liquid hydrocarbon mixture, the reaction water that contains organic oxygen-containing compound and tail gas by follow-up cooling and separation circuit, a part of tail gas gas disposal workshop section that truncates;

(6) in product deep processing workshop section, synthesizing section, perhaps the liquid hydrocarbon mixture that obtains together of synthesizing section and vent gas treatment workshop section under catalyst action, mainly carries out the hydrogenation saturated reaction of alkene and the hydrogenation and removing of impurity, and is separated into processed oil;

(8) in product deep processing workshop section, the non-sour organic oxygen-containing compound of the reaction water Separation and Recovery that contains organic oxygen-containing compound alcohol, aldehyde, ketone, ester or ether wherein that is generated from synthesizing section Fischer-Tropsch synthesis device;

(9) generating workshop section comprises fuel gas-steam turbine combined cycle generation unit and steam turbine generation unit; The fuel used gas of fuel gas-steam turbine combined cycle generation unit is mainly the tail gas of each workshop section noted earlier, when peak of power consumption value and improper operating mode, makes the product of stand-by storage and the byproduct fuel that acts as a supplement; The steam turbine generation unit uses the steam of each workshop section's by-product noted earlier to drive generating.

2. according to claim 1 a kind of be the method for raw material coproducing oil product, methyl alcohol and electric energy with the carbon containing combustible solid, it is characterized in that, described carbon containing combustible solid is coal or refinery coke or the higher solid matter of other any combustible carbon content, or the combination of several materials.

3. according to claim 1 a kind of be the method for raw material coproducing oil product, methyl alcohol and electric energy with the carbon containing combustible solid, it is characterized in that described oxygen-containing gas is oxygen or air, perhaps other oxygen rich gass.

4. according to claim 1 a kind of be the method for raw material coproducing oil product, methyl alcohol and electric energy with the carbon containing combustible solid, it is characterized in that, the ratio of described synthetic gas conversion and not conversion, the degree of synthetic gas conversion depends on the proportion of production of required oil product, methyl alcohol and electric energy, and the combining and configuring of methanol sythesis reactor that is adopted and Fischer-Tropsch synthesis device.

5. according to claim 1 a kind of be the method for raw material coproducing oil product, methyl alcohol and electric energy with the carbon containing combustible solid, it is characterized in that, described Fischer-Tropsch synthesis device and methanol sythesis reactor are one or more levels series connection, adopt when multistage all or part of unstripped gas of the tail gas of previous stage as next stage.

6. according to claim 5 a kind of be the method for raw material coproducing oil product, methyl alcohol and electric energy with the carbon containing combustible solid, it is characterized in that, described one or more levels placed in-line Fischer-Tropsch synthesis device and methanol sythesis reactor, each grade is made up of the synthesis reactor of one or more parallel connections.

7. according to claim 1 a kind of be the method for raw material coproducing oil product, methyl alcohol and electric energy with the carbon containing combustible solid, it is characterized in that, the synthetic gas of described conversion and not conversion, be made into the mixed synthesis gas of definite composition according to the needs of different reactors at different levels, send to the inlet of each reactor.

8. according to claim 1 a kind of be the method for raw material coproducing oil product, methyl alcohol and electric energy with the carbon containing combustible solid, it is characterized in that, the gaseous fraction that described vent gas treatment workshop section reclaims comprises a part of hydrogen at least, reclaim wherein lower carbon number hydrocarbons and the required useful component of other production processes by deep cooling simultaneously.

9. according to claim 8 a kind of be the method for raw material coproducing oil product, methyl alcohol and electric energy with the carbon containing combustible solid, it is characterized in that, a part of hydrogen of described recovery according to the needs of different reactors at different levels as a supplement gas send to reactor inlet, to regulate the composition of inlet gas.

10. according to claim 8 a kind of be the method for raw material coproducing oil product, methyl alcohol and electric energy with the carbon containing combustible solid, it is characterized in that, described vent gas treatment workshop section, deep cooling reclaims the lower carbon number hydrocarbons component that obtains and sends to product deep processing workshop section production oil product as the part of liquid hydrocarbon mixture, perhaps continues to separate to produce various derived product.

11. according to claim 1 a kind of be the method for raw material coproducing oil product, methyl alcohol and electric energy with the carbon containing combustible solid, it is characterized in that described generating workshop section also uses a part of synthetic gas to generate electricity.

12. according to claim 1 a kind of be the method for raw material coproducing oil product, methyl alcohol and electric energy with the carbon containing combustible solid, it is characterized in that, all oil products and the organic oxygen-containing compound of described acquisition, all as the generating deposit fuel.

13. according to claim 1 a kind of be the method for raw material coproducing oil product, methyl alcohol and electric energy with the carbon containing combustible solid, it is characterized in that in the described purifying treatment, water need remove as far as possible, and removes CO ₂Amount depend on the requirement of methyl alcohol synthetic.