CN110129098A - It is a kind of to use the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages - Google Patents

It is a kind of to use the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages Download PDF

Info

Publication number
CN110129098A
CN110129098A CN201910451355.5A CN201910451355A CN110129098A CN 110129098 A CN110129098 A CN 110129098A CN 201910451355 A CN201910451355 A CN 201910451355A CN 110129098 A CN110129098 A CN 110129098A
Authority
CN
China
Prior art keywords
feedstock hydrocarbon
runner
hydrocarbon
flow
feedstock
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
CN201910451355.5A
Other languages
Chinese (zh)
Inventor
罗进成
朱春鹏
徐宏伟
韦孙昌
贺根良
赵蒙
曾梅
林益安
郑亚兰
杨云龙
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Northwest Chemical Research Institute Co Ltd
Original Assignee
Northwest Chemical Research Institute Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Northwest Chemical Research Institute Co Ltd filed Critical Northwest Chemical Research Institute Co Ltd
Priority to CN201910451355.5A priority Critical patent/CN110129098A/en
Publication of CN110129098A publication Critical patent/CN110129098A/en
Pending legal-status Critical Current

Links

Classifications

    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/001Processes for the treatment of water whereby the filtration technique is of importance
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/02Treatment of water, waste water, or sewage by heating
    • C02F1/04Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/048Purification of waste water by evaporation
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/02Treatment of water, waste water, or sewage by heating
    • C02F1/04Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/06Flash evaporation
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46Gasification of granular or pulverulent flues in suspension
    • C10J3/466Entrained flow processes
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46Gasification of granular or pulverulent flues in suspension
    • C10J3/48Apparatus; Plants
    • C10J3/50Fuel charging devices
    • C10J3/506Fuel charging devices for entrained flow gasifiers
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72Other features
    • C10J3/82Gas withdrawal means
    • C10J3/84Gas withdrawal means with means for removing dust or tar from the gas
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02Processes for making hydrogen or synthesis gas
    • C01B2203/0205Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0211Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step
    • C01B2203/0216Processes for making hydrogen or synthesis gas containing a reforming step containing a non-catalytic reforming step containing a non-catalytic steam reforming step
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0415Purification by absorption in liquids
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205Composition of the feed
    • C01B2203/1211Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235Hydrocarbons
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205Composition of the feed
    • C01B2203/1211Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235Hydrocarbons
    • C01B2203/1241Natural gas or methane
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/18Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00Details of gasification apparatus
    • C10J2200/15Details of feeding means
    • C10J2200/152Nozzles or lances for introducing gas, liquids or suspensions
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903Feed preparation
    • C10J2300/0906Physical processes, e.g. shredding, comminuting, chopping, sorting
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913Carbonaceous raw material
    • C10J2300/093Coal
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953Gasifying agents
    • C10J2300/0959Oxygen
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953Gasifying agents
    • C10J2300/0973Water
    • C10J2300/0976Water as steam
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/16Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603Integration of gasification processes with another plant or parts within the plant with gas treatment
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/16Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1615Stripping
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/16Integration of gasification processes with another plant or parts within the plant
    • C10J2300/169Integration of gasification processes with another plant or parts within the plant with water treatments

Abstract

The one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages is used the invention discloses a kind of, which, which includes: one, solid block is contained to feedstock hydrocarbon is made powder or slurry;Two, the gentle agent of feedstock hydrocarbon will be contained and pass through hybrid reaction generation raw gas in the one-jet runner containing feedstock hydrocarbon of overhead multiple flow passages and gasifying agent runner feeding reactor respectively;Three, washing after rough coal air cooling is removed in raw gas and is mingled with to obtain raw gas;Four, Heisui River that cooling and washing generates successively is concentrated, is filtered and heat recovery obtains buck.The present invention is fed by the one-jet runner containing feedstock hydrocarbon of overhead multiple flow passages and gasifying agent runner, realize the charging of variform, type containing feedstock hydrocarbon, to which a variety of sufficiently gasify simultaneously containing feedstock hydrocarbon is converted to raw gas, improve the quality of raw gas product, gasification process is expanded to the adaptation range of raw material, gasification efficiency is improved, equipment and operating cost are reduced, ensure that the safety of gasification process.

Description

It is a kind of to use the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages
Technical field
The invention belongs to the fields of gasification technology containing feedstock hydrocarbon, and in particular to a kind of one-jet using overhead multiple flow passages Gasification process containing feedstock hydrocarbon.
Background technique
Entrained flow bed gasification technology is one of clean coal technology relatively advanced at present, and the technology is mostly using coal as material synthesis gas Change product, then further production synthesizes the basic chemicals such as ammonia, methanol, natural gas, fuel oil, has obtained at home extensive Using.In recent years, as demand of the market to gasification product increases, the air flow bed that high throughput is badly in need of in energy processing enterprise is set It is standby, to improve the production efficiency of gasification product.The most widely used air-flow bed apparatus is single injector overhead in enterprise at present Formula air flow bed, maximum throughput are 2000t/ days, and treating capacity is limited, strongly limits the exploitation of clean product of coal.
In addition, the diversity of gasified raw material is also one of the problem that entrained flow bed gasification technology needs to solve.Since gasification is former The otherness for expecting self property is blended in the case that especially material state is different in a variety of gasified raw materials and is difficult to realize a variety of originals Gasify trans-utilization while material;And when containing imflammable gas in gasified raw material, the gasification such as imflammable gas and oxygen Agent is easy to produce danger when mixing.Therefore, it is necessary to which developing one kind is suitable for a variety of different gasified raw materials in a reactor The technique of gasification simultaneously realizes the effect for reducing equipment and operating cost while improving product property.
Summary of the invention
Technical problem to be solved by the present invention lies in view of the above shortcomings of the prior art, provide a kind of use above to set The one-jet gasification process containing feedstock hydrocarbon of formula multiple flow passages.The technique contains hydrocarbon feedstream by the way that overhead multiple flow passages are one-jet Road and the charging of gasifying agent runner, realize one or more same forms, charging of the variety classes containing feedstock hydrocarbon, and a kind of Or charging of a variety of different conditions containing feedstock hydrocarbon, so that a variety of sufficiently gasify simultaneously containing feedstock hydrocarbon is converted to raw gas, The quality for improving raw gas product, expands gasification process to the adaptation range of raw material, while improving gasification efficiency, reduces Equipment and operating cost avoid when gaseous state is mixed containing feedstock hydrocarbon with gasifying agent and generate danger, ensure that the peace of gasification process Quan Xing.
In order to solve the above technical problems, the technical solution adopted by the present invention is that: it is a kind of to use overhead multiple flow passages single injector Gasification process containing feedstock hydrocarbon, which is characterized in that the technique the following steps are included:
Step 1: solid block pre-treatment containing feedstock hydrocarbon: solid block being contained feedstock hydrocarbon system using dry grinding method Slurry is made containing feedstock hydrocarbon in solid block at powder, or using wet grinding method;
Step 2: material gasification: containing the gentle agent of feedstock hydrocarbon, to pass through overhead multiple flow passages respectively one-jet carbon containing Hydrogen feedstock runner and gasifying agent runner, which are sent into reactor, to be mixed, and then reaction is generated containing the raw gas being mingled with;It is described carbon containing Hydrogen feedstock is that gaseous state contains feedstock hydrocarbon, liquid containing one or both of powder or slurry obtained in feedstock hydrocarbon, step 1 More than;The main component of the high temperature rough gas is CO and H2;It is described that be mingled be completely organic containing unreacted in feedstock hydrocarbon Object and mixture containing the inorganic substances contained in feedstock hydrocarbon;
Step 3: product purifies: being water-cooled what is generated in step 2 containing the raw gas being mingled with, then pass through washing Being mingled in raw gas is washed away, raw gas is obtained;
Step 4: usage on black water: the cooling water containing ash and water washing process that the cooling procedure as described in step 3 is generated The Heisui River of the composition containing grey washing water of middle generation is successively concentrated, is filtered and heat recovery, and buck, part of buck are obtained As waste water outlet, remaining buck is after heat recovery for the water washing in step 3.
Gasification process containing feedstock hydrocarbon of the invention is broadly divided into raw material pre-treatment workshop section, material gasification and product purification work Section and usage on black water workshop section.Of the invention is that gaseous state contains feedstock hydrocarbon (such as natural gas), liquid contains hydrocarbon original containing feedstock hydrocarbon Expect (such as residual oil, highly concentrated organic liquor) and solid block (such as coal, petroleum coke, active carbon, coke, coke blacking) containing feedstock hydrocarbon One or more of, since solid block is not easy to feed containing feedstock hydrocarbon, need to carry out pre-treatment before use, using dry method Polishing or wet grinding method are made into powder or slurry, wherein contain feedstock hydrocarbon to solid block during wet grinding method Quality is prepared as pulping water in middle addition water or/and aqueous solution containing hydrocarbon substance, preferably waste water of the addition containing hydrocarbon substance The slurry that percentage is 55%~70%, then containing the gentle agent of feedstock hydrocarbon, to pass through overhead multiple flow passages respectively one-jet Runner containing feedstock hydrocarbon and gasifying agent runner, which are sent into reactor, to be mixed, and it is placed in the middle which is placed in gasification reactor top Position, CO and H are thought in each storeroom generation in gasification reactor2Based on containing the raw gas being mingled with, then through cooling and water Washing slagging-off, obtains clean raw gas, while cooling water and wash water being recycled.
The present invention is fed by the one-jet runner containing feedstock hydrocarbon of overhead multiple flow passages and gasifying agent runner, due to above setting Formula multiple flow passages single injector is designed using multiple flow passages, is increased the runner quantity being sent into reactor containing feedstock hydrocarbon, is realized one Kind or a variety of same forms, variety classes contain the charging of feedstock hydrocarbon (such as coal, petroleum coke, coke breeze, organic solid waste), with And one or more different conditions contain the charging of feedstock hydrocarbon (such as coal, natural gas, mink cell focus), to realize a variety of contain Sufficiently gasify while feedstock hydrocarbon and then be converted to raw gas, improves the H/C atomic ratio of raw gas product, expand gasification work Skill improves gasification efficiency to the adaptation range of raw material, reduces equipment and operating cost;In addition, gasification of the invention Technique will contain the gentle agent of feedstock hydrocarbon and separately feed, and avoid containing production when imflammable gas is mixed with gasifying agent in feedstock hydrocarbon It is raw dangerous, it ensure that the safety of gasification process.
Above-mentioned is a kind of using the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages, which is characterized in that step Gasifying agent described in two is high purity oxygen gas, and the bulk purity of the high purity oxygen gas is 90%~99.8%.Above-mentioned high purity oxygen gas is The common oxidant of gasification process containing feedstock hydrocarbon can adapt to most of gasifications containing feedstock hydrocarbon, and use scope is wide, and makes It is more convenient with being adjusted with flow.
Above-mentioned is a kind of using the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages, which is characterized in that step The single injector of overhead multiple flow passages described in two has multiple flow passages structure, and the quantity of runner is 3+2n in the multiple flow passages structure, Middle n is the positive integer not less than 1, and the center flow channels in the multiple flow passages structure are gasifying agent runner, and outside from center flow channels Successively successively it is arranged alternately according to the sequence of runner containing feedstock hydrocarbon, gasifying agent runner.Overhead multiple flow passages single spraying of the invention Multiple runners are provided in mouth, the runner is divided into runner containing feedstock hydrocarbon and gasifying agent runner, and center flow channels are gasifying agent stream Road, and be successively successively arranged alternately according to the sequence of runner containing feedstock hydrocarbon, gasifying agent runner outward from center flow channels, therefore from What respectively runner containing feedstock hydrocarbon was independently sent into is being located at instead containing feedstock hydrocarbon and the gasifying agent being independently sent into from each gasifying agent runner It answers and carries out being mixed and fed into reactor at the one-jet head outlet of overhead multiple flow passages at the top of device, to increase into anti- The contact area containing feedstock hydrocarbon and gasifying agent in device is answered, is conducive to contain feedstock hydrocarbon and the abundant gasification reaction of gasifying agent, into One step improves gasification efficiency, while improving the charging ability of the gentle agent containing feedstock hydrocarbon.
Above-mentioned is a kind of using the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages, which is characterized in that uses Feedstock hydrocarbon pressurized equipment will contain feedstock hydrocarbon and be placed in gasification reactor top by mutually independent pipeline containing feedstock hydrocarbon feeding In a multiple flow passages nozzle for holding middle position;The feedstock hydrocarbon pressurized equipment is double acting feedstock hydrocarbon force (forcing) pump and nonoculture With feedstock hydrocarbon force (forcing) pump or double acting feedstock hydrocarbon force (forcing) pump.Feedstock hydrocarbon pressurization will be contained using feedstock hydrocarbon force (forcing) pump Nozzle is sent by independent respectively runner containing feedstock hydrocarbon afterwards and flow to the exit of nozzle, and passes through independent each gasifying agent stream Road enter nozzle and flow to the exit of nozzle gasifying agent carry out physics by force mix and realized in a manner of injection containing feedstock hydrocarbon It being sufficiently mixed and being atomized with gasifying agent, further increasing the contact area containing feedstock hydrocarbon and gasifying agent, be conducive to carbon containing The abundant gasification of hydrogen feedstock and gasifying agent, improves gasification efficiency.
Above-mentioned is a kind of using the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages, which is characterized in that described Double acting feedstock hydrocarbon force (forcing) pump be reciprocating double-action diaphragm pump, the reciprocating double-action diaphragm pump by adjust two sides every Membrane cavity will be delivered to two different runners containing feedstock hydrocarbon containing feedstock hydrocarbon, in described two different runners containing feedstock hydrocarbon Flow ratio containing feedstock hydrocarbon is 1~2, and the double acting feedstock hydrocarbon pump while conveying or stopping conveying containing feedstock hydrocarbon. Relative to single-acting force (forcing) pump, power consumption is not only saved using reciprocating double-action diaphragm pump, while ensure that force (forcing) pump Material when malfunction in two different runners containing feedstock hydrocarbon is able to maintain synchronous stopping, avoiding because of gasifying agent in short-term Between flow it is exceeded and cause safety accident.Flow ratio containing feedstock hydrocarbon in preferred two different runners containing feedstock hydrocarbon It is 1~2 and adjustable, preferably maintains overhead multiple flow passages single injector and processed to the atomizing effect of material and convenient for nozzle, together When by adjust two different runners containing feedstock hydrocarbon in the flow ratio containing feedstock hydrocarbon, improve including overhead multithread Gasification installation including road single injector ensure that gasification installation is containing for the use ability of the supply disequilibrium containing feedstock hydrocarbon Feedstock hydrocarbon can also operate normally when supplying fluctuating change.And double acting feedstock hydrocarbon pump while conveying or stopping conveying are containing hydrocarbon The function of raw material is avoided using complex facilities such as interlocks, and the problems such as be not in signal relative delay, so that gasification The safety of device operation greatly improves.
Above-mentioned is a kind of using the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages, which is characterized in that step The flow proportional range of the gentle agent containing feedstock hydrocarbon described in two is 0.001~0.003, when the gentle agent containing feedstock hydrocarbon Flow proportional carries out protection cutting when deviateing the range, stop the feeding of the gentle agent containing feedstock hydrocarbon.Preferably contain hydrocarbon original The flow proportional range of material and gasifying agent, which ensure that, to be able to maintain that containing reacting between feedstock hydrocarbon and gasifying agent comparatively ideal Under state, to improving the mass transitions rate of raw material to 96% or more;When the flow proportional of the gentle agent containing feedstock hydrocarbon is inclined Protection cutting is carried out when from the range, is stopped the feeding of the gentle agent containing feedstock hydrocarbon, is avoided entering gas because of any material excess Change reactor and causes safety accident.
Above-mentioned is a kind of using the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages, which is characterized in that step Two is described containing gaseous state when containing feedstock hydrocarbon is contained in feedstock hydrocarbon, and the gaseous state can be sent into containing feedstock hydrocarbon by gasifying agent runner In reactor.Since gaseous state is identical as the state of gasifying agent containing feedstock hydrocarbon, when intake of the gaseous state containing feedstock hydrocarbon compared with When big, gaseous state can be sent into reactor containing feedstock hydrocarbon by gasifying agent channel, improve charging of the gaseous state containing feedstock hydrocarbon Rate promotes gaseous state coming into full contact with containing feedstock hydrocarbon and gasifying agent, is conducive to gaseous state filling containing feedstock hydrocarbon and gasifying agent Divide gasification reaction.
Above-mentioned is a kind of using the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages, which is characterized in that described During being sent into reactor by overhead multiple flow passages nozzle containing the gentle agent of feedstock hydrocarbon, what is be not used by contains feedstock hydrocarbon Inert gas is filled in runner and gasifying agent runner, and inert gas is flowed to reactor direction.Gentle containing feedstock hydrocarbon During agent is sent into reactor by overhead multiple flow passages nozzle, when containing in a certain or certain several carbon containing hydrogen feedstock channel Feedstock hydrocarbon occurs that supply is insufficient or produce load needs lower timing, can stop being passed through to corresponding runner containing feedstock hydrocarbon and contains Feedstock hydrocarbon, in order to protect multiple flow passages nozzle, on the feeding line for accessing each gentle agent runner of feedstock hydrocarbon runner Configured with high-pressure inert gas access device, it is passed through in the runner containing feedstock hydrocarbon containing feedstock hydrocarbon to stopping and conveys inert gas To maintain the positive pressure in the runner, to prevent backflowing containing feedstock hydrocarbon or raw gas and causing to spray in nozzle head or reactor The damage of mouth.
Above-mentioned is a kind of using the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages, which is characterized in that step The detailed process of heat recovery described in four are as follows: filtered Heisui River is subjected to vacuum flashing, the water formation in Heisui River is dodged By flash steam, water washing is exchanged heat with water in a manner of direct contact heat transfer and described in step 3 after steam.The heat Way of recycling avoids the problem of gasification process in the prior art is easily blocked using heat exchanger caused by indirect heat exchange, easily revealed, The rate of recovery that is energy-efficient and improving heat.
Compared with the prior art, the present invention has the following advantages:
1, the present invention is fed by the one-jet runner containing feedstock hydrocarbon of overhead multiple flow passages and gasifying agent runner, due to upper It sets formula multiple flow passages single injector to design using multiple flow passages, increases the runner quantity being sent into reactor containing feedstock hydrocarbon, realize One or more same forms, variety classes contain the charging of feedstock hydrocarbon (such as coal, petroleum coke, coke breeze, organic solid waste), And one or more different conditions contain the charging of feedstock hydrocarbon (such as coal, natural gas, mink cell focus), to realize a variety of While containing feedstock hydrocarbon, which sufficiently gasifies, is converted to raw gas, improves the quality of raw gas product, expands gasification process to original The adaptation range of material, while gasification efficiency is improved, reduce equipment and operating cost;In addition, gasification process of the invention will Gaseous state gentle agent containing feedstock hydrocarbon is separately fed, and is avoided and is generated dangerous, guarantor when gaseous state is mixed containing feedstock hydrocarbon with gasifying agent The safety of gasification process is demonstrate,proved.
2, it is one-jet containing hydrocarbon feedstream by overhead multiple flow passages will to contain the gentle agent of feedstock hydrocarbon respectively by the present invention Road and the charging of gasifying agent runner, are designed using the one-jet multiple flow passages of overhead multiple flow passages, improve gentleization containing feedstock hydrocarbon The charging ability of agent solves traditional handicraft after inlet amount increase because equipment attrition, stock dispersion variation can not be normal The problem of production;In addition, due to the center flow channels in overhead multiple flow passages single injector be gasifying agent runner, and from center flow channels to It is successively successively arranged alternately, increases into containing in reactor according to the sequence of runner containing feedstock hydrocarbon, gasifying agent runner outside The contact area of feedstock hydrocarbon and gasifying agent, to be conducive to further mention containing feedstock hydrocarbon and the abundant gasification reaction of gasifying agent High gasification efficiency;In addition, the design that center flow channels are gasifying agent runner can also make operator by simply adjusting in this The heart runner gasification agent flux mode control containing feedstock hydrocarbon by after materialization shape and atomization center with a distance from nozzle head, Facilitate production.
3, it is one-jet containing hydrocarbon feedstream by overhead multiple flow passages will to contain the gentle agent of feedstock hydrocarbon respectively by the present invention Road and the charging of gasifying agent runner can be according to practical need due to mutually independent between runner containing feedstock hydrocarbon and gasifying agent runner Feed loading, operation side are adjusted by the quantity of the runner containing feedstock hydrocarbon and gasifying agent runner that increase or decrease charging Just, the adjustable range of feed loading is relatively wide and adjusts accurately and timely, is conducive to going on smoothly for gasification reaction.
4, the present invention on feed-stock pipeline containing feedstock hydrocarbon and gasifying agent snorkel line by being arranged flow detection controller With flow control valve, and it is connected with overall operational device, containing for the one-jet runner containing feedstock hydrocarbon of overhead multiple flow passages will be entered After feedstock hydrocarbon total flow carries out summation conversion with volume calorific value, the flow with the gasifying agent for being passed through gasifying agent runner is according to certain Control is adjusted in volume ratio, and can carry out protection cutting simultaneously, to ensure that the gasification of the gentle agent containing feedstock hydrocarbon Being normally carried out for reaction, avoids the waste containing feedstock hydrocarbon or gasifying agent, further improves the efficiency and peace of gasification reaction Quan Xing, process is simple, control require it is lower, it is easy to operate.
5, the present invention on feed-stock pipeline containing feedstock hydrocarbon and gasifying agent snorkel line by being arranged flow detection controller With flow control valve, and it is connected with overall operational device, containing for the one-jet runner containing feedstock hydrocarbon of overhead multiple flow passages will be entered After feedstock hydrocarbon total flow carries out summation conversion with volume calorific value, the flow with the gasifying agent for being passed through gasifying agent runner is according to certain Control is adjusted in volume ratio, can include feedstock hydrocarbon or gas according to runners one or more in overhead multiple flow passages single injector The other runners of changes in flow rate adjust automatically of agent include the flow of feedstock hydrocarbon or gasifying agent, convenient in time, avoid flow The hysteresis quality of adjusting further ensures going on smoothly for gasification reaction, reduces security risks caused by Feedstock fluctuation.
6, the present invention makes the flash steam of Heisui River formation and being exchanged heat with water for water washing using direct contact heat transfer, keeps away Exempted from the problem of gasification process in the prior art easily block using heat exchanger caused by indirect heat exchange, easily revealed, it is energy-efficient and Improve the rate of recovery of heat.
Technical solution of the present invention is described in further detail below by drawings and examples.
Detailed description of the invention
Fig. 1 is process flow chart of the invention.
Fig. 2 is the one-jet structural schematic diagram of overhead multiple flow passages that the present invention uses.
Fig. 3 is the structural schematic diagram for the double acting feedstock hydrocarbon pressurized equipment that the present invention uses.Description of symbols:
1-wet lapping equipment;2-raw material slurry storage tanks;
4-dry powder raw material storage tanks;5-gasification reactors;
5-gasification reactors;6-gas coolers;
7-thick slag discharge systems;8-raw gas washing, purifying devices;
9-buck inspissators;10-dope filters;
11-grey water heaters;12-condensers;
13-grey water collectors;14-the first gasifying agent runner;
15-the first runner containing feedstock hydrocarbon;16-the second gasifying agent runner;
17-the second runner containing feedstock hydrocarbon;18-third gasifying agent runners;
19-third runners containing feedstock hydrocarbon;20-the four gasifying agent runner;
21-water leg chambers;22-water inlets;
23-water outlets;24-the first gasifying agent interface;
25-the first interface containing feedstock hydrocarbon;26-the second gasifying agent interface;
27-the second interface containing feedstock hydrocarbon;28-third gasifying agent interfaces;
29-third interfaces containing feedstock hydrocarbon;30-the four gasifying agent interface;
31-driving wheels;32-proportion adjustment wheels;
33-First piston bars;34-first pistons;
35-first piston cavitys;36-first shells;
37-the first inlet check valve;38-the first diaphragm;
39-the first diaphragm cavity;40-the second diaphragm;
41-first fluid pressurizing chambers;42-first outlet check-valves;
43-second piston bars;44-second pistons;
45-second piston cavitys;46-second shells;
47-the second inlet check valve;48-third diaphragms;
49-the second diaphragm cavity;50-the four diaphragm;
51-second fluid pressurizing chambers;52-second outlet check-valves.
Specific embodiment
As shown in Figure 1, gasification process containing feedstock hydrocarbon of the invention is broadly divided into raw material pre-treatment workshop section I, material gasification And product purification section II and usage on black water workshop section III, of the invention is gaseous state (such as natural gas containing feedstock hydrocarbon containing feedstock hydrocarbon Deng), liquid contain feedstock hydrocarbon (such as residual oil, highly concentrated organic liquor) and solid block (such as coal, petroleum coke, activity containing feedstock hydrocarbon One or more of charcoal, coke, coke blacking etc.), it is handled in workshop section I before raw material, since solid block contains hydrocarbon original Material is not easy to feed, and needs to carry out pre-treatment before use: solid block is pressed containing feedstock hydrocarbon with water or/and aqueous solution containing hydrocarbon substance Ratio is sent into wet lapping equipment 1, and the slurry containing feedstock hydrocarbon that mass percent is 55%~70% is made and is stored in original In slurry body storage tank 2;Or solid block is entered in dry grinding equipment 3 together with inertia high temperature drying gas containing feedstock hydrocarbon It obtains powder containing feedstock hydrocarbon and is stored in dry powder raw material storage tank 4, used for subsequent gasification.
In material gasification and product purification section II, by slurry containing feedstock hydrocarbon obtained in raw material pre-treatment workshop section I Or powder containing feedstock hydrocarbon and gaseous state pass through containing one or more of feedstock hydrocarbon containing hydrocarbon containing feedstock hydrocarbon, liquid After raw material pressurized equipment P1 pressurization, gasification reactor is sent by the one-jet runner containing feedstock hydrocarbon of an overhead multiple flow passages In 5, while gasifying agent being sent into gasification reactor 5 by the one-jet gasifying agent runner of overhead multiple flow passages, passes through physics The mode of strong mixed injection realizes being sufficiently mixed and being atomized containing feedstock hydrocarbon and gasifying agent, and overhead multiple flow passages single injector is placed in Place placed in the middle right above gasification reactor.The gentle agent containing feedstock hydrocarbon enters after gasification reactor 5 to be occurred instead under the high temperature conditions It should generate with CO+H2Based on raw gas.When in a certain runner containing feedstock hydrocarbon containing feedstock hydrocarbon occur supply it is insufficient or When needing to lower produce load, it can stop being passed through into the runner containing feedstock hydrocarbon containing feedstock hydrocarbon, and by being arranged carbon containing High pressure nitrogen access device on the feed-stock pipeline of hydrogen feedstock runner is to the supplying nitrogen of runner containing feedstock hydrocarbon to maintain this to contain Positive pressure in runner containing feedstock hydrocarbon, the damage of nozzle caused by avoiding the high temperature rough gas generated in gasification reactor 5 from backflowing.Separately Outside, when using containing feedstock hydrocarbon as the gaseous states such as natural gas, coke-stove gas when containing feedstock hydrocarbon, sending for gasifying agent runner can be closed Valve X2 on gas pipeline and overhead multiple flow passages single injector gasifying agent, the pipeline of supplying gas for opening the gasifying agent runner contain with gaseous state Gaseous state is sent into gasification reactor by the gasifying agent runner containing feedstock hydrocarbon by the valve X1 connected on feedstock hydrocarbon feed-stock pipeline Gasify in 5, to improve feed rate, and then improves gasification efficiency.
The effect of the P1 of pressurized equipment containing feedstock hydrocarbon is after containing feedstock hydrocarbon pressurization by overhead multiple flow passages single injector Runner containing feedstock hydrocarbon be sent into gasification reactor 5 in, the quantity of runner in the one-jet multiple flow passages structure of overhead multiple flow passages For 3+2n, wherein n is the positive integer not less than 1, then the number of units of the P1 of pressurized equipment containing feedstock hydrocarbon is n platform, and wherein n is preferably 1 Or 2.As n=1, the quantity of runner is 5 in the one-jet multiple flow passages structure of overhead multiple flow passages, the runner containing feedstock hydrocarbon Quantity is 2,1 double acting force (forcing) pump containing feedstock hydrocarbon is arranged as pressurized equipment containing feedstock hydrocarbon, the double acting is containing hydrocarbon Two material outlets of raw material force (forcing) pump will contain feedstock hydrocarbon and be delivered to 2 runners containing feedstock hydrocarbon respectively by feed-stock pipeline In;As n=2, the quantity of runner is 7 in the one-jet multiple flow passages structure of overhead multiple flow passages, the runner containing feedstock hydrocarbon Quantity is 3, and 1 double acting force (forcing) pump containing feedstock hydrocarbon is arranged and 1 single-acting force (forcing) pump containing feedstock hydrocarbon is used as containing hydrocarbon Raw material pressurized equipment, the 1 of two material outlet and the single-acting force (forcing) pumps containing feedstock hydrocarbon of double acting force (forcing) pump containing feedstock hydrocarbon A material outlet will contain feedstock hydrocarbon and will be delivered in 3 runners containing feedstock hydrocarbon respectively by feed-stock pipeline.
Corresponding flow detection controller is mounted on the pipeline of supplying gas of feed-stock pipeline and gasifying agent containing feedstock hydrocarbon 2) and flow control valve (is respectively labeled as V1~V3+2m, m=1 or 2), and flow (it is respectively labeled as F1~F3+2m, m=1 or It detects controller and flow control valve corresponds, the quantity of flow monitoring controller, the quantity of flow control valve and overhead Runner quantity is consistent in multiple flow passages single injector, is controlled by the circuit between each flow detection controller and corresponding each flow control valve System adjusts the flow of gasifying agent in flow and pipeline of respectively supplying gas in each feed-stock pipeline containing feedstock hydrocarbon.In Fig. 1 by taking m=1 as an example, Be separately installed on the feed-stock pipeline of two solid carbon-contg hydrogen feedstocks flow monitoring controller F1 and corresponding flow control valve V1, Flow monitoring controller F2 and corresponding flow control valve V2, liquid are equipped with flow monitoring on the feed-stock pipeline containing feedstock hydrocarbon Controller F3 and corresponding flow control valve V3, gaseous state are equipped with flow monitoring controller F4 on the feed-stock pipeline containing feedstock hydrocarbon And corresponding flow control valve V4, flow monitoring controller F5 is installed on the pipeline of supplying gas of gasifying agent and corresponding flow is adjusted Valve V5, flow detection controller F1~F5 are connected with overall operational device Y1.When each stream on respectively feed-stock pipeline containing feedstock hydrocarbon The data of real-time traffic containing feedstock hydrocarbon that amount detection controller F1~F4 will test are transferred to overall fortune in electrical signal form Device Y1 is calculated, overall operational device Y1 is by the real-time traffic data in feed-stock pipeline by the heat in respectively runner containing feedstock hydrocarbon with body Accumulated heat value carries out summation conversion, then according to the corresponding relationship of the volume calorific value that pre-sets and gasifying agent flow ratio, with Each flow detection controller F5 of each gasifying agent to supply gas on pipeline detect and be sent to overall operational device Y1 gasifying agent it is real-time Data on flows compares and feedback regulation, so that gasification agent flux is adjusted to appropriate value, to will be fed into gasification reactor 5 The flow and gasifying agent containing feedstock hydrocarbon flow control in a certain proportion.When in feeding gasification reactor 5 When the flow of flow and gasifying agent containing feedstock hydrocarbon deviates the proportional region, automatic trigger protective device carries out protection cutting, The feeding for stopping the gentle agent containing feedstock hydrocarbon, to stop entire gasification process.
Carry out gasification reaction in gasification reactor 5 containing feedstock hydrocarbon and gasifying agent, generation with CO+H2Based on raw gas The inanimate matter ash for carrying molten state enter in the gas-guide tube of rough coal Gas Cooler 6 and come into full contact with its internal water carry out it is cold But, raw gas and inanimate matter ash are obtained, wherein inanimate matter ash settles into rough coal Gas Cooler 6 under gravity In the cooling water of bottom, the lime-ash of cooling water lower part deposition is discharged by ash discharge technique through thick slag discharge system 7, and middle and upper part is cooling Water because after (180 DEG C~300 DEG C) of the Heisui River discharge rough coal Gas Cooler 6 containing tiny ash content into wastewater treatment working section III into Row is further processed;Raw gas is separated from water because solubility in water is lower, is turned back and is risen to the top of rough coal Gas Cooler 6 Portion is discharged from outlet, is further washed subsequently into raw gas washing, purifying device 8, in raw gas washing, purifying device 8, is taken Raw gas with tiny ash is in contact with the return buck from waste water water treatment system (III), is washed by intrusive water-bath It washs and washs the mode combined with rising contact column plate, remove the tiny ash carried in raw gas, obtain clean up to standard Raw gas and washing Heisui River (150 DEG C~280 DEG C) containing fine ash, raw gas are discharged from the top of raw gas washing, purifying device 8 And be sent into downstream section as the final products of this gasification process and utilized, the washing Heisui River (150 DEG C~280 containing fine ash DEG C) after the bottom of raw gas washing, purifying device 8 is collected, a part send the cooling to gas cooler 6 as high temperature rough gas Water uses, and another part send to subsequent grey water treatment system (III) and is further processed.
In wastewater treatment working section III, in rough coal Gas Cooler 6 containing tiny ash content Heisui River (180 DEG C~300 DEG C) and (150 DEG C~280 DEG C) of the washing Heisui River containing fine ash in raw gas washing, purifying device 8, which enters in buck inspissator 9, to be subtracted Pressure flash distillation, moisture vaporization forms (130 DEG C~220 DEG C) of flash steam separation and is discharged from the top of buck inspissator 9, into buck In heater 11, remaining unvaporized liquid and fine ash are discharged from the bottom of buck inspissator 9, carry out into dope filter 10 Filtering, obtains fine ash and buck, fine ash (water content is 40wt%~60wt%, and temperature is 50 DEG C~80 DEG C) be accumulated as fine slag from The bottom of dope filter 10 is discharged, and (dust burdening enters in grey water collector 13 buck in 5wt% or less), removes least a portion of ash Water is sent to formation outlet water outside gasification process section to reduce accumulation of the salinity in water body, most buck (80 DEG C~110 DEG C) give into grey water heater 11.
After moisture vaporization is formed in buck inspissator 9 (130 DEG C~220 DEG C) of flash steam enter in grey water heater 11, Heat is carried out in a manner of directly mixing with the buck (80 DEG C~110 DEG C) being delivered in grey water heater 11 by grey water collector 13 Amount exchange, buck are discharged after being heated to 90 DEG C~160 DEG C by the bottom of grey water heater 11, are back to material gasification and product It is utilized in raw gas washing, purifying device 8 in purification section II as return buck, to the raw gas for carrying tiny ash It is washed;Remaining uncooled flash steam (100 DEG C~160 DEG C) is set in grey water heater 11 in grey water heater 11 After the washing purifying device effect of inner upper end, exports and sent to condenser 12 from the top of grey water heater 11, be condensed into liquid The laggard ash charge water collector 13 of state is recycled.Due in grey water heater 11 flash steam (130 DEG C~220 DEG C) directly to connect The mode of touch heat exchange and (80 DEG C~110 DEG C) of buck heat exchange, return again into material gasification and product purification section II, and Washing purifying device is set in grey water heater 11, relative to the method for existing indirect type buck heat exchange, is avoided in steam Indirect type ash water- to-water heat exchanger caused by due to carrying fine ash blocking and thus caused by heat exchange efficiency it is low the problems such as, equipment therefore Barrier rate is low, safe and efficient.
As shown in Fig. 2, the overhead multiple flow passages single injector of the embodiment of the present invention 4 and embodiment 6 all has 7 flow passage structures, The quantity of runner is 7 in 7 flow passage structure, and the center flow channels in 7 flow passage structure are the first gasifying agent runner 14, and It is followed successively by the first runner containing feedstock hydrocarbon 15, the second gasifying agent runner 16, second outward containing hydrocarbon from the first gasifying agent runner 14 Raw material runner 17, third gasifying agent runner 18, third runner containing feedstock hydrocarbon 19 and the 4th gasifying agent runner 20, described first contains Feedstock hydrocarbon runner 15, the second runner containing feedstock hydrocarbon 17, third runner containing feedstock hydrocarbon 19 inlet respectively correspond setting There are the first interface containing feedstock hydrocarbon 25, the second interface containing feedstock hydrocarbon 27 and third interface containing feedstock hydrocarbon 29, second gas The inlet of agent runner 16, third gasifying agent runner 18 and the 4th gasifying agent runner 20, which respectively corresponds, is provided with the first gasifying agent Interface 24, the second gasifying agent interface 26, third gasifying agent interface 28 and the 4th gasifying agent interface 30, the 4th gasifying agent runner 20 outside setting water leg chamber 21 and matched water inlet 22 and water outlet 23.Containing feedstock hydrocarbon by adding containing feedstock hydrocarbon Enter feeding line independent after pressure equipment pressurization to connect through the first interface containing feedstock hydrocarbon 25, second containing feedstock hydrocarbon respectively Mouth 27 and third interface containing feedstock hydrocarbon 29 enter corresponding first runner containing feedstock hydrocarbon 15, the second runner containing feedstock hydrocarbon 17 Contain runner containing feedstock hydrocarbon 19 with third, gasifying agent enters respective admission line respectively through the first gasifying agent interface 24, second Gasifying agent interface 26, third gasifying agent interface 28 and the 4th gasifying agent interface 30 enter corresponding first gasifying agent runner 14, the Two gasifying agent runners 16, third gasifying agent runner 18 and the 4th gasifying agent runner 20.
As shown in figure 3, the double acting force (forcing) pump containing feedstock hydrocarbon in 1~embodiment of the embodiment of the present invention 6 is reciprocating double Diaphragm pump is acted on, reciprocating double-action diaphragm pump includes driving wheel 31 and the proportion adjustment wheel 32 with the mating connection of driving wheel 31 Composition, the proportion adjustment wheel 32 are connect by First piston bar 33 with the first piston 34 of the first cylinder body, first piston 34, the One shell 36 and the first diaphragm 38 constitute first piston cavity 35, and the first diaphragm 38 and the second diaphragm 40 constitute the first diaphragm Chamber 39, the second diaphragm 40 and the first inlet check valve 37, first outlet check-valves 42 constitute first fluid pressurizing chamber 41;It is described Proportion adjustment wheel 32 is connect by second piston bar 43 with the second piston 44 of the second cylinder body, second piston 44, second shell 46 Second piston cavity 45 is constituted with third diaphragm 48, third diaphragm 48 and the 4th diaphragm 50 constitute the second diaphragm cavity 49, the Four diaphragms 50 and the second inlet check valve 47, second outlet check-valves 52 constitute second fluid pressurizing chamber 51.When driving wheel 31 When proportion adjustment wheel 32 being driven to rotate, First piston bar 33, the second piston bar 43 being connected on proportion adjustment wheel 32 start to do It moves back and forth, respectively corresponds the first piston 34 for driving its head, second piston 44 with moving reciprocatingly, make first piston cavity 35 and the size of second piston cavity 45 be in cyclically-varying, and then make the first diaphragm 38, the second diaphragm 40, the first diaphragm cavity 39, first fluid pressurizing chamber 41 and third diaphragm 48, the 4th diaphragm 50, the second diaphragm cavity 49, second fluid pressurizing chamber 51 Shape or volume correspond to generating period and sexually revise, when first piston 34 or the release of second piston 44, first fluid pressurizing chamber 41 Or the volume of second fluid pressurizing chamber 51, when becoming larger, corresponding first inlet check valve 37 or the second inlet check valve 47 are because of internal drop Low opening, and corresponding first outlet check-valves 42 or second outlet check-valves 52 are closed under the effect of gravity, contain feedstock hydrocarbon Into in first fluid pressurizing chamber 41 or second fluid pressurizing chamber 51, when first piston 34 or the recycling of second piston 44, first The volume of fluid pressurizing chamber 41 or second fluid pressurizing chamber 51 becomes smaller, corresponding first inlet check valve 37 or the second inlet check valve 47 close under the effect of gravity, and corresponding first outlet check-valves 42 or second outlet check-valves 52 are rushed to summit by containing feedstock hydrocarbon And open, to complete containing the pressurized submitting first fluid pressurizing chamber 41 of feedstock hydrocarbon or second fluid pressurizing chamber 51 containing hydrocarbon The pressurized delivered of raw material.Fluid flow pulse ripple caused by pressurizeing in order to avoid single series fluid, preferably uses this field Three series known to technical staff are that three cylinder parallel connections conveying is respectively arranged in the both sides of force (forcing) pump, keep the stabilization of fluid conveying flow. The characteristics of reciprocating double-action diaphragm pump used in 1~embodiment of the embodiment of the present invention 6, is that pump body setting is proportional Regulating wheel 32, one end of First piston bar 33 are connected to a point A fixed on proportion adjustment wheel 32, one end of second piston bar 43 Then be optionally coupled on several tie points of proportion adjustment wheel 32 (B1, B2, B3, B4 ..., Bn, n be it is just whole greater than 1 Count, take n=4 in Fig. 3), and the position of several tie points is sequentially increased along the radius of proportion adjustment wheel 32.When second piston bar 43 One end and the tie point of proportion adjustment wheel 32 when successively inwardly or outwardly being replaced along proportion adjustment wheel 32, corresponding second piston bar 43 movement travel can gradually increase or reduce, cause second piston cavity 45, third diaphragm 48, the 4th diaphragm 50 deformation and The volume variation of two diaphragm cavities 49 is gradually increased or reduces, and the content change of second fluid pressurizing chamber 51 is finally caused to be gradually increased Or reduce, to determine that second fluid pressurizing chamber 51 includes the conveying capacity size of feedstock hydrocarbon.Therefore reciprocal by adjusting this Formula double-operation diaphragm pumps the position of one end of interior second piston bar 43 and the tie point of proportion adjustment wheel 32, is conveniently adjusted to two The feed flow containing feedstock hydrocarbon of a different runners containing feedstock hydrocarbon, thus by containing in two different runners containing feedstock hydrocarbon The flow ratio of feedstock hydrocarbon is adjusted to 1~2.
Gasification process of the invention is described in detail by 1~embodiment of embodiment 7.
Embodiment 1
The present embodiment the following steps are included:
Step 1: solid block pre-treatment containing feedstock hydrocarbon: the Shaanxi 143.3t Shen Fu bituminous coal being sent into wet process with 53t water and is ground It grinds in equipment 1, while being passed through the aqueous solution that 2.5t contains 10wt% surfactant sodium naphthalene sulfonate, it is then that above-mentioned material is abundant Mixing is ground, and obtaining coal content is 63wt% and the preferable water-coal-slurry of mobility, stability, then water-coal-slurry is conveyed It is stored into raw material slurry storage tank 2 spare;The water content of the Shaanxi Shen Fu bituminous coal is 12.77wt%, and granularity is in 1mm~20mm In free distribution;The granularity that the granularity of coal is respectively less than 0.1mm and 35wt% coal in the water-coal-slurry is greater than 0.075mm;
Step 2: material gasification: the high purity oxygen gas point for being 99.6% by water-coal-slurry obtained in step 1 and bulk purity Not Tong Guo the one-jet runner containing feedstock hydrocarbon of overhead multiple flow passages and gasifying agent runner in the one-jet head of overhead multiple flow passages Portion's mixing is atomized and is sent into reactor 5, and then generating main component in 1320 DEG C of reactions is CO and H2Raw gas, raw gas (with CO+H2Meter) yield be 184558Nm3/ h, raw gas composition and flow see the table below 1;The overhead multiple flow passages single injector With 5 flow passage structures, the center flow channels of 5 flow passage structure are the first gasifying agent runner, and are followed successively by outward from center flow channels First runner containing feedstock hydrocarbon, the second gasifying agent runner, the second runner containing feedstock hydrocarbon, third gasifying agent runner, it is described carbon containing It is carbon containing that hydrogen feedstock respectively enters overhead multiple flow passages one-jet first under the pressurization of double acting feedstock hydrocarbon force (forcing) pump In hydrogen feedstock runner and the second runner containing feedstock hydrocarbon, two rates of discharge of the double acting feedstock hydrocarbon force (forcing) pump are 99.4t/h, outlet pressure are 7.3MPa, and the oxygen is delivered to three gasifying agent runners from air separation unit by air duct In, the pressure of oxygen is 8.3MPa, total flow 74537Nm3/ h, the oxygen flow into the first gasifying agent runner are 11180Nm3/ h, the oxygen flow into the second gasifying agent runner are 26088Nm3/ h, into the oxygen stream of third gasifying agent runner Amount is 37269Nm3/h;
The composition and flow for the raw gas that 1 embodiment 1 of table generates
Step 3: product purifies: being 1320 DEG C by the temperature generated in step 2 and contain the thick of 23987kg high-temperature slag Coal gas is sent into rough coal Gas Cooler 6 and is water-cooled, and raw gas and the thick slag of 15591kg inanimate matter ash and 8396kg inanimate matter are obtained Ash fine slag, the thick slag of inanimate matter ash settle into the cooling water of 6 bottom of rough coal Gas Cooler and by ash discharge technique through thick Slag discharge system 7 is discharged, and inanimate matter ash fine slag is settled into the cooling water of 6 bottom of rough coal Gas Cooler and formed containing tiny The Heisui River of ash content, wherein 5258kg inanimate matter ash fine slag is suspended in cooling water, and the temperature in the Heisui River is 251 DEG C, and pressure is 6.5MPa, the fine ash containing 5258kg, will the Heisui River be discharged rough coal Gas Cooler 6 after be sent into wastewater treatment working section III in carry out into The processing of one step;The raw gas for being entrained with 3138kg fine ash is washed after the discharge of the top exit of rough coal Gas Cooler 6 into raw gas It washs clarifier 8 to be washed, obtains clean (dustiness≤0.1mg/m up to standard3) raw gas and washing Heisui River containing fine ash, Wherein, the composition of clean raw gas up to standard and flow see the table below 2, and the temperature in the washing Heisui River is 238 DEG C, pressure 6.5MPa, Fine ash containing 3138kg, the washing Heisui River a part send the cooling water to gas cooler 6 as high temperature rough gas to use, separately A part is sent to subsequent grey water treatment system (III) and is further processed;
The composition and flow of the cleaning that 2 embodiment 1 of table generates raw gas up to standard
Component Flow (Nm3/h) It forms (mol%)
H2 81809.48 14.57
CO 102748.85 18.30
CO2 43796.56 7.80
H2S 2060.49 3.67E-01
COS 232.49 4.14E-02
CH4 237.41 4.23E-02
N2 709.44 1.26E-01
Ar 297.74 5.30E-02
H2O 329639.66 58.70
It amounts to 561532.12 100.00
Step 4: usage on black water: buck inspissator 9 is sent into Heisui River obtained in step 3 and washing Heisui River and depressurized Flash distillation, the flash steam that moisture vaporization forms 220 DEG C separate and are discharged into grey water heater 11 from the top of buck inspissator 9 In, remaining unvaporized liquid and 8396kg fine ash amount to 409745kg and are discharged into dope mistake from the bottom of buck inspissator 9 Filter 10 is filtered, and obtains fine ash and buck, and it is thin that water content 50wt%, temperature are that 68 DEG C of fine ash is accumulated as 14400kg Slag is discharged from the bottom of dope filter 10, and the buck that obtained 402545kg dust burdening is 2.5wt%, temperature is 68 DEG C enters In grey water collector 13;In grey water heater 11, flow 52001Nm3The steam of/h is sent into from grey water collector 13 292368kg temperature be that 95 DEG C of buck carries out heat exchange in a manner of directly mixing, obtained 302147kg temperature is 132 DEG C of hot buck is used to be pumped in raw gas washing, purifying device 8 as return buck and is utilized, and is discharged in grey water heater 11 Temperature be 149 DEG C uncooled flash steam enter and be condensed into that flow is 32007kg/h, temperature is 95 DEG C in condenser 12 Buck enters grey water collector 13 and is recycled.
For the salinity deposited in the present embodiment usage on black water workshop section system is discharged, from the buck that dope filter 10 is discharged 16580kg is drawn, temperature is that 68 DEG C of buck is sent to grey water collector 13, is cooled to 40 DEG C or less and drains into and is used as this work outside battery limit (BL) The waste water outlet of skill.
Embodiment 2
The present embodiment the following steps are included:
Step 1: solid block pre-treatment containing feedstock hydrocarbon: the Shaanxi 53.6t Shen Fu bituminous coal and 20.5t water are sent into wet process In milling apparatus 1, while it being passed through the aqueous solution that 0.5t contains 25wt% sodium lignin sulfonate, is then sufficiently mixed above-mentioned material It is ground, obtaining coal content is 55wt% and the preferable water-coal-slurry of mobility, stability, then water-coal-slurry is delivered to original It is stored in slurry body storage tank 2 spare;The water content of the Shaanxi Shen Fu bituminous coal is 14.78wt%, and granularity is in certainly in 1mm~20mm By being distributed;The granularity that the granularity of coal is respectively less than 0.1mm and 35wt% coal in the water-coal-slurry is greater than 0.075mm;
Step 2: material gasification: by water-coal-slurry, mink cell focus obtained in step 1 and bulk purity be 99.6% it is high-purity Oxygen passes through the one-jet runner containing feedstock hydrocarbon of overhead multiple flow passages and gasifying agent runner in overhead multiple flow passages single spraying respectively The head mixing of mouth is atomized and is sent into reactor 5, and then generating main component in 1320 DEG C of reactions is CO and H2Raw gas, Raw gas is (with CO+H2Meter) yield be 10000Nm3/ h, the composition and flow of raw gas see the table below 3;The overhead multiple flow passages Single injector has 5 flow passage structures, and the center flow channels of 5 flow passage structure are the first gasifying agent runner, and outside from center flow channels It is followed successively by the first runner containing feedstock hydrocarbon, the second gasifying agent runner, the second runner containing feedstock hydrocarbon, third gasifying agent runner, institute It states mink cell focus and water-coal-slurry and respectively enters overhead multiple flow passages single injector under the pressurization of double acting feedstock hydrocarbon force (forcing) pump The first runner containing feedstock hydrocarbon and the second runner containing feedstock hydrocarbon in, the water-coal-slurry outlet of double acting feedstock hydrocarbon pump Flow is 87.1t/h, and outlet pressure 7.3MPa, the flow of heavy oil export is 8.4t/h, and outlet pressure is 7.3MPa, The oxygen is delivered in three gasifying agent runners by air duct from air separation unit, and the pressure of oxygen is 8.3MPa, total to flow Amount is 35141Nm3/ h, the oxygen flow into the first gasifying agent runner are 5271Nm3/ h, into the oxygen of the second gasifying agent runner Throughput is 10470Nm3/ h, the oxygen flow into third gasifying agent runner are 19400Nm3/h;
The composition and flow for the raw gas that 3 embodiment 2 of table generates
Step 3: product purifies: being 1320 DEG C by the temperature generated in step 2 and contain the thick of 5211kg high-temperature slag Coal gas is sent into rough coal Gas Cooler 6 and is water-cooled, and raw gas and the thick slag of 3387kg inanimate matter ash and 1824kg inanimate matter are obtained Ash fine slag, the thick slag of inanimate matter ash settle into the cooling water of 6 bottom of rough coal Gas Cooler and by ash discharge technique through thick Slag discharge system 7 is discharged, and inanimate matter ash fine slag is settled into the cooling water of 6 bottom of rough coal Gas Cooler and formed containing tiny The Heisui River of ash content, wherein 1158kg inanimate matter ash fine slag is suspended in cooling water, and the temperature in the Heisui River is 180 DEG C, and pressure is 6.5MPa is further processed being sent into wastewater treatment working section III after Heisui River discharge rough coal Gas Cooler 6;It is entrained with The raw gas of 666kg fine ash enters raw gas washing, purifying device 8 after the discharge of the top exit of rough coal Gas Cooler 6 and is washed It washs, obtains clean (dustiness≤0.1mg/m up to standard3) raw gas and washing Heisui River containing fine ash, wherein it is clean up to standard The composition and flow of raw gas see the table below 4, and the temperature in the washing Heisui River is 150 DEG C, and pressure 6.3MPa contains the thin of 751kg Ash, the washing Heisui River a part send the cooling water to gas cooler 6 as high temperature rough gas to use, and another part is sent to subsequent Grey water treatment system (III) be further processed;
The composition and flow of the cleaning that 4 embodiment 2 of table generates raw gas up to standard
Component Flow (Nm3/h) It forms (mol%)
H2 44085.86 16.18
CO 55914.14 20.52
CO2 17711.32 6.50
H2S 177.40 6.51E-02
COS 20.01 7.34E-03
CH4 42.27 1.55E-02
N2 366.01 1.34E-01
Ar 140.39 5.15E-02
H2O 153994.64 56.52
It amounts to 272452.05 100.00
Step 4: usage on black water: buck inspissator 9 is sent into Heisui River obtained in step 3 and washing Heisui River and depressurized Flash distillation, the flash steam that moisture vaporization forms 130 DEG C separate and are discharged into grey water heater 11 from the top of buck inspissator 9 In, remaining unvaporized liquid and 1025kg fine ash amount to 98542kg and are discharged into dope filtering from the bottom of buck inspissator 9 Device 10 is filtered, and obtains fine ash and buck, and it is thin that the fine ash that wherein water content is 40wt%, temperature is 50 DEG C is accumulated as 1531kg Slag is discharged from the bottom of dope filter 10, and obtained 96870kg dust burdening is 0.1wt%, temperature is 50 DEG C (50 DEG C~110 DEG C) buck enter in grey water collector 13;In grey water heater 11, flow 405101Nm3The steam of/h with from buck The 75645kg temperature being sent into collector 13 is that 80 DEG C of buck carries out heat exchange in a manner of directly mixing, and is obtained 80359kg hot buck at a temperature of 90 °C is used to be pumped in raw gas washing, purifying device 8 as return buck and is utilized, and buck adds The uncooled flash steam that remaining temperature is 100 DEG C in hot device 11 enter in condenser 12 be condensed into flow be 27838kg/h, Temperature is that 85 DEG C of buck enters grey water collector 13 and recycled.
For the salinity deposited in discharge usage on black water workshop section system, drawn from the buck that dope filter 10 is discharged 32458kg, temperature are that 50 DEG C of buck is sent to grey water collector 13, are cooled to 40 DEG C or less and drain into and are used as this technique outside battery limit (BL) Waste water outlet.
Embodiment 3
The present embodiment the following steps are included:
Step 1: solid block pre-treatment containing feedstock hydrocarbon: the Shaanxi 52.9t Shen Fu bituminous coal and 29.6t water are sent into wet process In milling apparatus 1, while it being passed through the aqueous solution that 1000kg contains 25wt% water-coal-slurry specialist additive sodium humate, it then will be upper It states material and is sufficiently mixed and ground, obtaining coal content is 60wt% and the preferable water-coal-slurry of mobility, stability, then will Water-coal-slurry be delivered in raw material slurry storage tank 2 store it is spare;The water content of the Shaanxi Shen Fu bituminous coal is 5.66wt%, and granularity is small It in 10mm and is in freely to be distributed;
Step 2: material gasification: the high pure oxygen for being 90% by water-coal-slurry, natural gas obtained in step 1 and bulk purity Gas passes through the one-jet runner containing feedstock hydrocarbon of overhead multiple flow passages and gasifying agent runner in overhead multiple flow passages single injector respectively Head mixing, be atomized and be sent into reactor 5, then generating main components in 1300 DEG C of reactions is CO and H2Raw gas, slightly Coal gas is (with CO+H2Meter) yield be 200000Nm3/ h, the composition and flow of raw gas see the table below 5;The overhead multiple flow passages Single injector has 5 flow passage structures, and the center flow channels of 5 flow passage structure are the first gasifying agent runner, and outside from center flow channels It is followed successively by the first runner containing feedstock hydrocarbon, the second gasifying agent runner, the second runner containing feedstock hydrocarbon, third gasifying agent runner, institute It states water-coal-slurry and respectively enters overhead multiple flow passages one-jet first under the pressurization of double acting feedstock hydrocarbon force (forcing) pump and contain In feedstock hydrocarbon runner and the second runner containing feedstock hydrocarbon, two outlet water-coal-slurry of the double acting feedstock hydrocarbon force (forcing) pump Flow is respectively 55.73t/h and 27.9t/h, and outlet pressure is 7.3MPa, the outlet that the flow of water-coal-slurry is 55.73t/h with The connection of first runner containing feedstock hydrocarbon, the outlet that the flow of water-coal-slurry is 27.9t/h are connect with the second runner containing feedstock hydrocarbon, institute It states oxygen and is delivered in the first gasifying agent runner and third gasifying agent runner by air duct from air separation unit, the pressure of oxygen For 8.3MPa, total flow 62679Nm3/ h, the oxygen flow into the first gasifying agent runner are 15401Nm3/ h, into third The oxygen flow of gasifying agent runner is 47278Nm3/ h, natural gas are entered in reactor 5 by the second gasifying agent runner, natural gas Flow be 45488Nm3/h;
The composition and flow for the raw gas that 5 embodiment 3 of table generates
Step 3: product purifies: being 1300 DEG C by the temperature generated in step 2 and contain 5931.4kg high-temperature slag Raw gas is sent into rough coal Gas Cooler 6 and is water-cooled, and obtains raw gas and the thick slag of 3855kg inanimate matter ash and 2076kg is inorganic Matter ash fine slag, the thick slag of inanimate matter ash are settled into the cooling water of 6 bottom of rough coal Gas Cooler and are passed through by ash discharge technique Thick slag discharge system 7 is discharged, and inanimate matter ash fine slag is settled into the cooling water of 6 bottom of rough coal Gas Cooler and formed containing thin The Heisui River of small ash content, wherein 1412kg inanimate matter ash fine slag is suspended in cooling water, and the temperature in the Heisui River is 270 DEG C, pressure For 6.3MPa, it is further processed being sent into wastewater treatment working section III after Heisui River discharge rough coal Gas Cooler 6;It is entrained with The raw gas of 664kg fine ash enters raw gas washing, purifying device 8 after the discharge of the top exit of rough coal Gas Cooler 6 and is washed It washs, obtains clean (dustiness≤0.1mg/m up to standard3) raw gas and washing Heisui River containing fine ash, wherein it is clean up to standard The composition and flow of raw gas see the table below 6, and the temperature in the washing Heisui River is 254 DEG C, and pressure 6.05MPa contains the thin of 664kg Ash, the washing Heisui River a part send the cooling water to gas cooler 6 as high temperature rough gas to use, and another part is sent to subsequent Grey water treatment system (III) be further processed;
The composition and flow of the cleaning that 6 embodiment 3 of table generates raw gas up to standard
Component Flow (Nm3/h) It forms (mol%)
H2 109086.82 41.28
CO 90913.18 25.96
CO2 19847.84 4.25
H2S 246.02 0.03
COS 27.74 0.004
CH4 246.74 0.12
N2 708.52 0.05
Ar 250.62 0.07
H2O 119333.56 28.22
It amounts to 340661.04 100.00
Step 4: usage on black water: buck inspissator 9 is sent into Heisui River obtained in step 3 and washing Heisui River and depressurized Flash distillation, the flash steam that moisture vaporization forms 205 DEG C separate and are discharged into grey water heater 11 from the top of buck inspissator 9 In, remaining unvaporized liquid and 2076kg fine ash amount to 85402kg and are discharged into dope filtering from the bottom of buck inspissator 9 Device 10 is filtered, and obtains fine ash and buck, the fine ash that water content 55wt%, temperature are 73 DEG C be accumulated as 4613kg fine slag from The bottom of dope filter 10 is discharged, and the buck that obtained 80788kg dust burdening is 0.3wt%, temperature is 73 DEG C enters buck In collector 13;In grey water heater 11, flow 52001Nm3The steam of/h be sent into from grey water collector 13 98456kg temperature is that 105 DEG C of buck carries out heat exchange in a manner of directly mixing, and obtained 116006kg temperature is 152 DEG C hot buck use be pumped in raw gas washing, purifying device 8 as return buck be utilized, it is remaining in grey water heater 11 The uncooled flash steam that temperature is 120 DEG C enters the ash for being condensed into that flow is 24236kg/h, temperature is 98 DEG C in condenser 12 Water enters grey water collector 13 and is recycled.
For the salinity deposited in discharge usage on black water workshop section system, drawn from the buck that dope filter 10 is discharged 38596kg, temperature are that 73 DEG C of buck is sent to grey water collector 13, are cooled to 40 DEG C or less and drain into and are used as this technique outside battery limit (BL) Waste water outlet.
Embodiment 4
The present embodiment the following steps are included:
Step 1: solid block pre-treatment containing feedstock hydrocarbon: 35.2t Kuqa bituminous coal and 17.8t water are sent into wet process In milling apparatus 1, while it being passed through the aqueous solution that 800kg contains 25wt% sodium naphthasulfonate, is then sufficiently mixed above-mentioned material It is ground, obtaining coal content is 70wt% and the preferable water-coal-slurry of mobility, stability, then water-coal-slurry is delivered to original It is stored in slurry body storage tank 2 spare;The water content of the Kuqa bituminous coal is 8.36wt%, and it is in freely to divide that granularity, which is less than 10mm, Cloth;
Step 2: material gasification: being by water-coal-slurry, heavy oil residue obtained in step 1, natural gas and bulk purity 99.8% high purity oxygen gas passes through the one-jet runner containing feedstock hydrocarbon of overhead multiple flow passages respectively and gasifying agent runner is set upper The mixing of formula multiple flow passages one-jet head is atomized and is sent into reactor 5, then 1280 DEG C of reactions generate main components be CO with H2Raw gas, raw gas is (with CO+H2Meter) yield be 168500Nm3/ h, the composition and flow of raw gas see the table below 7;It is described Overhead multiple flow passages single injector has 7 flow passage structures, and the center flow channels of 7 flow passage structure are the first gasifying agent runner, and from Center flow channels are followed successively by the first runner containing feedstock hydrocarbon, the second gasifying agent runner, the second runner containing feedstock hydrocarbon, third gas outward Agent runner, third runner containing feedstock hydrocarbon, the 4th gasifying agent runner, the heavy oil residue is in single-acting feedstock hydrocarbon force (forcing) pump Pressurization under enter one-jet first runner containing feedstock hydrocarbon of overhead multiple flow passages, the single-acting feedstock hydrocarbon pressurizes The flow of the outlet heavy oil residue of pump is 12.5t/h, outlet pressure 7.3MPa, and the water-coal-slurry adds in double acting feedstock hydrocarbon One-jet second runner containing feedstock hydrocarbon of overhead multiple flow passages and third are respectively enterd under the pressurization of press pump containing hydrocarbon original In stream road, the flow of two outlet water-coal-slurry of the double acting feedstock hydrocarbon force (forcing) pump is respectively 19.5t/h and 34.3t/ H, outlet pressure are 7.3MPa, and the outlet that the flow of water-coal-slurry is 19.5t/h is connect with the second runner containing feedstock hydrocarbon, water coal The flow of slurry is that the outlet of 34.3t/h is connect with third runner containing feedstock hydrocarbon, and the oxygen is filled by air duct from space division It sets and is delivered in the first gasifying agent runner and third gasifying agent runner, the pressure of oxygen is 8.3MPa, total flow 51358Nm3/ H, the oxygen flow into the first gasifying agent runner are 9891Nm3/ h, the oxygen flow into third gasifying agent runner are 15305Nm3/ h, natural gas are entered in reactor 5 by the second gasifying agent runner, and the flow of natural gas is 10000Nm3/ h enters The oxygen flow of 4th gasifying agent runner is 26162Nm3/h;
The composition and flow for the raw gas that 7 embodiment 4 of table generates
Step 3: product purifies: being 1280 DEG C by the temperature generated in step 2 and contain 5012.8kg high-temperature slag Raw gas is sent into rough coal Gas Cooler 6 and is water-cooled, and raw gas, the thick slag of 3258kg inanimate matter ash and 1754kg inanimate matter are obtained Ash fine slag, the thick slag of inanimate matter ash settle into the cooling water of 6 bottom of rough coal Gas Cooler and by ash discharge technique through thick Slag discharge system 7 is discharged, and inanimate matter ash fine slag is settled into the cooling water of 6 bottom of rough coal Gas Cooler and formed containing tiny The Heisui River of ash content, wherein 1193kg inanimate matter ash fine slag is suspended in cooling water, and the temperature in the Heisui River is 300 DEG C, and pressure is 6.3MPa is further processed being sent into wastewater treatment working section III after Heisui River discharge rough coal Gas Cooler 6;It is entrained with The raw gas of 561kg fine ash enters raw gas washing, purifying device 8 after the discharge of the top exit of rough coal Gas Cooler 6 and is washed It washs, obtains clean (dustiness≤0.1mg/m up to standard3) raw gas and washing Heisui River containing fine ash, wherein it is clean up to standard The composition and flow of raw gas see the table below 8, and the temperature in the washing Heisui River is 280 DEG C, and pressure 6.1MPa contains the thin of 561kg Ash, the washing Heisui River a part send the cooling water to gas cooler 6 as high temperature rough gas to use, and another part is sent to subsequent Grey water treatment system (III) be further processed;
The composition and flow of the cleaning that 8 embodiment 4 of table generates raw gas up to standard
Component Flow (Nm3/h) It forms (mol%)
H2 92100.88 35.16
CO 76399.12 29.17
CO2 19736.05 7.53
H2S 190.24 0.07
COS 23.78 0.01
CH4 214.02 0.08
N2 689.61 0.26
Ar 237.80 0.09
H2O 72347.57 27.62
It amounts to 261939.06 100.00
Step 4: wastewater treatment: buck inspissator 9 is sent into Heisui River obtained in step 3 and washing Heisui River and depressurized Flash distillation, the flash steam that moisture vaporization forms 220 DEG C separate and are discharged into grey water heater 11 from the top of buck inspissator 9 In, remaining unvaporized liquid and 1754kg fine ash amount to 69524kg and are discharged into dope filtering from the bottom of buck inspissator 9 Device 10 is filtered, and obtains fine ash and buck, the fine ash that water content 60wt%, temperature are 80 DEG C be accumulated as 4385kg fine slag from The bottom of dope filter 10 is discharged, and the buck that obtained 65139kg dust burdening is 5wt%, temperature is 80 DEG C enters buck receipts In storage 13;In grey water heater 11, flow 48210Nm3The steam of/h be sent into from grey water collector 13 56254kg temperature is that 110 DEG C of buck carries out heat exchange in a manner of directly mixing, and obtained 72154kg temperature is 160 DEG C Hot buck use be pumped in raw gas washing, purifying device 8 as return buck be utilized, remaining temperature in grey water heater 11 Degree enters the ash for being condensed into that flow is 22840kg/h, temperature is 120 DEG C in condenser 12 for 160 DEG C of uncooled flash steam Water enters grey water collector 13 and is recycled.
For the salinity deposited in discharge usage on black water workshop section system, drawn from the buck that dope filter 10 is discharged 20120kg, temperature are that 80 DEG C of buck is sent to grey water collector 13, are cooled to 40 DEG C or less and drain into and are used as this technique outside battery limit (BL) Waste water outlet.
Embodiment 5
The present embodiment and embodiment 4 the difference is that: gasifying agent composition is only oxygen, containing in feedstock hydrocarbon without natural Gas is opened the nitrogen valve for leading to the second gasifying agent flow-path tube road, is simultaneously closed off towards the second gasifying agent flow-path tube road Gas material valve replaces natural gas to be entered in reactor 5 by the second gasifying agent runner using nitrogen.The flow of nitrogen is 200Nm3The gentle agent flow containing feedstock hydrocarbon of/h, other runners remain unchanged, the raw gas that obtains at this time composition and most Clean raw gas composition up to standard is shown in Table 9 and table 10 respectively eventually.
The composition and flow for the raw gas that 9 embodiment 5 of table generates
Component Flow (Nm3/h) It forms (mol%)
H2 87458.31 38.29
CO 71542.15 31.32
CO2 19860.05 8.69
H2S 190.28 0.08
COS 23.78 0.01
CH4 214.06 0.09
N2 889.75 0.39
Ar 237.84 0.10
H2O 47997.09 21.01
It amounts to 228413.3 100.00
The composition and flow of the cleaning that 10 embodiment 5 of table generates raw gas up to standard
Component Flow (Nm3/h) It forms (mol%)
H2 87397.58 34.90
CO 71478.53 28.54
CO2 19736.05 7.88
H2S 190.24 0.08
COS 23.78 0.01
CH4 214.02 0.09
N2 889.5694 0.36
Ar 237.8 0.09
H2O 70248.55 28.05
It amounts to 250416.1 100.00
Embodiment 6
The present embodiment the following steps are included:
Step 1: solid block pre-treatment containing feedstock hydrocarbon: by the regional bituminous coal in the peaceful east 119.6t and following from hot-blast stove Ring dry-heat air (main component N2、CO2) be fed together in dry grinding equipment 3 and ground, obtaining 106.8t water content is The coal dust of 1.5wt%, then coal dust is delivered in dry powder raw material storage tank 4 at the same be passed through nitrogen as fluidized gas store it is spare;Institute The water content for stating the regional bituminous coal in rather east is 12wt%, and granularity is less than 10mm and is in freely to be distributed;The granularity of the coal dust is less than 90 μ m;
Step 2: material gasification: high purity oxygen gas, vapor by coal dust obtained in step 1 and bulk purity for 95% It is one-jet in overhead multiple flow passages by the one-jet runner containing feedstock hydrocarbon of overhead multiple flow passages and gasifying agent runner respectively Head mixes and is atomized and is sent into reactor 5, and then generating main component in 1380 DEG C of reactions is CO and H2Raw gas, rough coal Gas is (with CO+H2Meter) yield be 195500Nm3/ h, the composition and flow of raw gas see the table below 11;The overhead multiple flow passages list Nozzle has 5 flow passage structures, and the center flow channels of 5 flow passage structure are the first gasifying agent runner, and from center flow channels outward according to Secondary is the first runner containing feedstock hydrocarbon, the second gasifying agent runner, the second runner containing feedstock hydrocarbon, third gasifying agent runner, described Coal dust respectively enters overhead multiple flow passages one-jet first containing feedstock hydrocarbon under the pressurization that double acting feedstock hydrocarbon pumps In runner and the second runner containing feedstock hydrocarbon, the flow of two outlet coal dusts of the double acting feedstock hydrocarbon force (forcing) pump is respectively 38.3t/h and 68.5t/h, outlet pressure are 4.0MPa, and the outlet that the flow of coal dust is 38.3t/h contains feedstock hydrocarbon with first Runner connection, the outlet that the flow of coal dust is 68.5t/h are connect with the second runner containing feedstock hydrocarbon, and the oxygen passes through snorkel Road is delivered in the first gasifying agent runner and third gasifying agent runner from air separation unit, and the pressure of oxygen is 5.5MPa, total flow For 61592Nm3/ h, the oxygen flow into the first gasifying agent runner are 11392Nm3/ h, into the oxygen of third gasifying agent runner Flow is 50200Nm3/ h, vapor are entered in reactor 5 by the second gasifying agent runner, and the flow of vapor is 14354Nm3/ H, temperature are 272 DEG C, pressure 5.5MPa;
The composition and flow for the raw gas that 11 embodiment 6 of table generates
Component Flow (Nm3/h) It forms (mol%)
H2 58930.57 27.12
CO 136911.59 63.01
CO2 6733.72 3.10
H2S 346.37 0.16
COS 254.78 0.12
CH4 209.51 0.10
N2 8854.06 4.07
Ar 246.36 0.11
H2O 4801.83 2.21
It amounts to 217288.78 100.00
Step 3: product purifies: being 1380 DEG C by the temperature generated in step 2 and contain the thick of 11479kg high-temperature slag Coal gas is sent into rough coal Gas Cooler 6 and is water-cooled, and raw gas, the thick slag of 7461kg inanimate matter ash and 4018kg inanimate matter ash are obtained Part fine slag, the thick slag of inanimate matter ash settle into the cooling water of 6 bottom of rough coal Gas Cooler and by ash discharge technique through thick slag Discharge system 7 is discharged, and inanimate matter ash fine slag, which settles into be formed in the cooling water of 6 bottom of rough coal Gas Cooler, contains ash fines The Heisui River divided, wherein 2947kg inanimate matter ash fine slag is suspended in cooling water, and the temperature in the Heisui River is 260 DEG C, and pressure is 3.8MPa is further processed being sent into wastewater treatment working section III after Heisui River discharge rough coal Gas Cooler 6;It is entrained with The raw gas of 1071kg fine ash enters raw gas washing, purifying device 8 after the discharge of the top exit of rough coal Gas Cooler 6 and is washed It washs, obtains clean (dustiness≤0.1mg/m up to standard3) raw gas and washing Heisui River containing fine ash, wherein it is clean up to standard The composition and flow of raw gas see the table below 12, and the temperature in the washing Heisui River is 242 DEG C, and pressure 3.7MPa contains 1071kg's Fine ash, the washing Heisui River a part send the cooling water to gas cooler 6 as high temperature rough gas to use, and another part is sent to rear Continuous grey water treatment system (III) is further processed;
The composition and flow of the cleaning that 12 embodiment 6 of table generates raw gas up to standard
Component Flow (Nm3/h) It forms (mol%)
H2 58776.86 12.48
CO 136723.14 29.03
CO2 6595.80 1.40
H2S 327.42 0.07
COS 240.04 0.05
CH4 208.45 0.04
N2 8762.47 1.86
Ar 246.36 0.05
H2O 259069.22 55.01
It amounts to 470949.76 100.00
Step 4: usage on black water: buck inspissator 9 is sent into Heisui River obtained in step 3 and washing Heisui River and depressurized Flash distillation, the flash steam that moisture vaporization forms 205 DEG C separate and are discharged into grey water heater 11 from the top of buck inspissator 9 In, remaining unvaporized liquid and 4018kg fine ash amount to 102351kg and are discharged into dope mistake from the bottom of buck inspissator 9 Filter 10 is filtered, and obtains fine ash and buck, and the fine ash that water content 50wt%, temperature are 65 DEG C is accumulated as 8036kg fine slag It is discharged from the bottom of dope filter 10, the buck that obtained 94315kg dust burdening is 1.2wt%, temperature is 65 DEG C enters ash In water collector 13;In grey water heater 11, flow 83102Nm3The steam of/h be sent into from grey water collector 13 104632kg temperature is that 98 DEG C of buck carries out heat exchange in a manner of directly mixing, and obtained 125384kg temperature is 144 DEG C hot buck use be pumped in raw gas washing, purifying device 8 as return buck be utilized, it is remaining in grey water heater 11 The uncooled flash steam that temperature is 128 DEG C, which enters, is condensed into that flow is 46026kg/h, temperature is 101 DEG C in condenser 12 Buck enters grey water collector 13 and is recycled.
For the salinity deposited in discharge usage on black water workshop section system, drawn from the buck that dope filter 10 is discharged 35421kg, temperature are that 65 DEG C of buck is sent to grey water collector 13, are cooled to 40 DEG C or less and drain into and are used as this technique outside battery limit (BL) Waste water outlet.
Embodiment 7
The present embodiment the following steps are included:
Step 1: solid block pre-treatment containing feedstock hydrocarbon: by 73.4t mind mansion area's bituminous coal and from the circulation of hot-blast stove Dry-heat air (main component N2、CO2) be fed together in dry grinding equipment 3 and ground, obtaining 63.6t water content is The coal dust of 0.8wt%, then coal dust is delivered in dry powder raw material storage tank 4 at the same be passed through nitrogen as fluidized gas store it is spare;Institute The water content of Shu Shen mansion area bituminous coal is 14wt%, and granularity is less than 12mm and is in freely to be distributed;The granularity of the coal dust is less than 90 μ m;
Step 2: material gasification: high purity oxygen gas, vapor by coal dust obtained in step 1 and bulk purity for 95% It is one-jet in overhead multiple flow passages by the one-jet runner containing feedstock hydrocarbon of overhead multiple flow passages and gasifying agent runner respectively Head mixes and is atomized and is sent into reactor 5, and then generating main component in 1230 DEG C of reactions is CO and H2Raw gas, rough coal Gas is (with CO+H2Meter) yield be 190528Nm3/ h, the composition and flow of raw gas see the table below 13;The overhead multiple flow passages list Nozzle has 7 flow passage structures, and the center flow channels of 7 flow passage structure are the first gasifying agent runner, and from center flow channels outward according to Secondary is the first runner containing feedstock hydrocarbon, the second gasifying agent runner, the second runner containing feedstock hydrocarbon, third gasifying agent runner, third Runner containing feedstock hydrocarbon, the 4th gasifying agent runner, single-acting feedstock hydrocarbon pump of the coal dust in double acting feedstock hydrocarbon pump sum Pressurization under respectively enter one-jet first runner containing feedstock hydrocarbon of overhead multiple flow passages, the second runner containing feedstock hydrocarbon Flow with third runner containing feedstock hydrocarbon, two outlet coal dusts of the double acting feedstock hydrocarbon force (forcing) pump is respectively 17.8t/ H and 22.3t/h, outlet pressure are 3.8MPa, and the outlet and the first runner containing feedstock hydrocarbon that the flow of coal dust is 17.8t/h connect It connects, the outlet that the flow of coal dust is 22.3t/h is connect with the second runner containing feedstock hydrocarbon, and the single-acting feedstock hydrocarbon pump goes out The flow of mouthful coal dust is 23.5t/h, outlet pressure 3.8MPa, and the oxygen is delivered to the from air separation unit by air duct In one gasifying agent runner and third gasifying agent runner, the pressure of oxygen is 4.8MPa, total flow 54322Nm3/ h, into first The oxygen flow of gasifying agent runner is 12461Nm3/ h, the oxygen flow into third gasifying agent runner are 41861Nm3/ h, water steam Gas is entered in reactor 5 by the second gasifying agent runner, and the flow of vapor is 13241Nm3/ h, temperature are 262 DEG C, and pressure is 4.8MPa;
The composition and flow for the raw gas that 13 embodiment 7 of table generates
Component Flow (Nm3/h) It forms (mol%)
H2 68578.42 32.92
CO 121987.3 58.56
CO2 6324.25 3.04
H2S 257.82 0.12
COS 119.52 0.06
CH4 215.84 0.10
N2 6324.51 3.04
Ar 234.21 0.11
H2O 4256.32 2.04
It amounts to 208298.2 100.00
Step 3: product purifies: being 1230 DEG C by the temperature generated in step 2 and contain the thick of 6887kg high-temperature slag Coal gas is sent into rough coal Gas Cooler 6 and is water-cooled, and raw gas and the thick slag of 4477kg inanimate matter ash and 2410kg inanimate matter are obtained Ash fine slag, the thick slag of inanimate matter ash settle into the cooling water of 6 bottom of rough coal Gas Cooler and by ash discharge technique through thick Slag discharge system 7 is discharged, and inanimate matter ash fine slag is settled into the cooling water of 6 bottom of rough coal Gas Cooler and formed containing tiny The Heisui River of ash content, wherein 1567kg inanimate matter ash fine slag is suspended in cooling water, and the temperature in the Heisui River is 263 DEG C, and pressure is 3.0MPa, the fine ash containing 724kg, will the Heisui River be discharged rough coal Gas Cooler 6 after be sent into wastewater treatment working section III in carry out into The processing of one step;The raw gas for being entrained with 843kg fine ash enters raw gas after the discharge of the top exit of rough coal Gas Cooler 6 and washs Clarifier 8 is washed, and clean (dustiness≤0.1mg/m up to standard is obtained3) raw gas and washing Heisui River containing fine ash, In, the composition and flow of clean raw gas up to standard see the table below 14, and the temperature in the washing Heisui River is 241 DEG C, pressure 2.8MPa, Fine ash containing 851kg, the washing Heisui River a part send the cooling water to gas cooler 6 as high temperature rough gas to use, separately A part is sent to subsequent grey water treatment system (III) and is further processed;
The composition and flow of the cleaning that 14 embodiment 7 of table generates raw gas up to standard
Component Flow (Nm3/h) It forms (mol%)
H2 68564.70 16.02
CO 121962.92 28.50
CO2 6134.52 1.43
H2S 257.05 0.06
COS 119.16 0.03
CH4 215.19 0.05
N2 6305.54 1.47
Ar 233.51 0.05
H2O 224171.52 52.38
It amounts to 427964.11 100.00
Step 4: usage on black water: buck inspissator 9 is sent into Heisui River obtained in step 3 and washing Heisui River and depressurized Flash distillation, the flash steam that moisture vaporization forms 205 DEG C separate and are discharged into grey water heater 11 from the top of buck inspissator 9 In, remaining unvaporized liquid and 1240kg fine ash amount to 65421kg and are discharged into dope filtering from the bottom of buck inspissator 9 Device 10 is filtered, and obtains fine ash and buck, the fine ash that water content 50wt%, temperature are 65 DEG C be accumulated as 2480kg fine slag from The bottom of dope filter 10 is discharged, and the buck that obtained 62941kg dust burdening is 1.2wt%, temperature is 65 DEG C enters buck In collector 13;In grey water heater 11, flow 75420Nm3The steam of/h be sent into from grey water collector 13 54124kg temperature is that 96 DEG C of buck carries out heat exchange in a manner of directly mixing, and obtained 110470kg temperature is 142 DEG C Hot buck use be pumped in raw gas washing, purifying device 8 as return buck be utilized, remaining temperature in grey water heater 11 Degree enters the buck for being condensed into that flow is 4259kg/h, temperature is 95 DEG C in condenser 12 for 125 DEG C of uncooled flash steam It is recycled into grey water collector 13.
For the salinity deposited in discharge usage on black water workshop section system, drawn from the buck that dope filter 10 is discharged 26541kg, temperature are that 65 DEG C of buck is sent to grey water collector 13, are cooled to 40 DEG C or less and drain into and are used as this technique outside battery limit (BL) Waste water outlet.
The above is only presently preferred embodiments of the present invention, is not intended to limit the invention in any way.It is all according to invention skill Art any simple modification, change and equivalence change substantially to the above embodiments, still fall within technical solution of the present invention Protection scope in.

Claims (9)

1. it is a kind of use the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages, which is characterized in that the technique include with Lower step:
Step 1: solid block pre-treatment containing feedstock hydrocarbon: powder is made containing feedstock hydrocarbon in solid block using dry grinding method End, or solid block is made containing feedstock hydrocarbon by slurry using wet grinding method;
Step 2: material gasification: containing the gentle agent of feedstock hydrocarbon, to pass through overhead multiple flow passages respectively one-jet containing hydrocarbon original Stream road and gasifying agent runner, which are sent into reactor, to be mixed, and then reaction is generated containing the raw gas being mingled with;It is described to contain hydrocarbon original Material is that gaseous state contains feedstock hydrocarbon, liquid containing one or more of powder or slurry obtained in feedstock hydrocarbon, step 1; The main component of the high temperature rough gas is CO and H2;It is described to be mingled with containing the complete organic matter of unreacted in feedstock hydrocarbon and to contain The mixture of the inorganic substances contained in feedstock hydrocarbon;
Step 3: product purifies: being water-cooled what is generated in step 2 containing the raw gas being mingled with, then remove by washing with water Being mingled in raw gas is gone, raw gas is obtained;
Step 4: usage on black water: being produced what the cooling procedure as described in step 3 generated in the process containing grey cooling water and water washing The Heisui River of the raw composition containing grey washing water is successively concentrated, is filtered and heat recovery, and buck, part of buck conduct are obtained Waste water outlet, remaining buck is after heat recovery for the water washing in step 3.
2. it is according to claim 1 a kind of using the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages, it is special Sign is that gasifying agent described in step 2 is high purity oxygen gas, and the bulk purity of the high purity oxygen gas is 90%~99.8%.
3. it is according to claim 1 a kind of using the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages, it is special Sign is that the single injector of overhead multiple flow passages described in step 2 has multiple flow passages structure, the number of runner in the multiple flow passages structure Amount is 3+2n, and wherein n is the positive integer not less than 1, and the center flow channels in the multiple flow passages structure are gasifying agent runner, and therefrom Heart runner is successively successively arranged alternately according to the sequence of runner containing feedstock hydrocarbon, gasifying agent runner outward.
4. it is according to claim 3 a kind of using the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages, it is special Sign is, will contain feedstock hydrocarbon using feedstock hydrocarbon pressurized equipment and be placed in gas by mutually independent pipeline containing feedstock hydrocarbon feeding In a multiple flow passages nozzle for changing reactor top middle position;The feedstock hydrocarbon pressurized equipment is that double acting feedstock hydrocarbon adds Press pump and single-acting feedstock hydrocarbon force (forcing) pump or double acting feedstock hydrocarbon force (forcing) pump.
5. it is according to claim 4 a kind of using the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages, it is special Sign is that the double acting feedstock hydrocarbon force (forcing) pump is reciprocating double-action diaphragm pump, and the reciprocating double-action diaphragm pump is logical Two different runners containing feedstock hydrocarbon will be delivered to containing feedstock hydrocarbon by overregulating two sides diaphragm cavity, described two different carbon containing Flow ratio in hydrogen feedstock runner containing feedstock hydrocarbon is 1~2, and the double acting feedstock hydrocarbon pumps while conveying or stopping convey Containing feedstock hydrocarbon.
6. it is according to claim 1 a kind of using the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages, it is special Sign is that the flow proportional range of the gentle agent containing feedstock hydrocarbon described in step 2 is 0.001~0.003, when containing hydrocarbon original The flow proportional of material and gasifying agent carries out protection cutting when deviateing the range, stops the feeding of the gentle agent containing feedstock hydrocarbon.
7. it is according to claim 1 a kind of using the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages, it is special Sign is that, containing gaseous state when containing feedstock hydrocarbon is contained in feedstock hydrocarbon described in step 2, the gaseous state can pass through gas containing feedstock hydrocarbon Agent runner is sent into reactor.
8. it is according to claim 3 a kind of using the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages, it is special Sign is, it is described reactor is sent by overhead multiple flow passages nozzle containing feedstock hydrocarbon gentle agent during, be not used by Runner containing feedstock hydrocarbon and gasifying agent runner in be filled with inert gas, and inert gas to reactor direction flow.
9. it is according to claim 1 a kind of using the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages, it is special Sign is, the detailed process of heat recovery described in step 4 are as follows: filtered Heisui River is carried out vacuum flashing, the water in Heisui River Gasification forms flash steam after flash steam being carried out with water for water washing in a manner of direct contact heat transfer and described in step 3 Heat exchange.
CN201910451355.5A 2019-05-28 2019-05-28 It is a kind of to use the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages Pending CN110129098A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201910451355.5A CN110129098A (en) 2019-05-28 2019-05-28 It is a kind of to use the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201910451355.5A CN110129098A (en) 2019-05-28 2019-05-28 It is a kind of to use the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages

Publications (1)

Publication Number Publication Date
CN110129098A true CN110129098A (en) 2019-08-16

Family

ID=67582281

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201910451355.5A Pending CN110129098A (en) 2019-05-28 2019-05-28 It is a kind of to use the one-jet gasification process containing feedstock hydrocarbon of overhead multiple flow passages

Country Status (1)

Country Link
CN (1) CN110129098A (en)

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102011008187A1 (en) * 2011-01-10 2012-07-12 Bodo M. Wolf Process for the production of fuel and synthesis gas
CN203613158U (en) * 2012-11-23 2014-05-28 新奥气化采煤有限公司 Nozzle, gasifier and carbonaceous organic matter gasification system
CN104694170A (en) * 2015-03-25 2015-06-10 西北化工研究院 Method for producing synthesis gas with carbon powder and natural gas/methane as raw materials
CN106939175A (en) * 2017-04-19 2017-07-11 神华集团有限责任公司 Gasification burner tip and gasification installation
CN107629820A (en) * 2017-09-22 2018-01-26 中国华能集团公司 A kind of gasification furnace and gasification process suitable for pluralities of fuel co-gasification
CN108728168A (en) * 2017-04-14 2018-11-02 航天长征化学工程股份有限公司 A kind of gasification burner tip
CN208586257U (en) * 2018-06-25 2019-03-08 新奥科技发展有限公司 Starch coupled gasification furnace burner

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102011008187A1 (en) * 2011-01-10 2012-07-12 Bodo M. Wolf Process for the production of fuel and synthesis gas
CN203613158U (en) * 2012-11-23 2014-05-28 新奥气化采煤有限公司 Nozzle, gasifier and carbonaceous organic matter gasification system
CN104694170A (en) * 2015-03-25 2015-06-10 西北化工研究院 Method for producing synthesis gas with carbon powder and natural gas/methane as raw materials
CN108728168A (en) * 2017-04-14 2018-11-02 航天长征化学工程股份有限公司 A kind of gasification burner tip
CN106939175A (en) * 2017-04-19 2017-07-11 神华集团有限责任公司 Gasification burner tip and gasification installation
CN107629820A (en) * 2017-09-22 2018-01-26 中国华能集团公司 A kind of gasification furnace and gasification process suitable for pluralities of fuel co-gasification
CN208586257U (en) * 2018-06-25 2019-03-08 新奥科技发展有限公司 Starch coupled gasification furnace burner

Similar Documents

Publication Publication Date Title
CA2515238C (en) Process for preparing 4-aminodiphenylamine
CN1994865B (en) Gasification device for two-stage gasification coupled with heat recovery and washing and its uses
CN105152509B (en) The supercritical processing methods of supercritical reaction device, supercritical reaction system and sludge
CN101293873B (en) Optimized melamine and alkali joint production method
CN101050390B (en) CO conversion technique matched to coal gasification
CN102352268B (en) Method for producing synthesis gas by using coal powder as raw material
EP2448664B1 (en) Process for producing steam using heat recovered from a polymerization reaction
CN103100365B (en) Plasma cracking carbonaceous material reactor system with hollow cathode or double hollow cathodes
CN102701923B (en) System device and process for preparing polymethoxy dimethyl ether
CN102557134B (en) Fluidized reduction furnace for producing high-purity vanadium trioxide and production method
CN102249461A (en) Supercritical water oxidation treatment system for high-salt high-chlorine organic wastewater
CN101508466A (en) High-efficiency, energy-conservation and clean method for producing chromate
CN101463021B (en) Method and equipment for automatically and continuously producing furfuryl alcohol
CN102219754B (en) Energy-saving and resource-saving system and process for producing melamine by using gas-phase quenching process
WO2011035555A1 (en) Comprehensive process and equipment for use of carbonaceous organic matter
CA2973506C (en) System and method for producing high-purity vanadium tetraoxide powder
CN102585211B (en) Continuous production method for amino end-capped polyether
CN101058404A (en) Biomass castoff supercritical water fluid bed partial oxidation hydrogen-preparation device and method
CN101293812A (en) Technique for joint production of methanol and natural gas with methyl hydride containing synthesis gas
CN102730917B (en) Low-water-content dehydrated sludge direct supercritical water gasification processing apparatus and method
AU2016212538A1 (en) System and method for preparing high-purity divanadium pentoxide powder
CN104774663B (en) One-step method coal synthetic natural gas and its system
US10195671B2 (en) System for preparing nanoparticles by supercritical hydrothermal synthesis
CN102502646B (en) Equipment and method for preparing polysilicon by fast circulating fluidized bed-based chemical vapor deposition
CN104130215B (en) The method of hydrogen peroxide direct oxidation propylene continuous preparation of epoxypropane

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination