WO2012097593A1 - 固体物料蒸发脱水方法 - Google Patents

固体物料蒸发脱水方法 Download PDF

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Publication number
WO2012097593A1
WO2012097593A1 PCT/CN2011/078819 CN2011078819W WO2012097593A1 WO 2012097593 A1 WO2012097593 A1 WO 2012097593A1 CN 2011078819 W CN2011078819 W CN 2011078819W WO 2012097593 A1 WO2012097593 A1 WO 2012097593A1
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Prior art keywords
digester
steam
solid material
water
outlet
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PCT/CN2011/078819
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English (en)
French (fr)
Inventor
徐斌
褚腊林
马红松
Original Assignee
Xu Bin
Chu Lalin
Ma Hongsong
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Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=44031254&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=WO2012097593(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Application filed by Xu Bin, Chu Lalin, Ma Hongsong filed Critical Xu Bin
Priority to EP11855992.1A priority Critical patent/EP2666847A4/en
Priority to US13/980,662 priority patent/US20130340274A1/en
Priority to AU2011356465A priority patent/AU2011356465B2/en
Publication of WO2012097593A1 publication Critical patent/WO2012097593A1/zh

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/26—Multiple-effect evaporating
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
    • C10L5/04—Raw material of mineral origin to be used; Pretreatment thereof
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10F—DRYING OR WORKING-UP OF PEAT
    • C10F5/00—Drying or de-watering peat
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B3/00—Drying solid materials or objects by processes involving the application of heat
    • F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
    • F26B3/06—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/06—Heat exchange, direct or indirect
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/08—Drying or removing water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/14—Injection, e.g. in a reactor or a fuel stream during fuel production
    • C10L2290/146—Injection, e.g. in a reactor or a fuel stream during fuel production of water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/14—Injection, e.g. in a reactor or a fuel stream during fuel production
    • C10L2290/148—Injection, e.g. in a reactor or a fuel stream during fuel production of steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/46—Compressors or pumps
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B2210/00—Drying processes and machines for solid objects characterised by the specific requirements of the drying good

Definitions

  • This invention relates to a process for dewatering solid materials. Background technique
  • Lignite is a coal with a lower degree of coalification. Its water content is high, it is easily weathered in the air, and contains a certain amount of primary humic acid. The volatile content is generally between 45-55%. Because lignite has high water content, low calorific value, easy weathering and spontaneous combustion, the transportation cost per unit of energy is high, which is not conducive to long-distance transportation and storage. The thermal efficiency of lignite direct combustion is also very low. Lignite as a feedstock needs to reduce the moisture in the coal to less than 10% during liquefaction, retorting and gasification. Therefore, the processing of lignite upgrading is called the key to the efficient development and utilization of lignite.
  • lignite upgrading refers to the change in the composition and structure of coal in the process of dehydration, molding and thermal decomposition of lignite, and conversion into upgraded coal with similar properties of bituminous coal.
  • Various existing lignite quality technology "lignite ⁇ ; ⁇ On the Present Situation and lignite technology development trend of China" (the second phase of the Shenhua Technology: Jun-Jie Shao --2009 April 2009) in an article with a more comprehensive description .
  • the most relevant to the present invention are the D-K non-evaporative dehydration process and the K-fuel technology.
  • Japan Power Development Corporation (D) and Chuan// 21 1, h Saki Heavy Industries (K) began research and successfully developed D-K non-evaporative dehydration process in 1976.
  • the D-K dewatering process can achieve the heating of lignite water under non-evaporation conditions, so that the water can be removed from the lignite in a liquid state, and the coal quality change is similar to natural coalification.
  • K-fuel technology which is the invention patent of KFx Company of the United States, "Method and device for hot-rolling carbonaceous raw materials" (Chinese Patent Publication No.: CN 1989227A), in which the carbonaceous raw materials are subjected to a pressurized steam environment. Heat upgrade to remove moisture and other by-products.
  • a variety of water/solid separation devices can be used in the processing vessel to maximize The water is removed from the upgraded charge.
  • the heating medium suction nozzle and the processing chamber venting strategy are designed on the processing vessel wall to minimize shorting of the heating medium to the container vent and continuously remove hot water from the charging and condensing steam to remove it from the processing vessel
  • the raw material does not carry free water when it is discharged.
  • the charge can then be rehydrated to improve stability during transport and storage.
  • the cooking device disclosed in the patent CN 1989 227 A has a complicated structure, in particular, a device in which a gas, a liquid and a solid are separated from each other is carried out by a separately provided liquid separator comprising a porous rotary table or a porous cone located inside the device and The porous tube and the separation table at the bottom of the device, wherein only the porous tube serves as a liquid-solid separation, and the porous rotary table and the separation table occupy the internal space of the device, and the patent requires that the porous rotary table and the separation table can be rotated.
  • the perforated pipe only serves as a drainage, and the inflow and out of steam relies on the provision of a plurality of steam inlets and steam outlets along the height of the apparatus, which also complicates the apparatus.
  • the patented method does not preheat the raw materials by using flash steam and hot water generated in the cooking, and therefore, the steam (thermal energy) consumption is high (about 2-3 times that of the patented technology).
  • the K-fuel technology digester is provided with upper and lower lock buckets, continuous cooking, intermittently entering (rowing) materials, and the material containing lignite passes through the lock valve under differential pressure, and the solid matter in the material wears out the valve greatly; Before the discharge bucket is discharged, it is difficult to discharge the free water first, which has a negative impact on the efficiency.
  • the D-K non-evaporative dehydration technology can only achieve semi-continuous operation at present, which affects the production capacity and operational stability of the device, and the lignite water content after cooking is still high, and the water content needs to be further reduced.
  • the invention relates to a method for multi-effect evaporation dehydration of a solid material, comprising: providing a plurality of digester, wherein the plurality of digester are connected in parallel for the flow direction of the solid material, wherein each digester is repeatedly executed
  • the following steps are arranged in chronological order:
  • At least a portion of the digester further comprises a step ix between the above steps vi i and vi ii: vacuuming the digester to further evaporate residual moisture in the solid material, further reducing The moisture content of the solid material.
  • condensed water from other digesteres in steps ⁇ and / or iii and / or iv is used as the hot water and / or separately from the water heater Providing the hot water for the digester to perform Step i; and/or, using the fourth steam from another digester as the first steam to cause the digester to perform step ii; and/or, using the third steam from other digester
  • the second steam is used to cause the digester to perform step iii; and/or the saturated steam discharged from step V of the other digester is used as the saturated steam in step iv of the digester.
  • FIG. 1 is a schematic process flow diagram of an embodiment of the present invention.
  • the drawings are for illustrative purposes only and are not intended to limit the scope of the invention in any way. Detailed description of the invention
  • the solid material is an aqueous solid material such as lignite.
  • Natural lignite contains a large amount of water.
  • the lignite is a lignite that has been washed and leached by water having a temperature greater than 30, which also contains a large amount of water, and it is desirable to remove the water therein.
  • the solid material is preferably in the form of a block or a granule.
  • the steam described in the present invention means water vapor.
  • the timing of entry may be entered at the same time or staggered from each other for a period of time, preferably offset from each other for a period of time.
  • the solid materials are separately treated in each digester, and the solid materials after the treatment are discharged from the respective digester, the discharge timing can be simultaneously discharged, or the discharge timing is also shifted from each other for a period of time, preferably shifted from each other for a period of time.
  • the discharged solid material enters a common downstream process.
  • the period of time may be performed sequentially according to each of the digester described below The time taken for each step of the steps is specifically determined by those skilled in the art.
  • Each of the digester of the present invention comprises a solids material inlet, a solids material outlet, a steam inlet, a steam outlet, a hot water inlet, and a condensate outlet.
  • the solid material inlet is disposed near the top of the digester
  • the solid material outlet and the condensate outlet are disposed near the bottom of the digester
  • the steam inlet and the steam outlet may be disposed at any suitable location on the digester, such as in the digester The upper part.
  • the hot water inlet can also be placed in any suitable location on the digester, for example in the lower middle of the digester.
  • the condensate outlet and the vapor outlet may be combined into one outlet, and preferably disposed adjacent the bottom of the digester.
  • the digester has a lock valve connected to the solid material inlet, and the lock valve is connected to the three-way ball valve and the lower hopper, and the solid material is sequentially taken from the solid material inlet through the lower hopper, the three-way ball valve and the lock valve.
  • the solid material outlet of the digester is connected to the lower lock valve, and the lower lock valve is connected to the lower hopper and the distributor in turn.
  • the remaining respective outlets or inlets are connected to respective discharge lines such as drain lines and exhaust lines or supply lines such as water supply lines and supply lines. All of these auxiliary devices and corresponding lines are arranged in a manner that is capable of achieving the objects of the present invention.
  • Each of the digester repeatedly performs the following steps in chronological order: i.
  • the solid material and hot water are charged, and the solid material is first heated with the hot water.
  • the solid material is charged into the digester from the inlet of the solid material, and after loading to a certain level, the charging is stopped and the solid material inlet is closed.
  • Hot water is introduced into the digester through the hot water inlet before, during or after charging.
  • the hot water is water having a temperature higher than the solid material.
  • the hot water may be hot water provided by a water heater alone or may be condensed water discharged from other digester in steps ii and / or iii and / or iv.
  • condensed water discharged from other digester in steps ⁇ and / or iii and / or iv.
  • the hot water After the hot water reaches the desired liquid level, the supply of hot water is stopped and the hot water inlet is closed. After the hot water sufficiently heats the solid material, the used hot water may preferably be discharged to the digester via the condensed water outlet, and the discharged hot water may be used for other purposes, for example, for the original
  • the solid material is subjected to a washing and leaching treatment to remove fine powder and sulfur contained therein.
  • the used hot water may not be discharged in the step i, and the following steps ⁇ or i are performed under the action of the pressure of the first steam or the second steam and the step ii or iii.
  • the generated condensed water is discharged together.
  • the first vapor is passed from the steam inlet.
  • the first vapor has a first enthalpy value, which will be compared below for the enthalpy order of the individual vapors used in the present invention.
  • a portion of the first vapor undergoes a phase change to become condensed water, which is discharged from the condensed water outlet during the step ⁇ .
  • the source of the first steam is not limited as long as it has the first threshold.
  • the fourth steam described below from other digester is used as the first steam.
  • the second steam is also passed through the steam inlet.
  • the second vapor has a second enthalpy value, which will be compared below for the enthalpy order of the individual vapors used in the present invention.
  • a portion of the second vapor undergoes a phase change to become condensed water, which is discharged from the condensed water outlet during the step iii.
  • the source of the second steam is not limited as long as it has a second enthalpy value.
  • the third steam described below from other digester is used as the second steam.
  • the saturated steam refers to water vapor at a certain temperature at a saturated vapor pressure corresponding to the temperature.
  • the predetermined heating temperature may be any desired temperature, which is greater than ⁇ , and the specific value may be set as needed.
  • the saturated steam is also passed from the steam inlet to the digester.
  • the source of saturated steam is not limited as long as it is saturated steam and its enthalpy is higher than the second enthalpy.
  • the saturated steam discharged from step V of the other digester is used as the saturated steam in step iv of the digester.
  • the superheated steam refers to steam obtained by continuously increasing the temperature on the basis of saturated steam, and its enthalpy is higher than that of saturated steam. After the superheated steam is introduced, the superheated steam heats the solid material to evaporate the water in the solid material, while the temperature of the superheated steam decreases to become saturated steam, and the evaporated water also becomes saturated steam, which is in the cooking process.
  • the digester is discharged through the saturated steam outlet, and the discharged saturated steam can be used in other digester in step iv, so that the heat energy of the partially saturated steam can be fully utilized.
  • the superheated steam may be passed through the steam inlet as described above or may be passed through a separate superheated steam inlet.
  • no new condensed water is produced in this step V, but in actual production, the drainage is not smooth due to the clogging of the coal ash, and there may be some condensed water that has not been drained in the previous steps, so it continues to pass in this step.
  • the condensate outlet exits the condensate.
  • Step V is carried out for a predetermined period of time which can be specifically determined based on a number of specific factors such as the superheated steam enthalpy, the desired water content of the solid material, and the pressure in the digester.
  • the third steam By opening the steam outlet to discharge the steam in the digester outward, the steam discharged during the decompression process is referred to herein as the third steam, and the temperature of the third steam from the digester during the decompression discharge process
  • the saturated state under the condition becomes an unsaturated state.
  • the water in the solid material also undergoes flashing, and a part of the steam is generated, further reducing the moisture content in the solid materials, and the steam generated by the vacuum flashing is also included in the The third steam then exits the digester.
  • the third steam can be passed to the other digester in step iii to act as the second steam in the other digester, while simultaneously between the digester in step vi and the digester in step iii After the pressure is equalized, the first decompression is completed after the pressures of the two digester are consistent.
  • the retort is subjected to a second decompression, and the fourth steam is discharged.
  • the second decompression is performed by opening the steam outlet to discharge the steam in the digester, and the decompression process is discharged.
  • Steam is called the fourth steam.
  • the decompression progresses, the water in the solid material continues to flash, producing a portion of the steam, which further reduces the moisture content of the solid material.
  • the steam generated by this decompression flash is also included in the The fourth steam is introduced and then discharged to the digester.
  • the fourth steam can be passed to another digester in step ⁇ to act as the first steam in the other digester, while simultaneously bringing the digester in step vi i to the digester in step ii
  • the pressure equalization is performed. After the pressures of the two digester are consistent, the second pressure reduction is completed, and the pressure in the digester is already close to the normal pressure.
  • At least a portion of the digester further includes a step ix between the step V ii and the step V iii: vacuuming the digester to continue evaporating the remaining water in the solid material. Further reduce the moisture content of the solid material.
  • the evacuation is carried out through a vacuum port provided on the digester.
  • the vacuum port may be a separately provided vacuum port, or may be used as a vacuum port by using existing outlets or inlets.
  • any one of the solid material inlet, the steam outlet, the hot water inlet, and the condensate outlet serves as a vacuuming port, and more preferably the solid material outlet and the condensed water outlet are used as a vacuuming port, most preferably
  • the condensed water outlet is also used as a vacuum port, which has the advantage that under the action of vacuuming, the condensed water which is difficult to discharge under non-vacuum conditions can be discharged as much as possible or even drained.
  • a certain degree of negative pressure is achieved in the digester by evacuation, for example, a gauge pressure of -80 to -90 kPa, which promotes further evaporation of moisture in the solid material, further reducing the moisture content of the solid material. This vacuuming process is performed for a predetermined time.
  • condensed water from other digesteres in steps ⁇ and / or iii and / or iv is used as the hot water and / or separately Providing the hot water by a water heater to cause the digester to perform step i; and/or using the fourth steam from another digester as the first steam to cause the digester to perform a step; and / Or, the third steam from another digester is used as the second steam to cause the digester to perform step iii; and/or the saturated steam discharged from step V of the other digester is used as the digester The saturated steam in step iv.
  • the benefit of this is that it takes full advantage of the condensate and the heat of the various steams to maximize thermal efficiency.
  • the order of enthalpy of various steams is as follows: superheated steam > saturated steam > third steam > fourth steam; or, superheated steam > saturated steam > second steam > first Steam.
  • the number of digester and the steps of each digester are adjusted to achieve that at least one digester is always performing step i at each moment, at least one digester is performing step ii, ..., and so on, ... at least one digester is performing step vi ii.
  • at least one digester is also being subjected to step ix.
  • Each outlet and inlet on each digester is adjusted during each step so that its open or closed condition meets the requirements for achieving each step.
  • the steam lines, water lines and valves between the digester are arranged and adjusted so that the flow of the desired steam and condensate can be carried out between the digester as needed.
  • the arrangement and adjustment of such outlets, inlets, lines and valves are well known to those skilled in the art and will not be described again. This allows a substantially continuous cooking operation to be carried out as a whole.
  • Figure 1 schematically shows an exemplary diagram of a plurality of digester parallel connections and a piping and valve arrangement between the digester, wherein the piping and valve arrangements are arranged as required to achieve the objectives of the present invention.
  • piping and valve arrangements are arranged as required to achieve the objectives of the present invention.
  • Those skilled in the art can implement such an arrangement, and the arrangement is not limited to the specific manner shown in the drawings.
  • the "plurality” in the present invention is at least 2, for example 6, 6, for example 8, 9, or more. It should be noted that although the drawings and the following embodiments are exemplified by 8 or 9 digesters, this is merely for convenience of the embodiment and easy to understand the present invention, and does not mean that it must be 8
  • the method of the invention can be achieved or continuously achieved by one or nine digester.
  • the plurality of the plurality described in the present invention is at least two.
  • One skilled in the art will calculate the number of digester specifically employed to achieve the continuous operation of the method of the present invention based on the specific time required for each step.
  • the following examples are only intended to illustrate the technical solutions of the present invention, and are not intended to limit the scope of the present invention in any way.
  • each digester The steps of each digester are as shown in Figure 1. Eight digester units are provided, numbered 1-8, respectively.
  • the aqueous lignite passes through the weighing system, the unloader and the belt conveyor in turn, from the lower hopper at the top of each digester.
  • the three-way ball valve and the locking valve respectively enter the eight digester, and each digester repeatedly performs the steps i-vi ii described herein in chronological order, and at any one time, each digester
  • the operations performed are as follows: digester 1 proceeds to step i, digester 2 proceeds to step ii, ... and so on..., digester 8 proceeds to step vi ii without vacuuming.
  • the saturated steam discharged from the digester 5 is used as the saturated steam of the digester 4
  • the third steam discharged from the digester 6 is used as the second steam in the digester 3 until the pressure equalization is reached between the two digester
  • the fourth steam discharged from the digester 7 is used as the first steam in the digester 2 until a pressure equalization is reached between the two digester.
  • Step vi is carried out for 30 minutes, and the pressure of saturated steam (containing non-condensable gas such as volatiles in coal) is 4.
  • OMPa gauge pressure, all pressures in this paper are gauge pressure
  • the temperature is 230 ⁇ 252* €
  • the corresponding saturated steam (100% steam) pressure is 2.7 - 4.
  • step v is carried out for 15 minutes, the temperature of the superheated steam introduced is 400, and the pressure is 4 MPa.
  • the upgraded lignite is discharged from the solid material outlet of each digester and reaches the belt through the lower lock valve, the lower hopper and the distributor. The machine is sent to the machine and then sent to the subsequent process.
  • Table 1 The properties of lignite raw coal and upgraded coal are shown in Table 1 below: Table 1
  • the dry basis refers to the mass of the coal after drying to complete dehydration as the denominator when calculating the percentage content of each substance
  • the dry ashless base refers to the quality of the coal after drying and dehydrating and removing ash when calculating the percentage content of each substance.
  • the receiving base is based on the coal received.
  • the temperature of the coal discharged from step vi i i is 100-110.
  • each digester is as shown in Figure 1, but nine digester are provided, numbered 1-9, respectively.
  • the water-containing lignite enters the 9 digester separately, and each digester is repeatedly executed in chronological order.
  • Said step i-ix, and at any one time, the operation performed by each digester is as follows: digester 1 performs step i, digester 2 performs step ii, ... and so on..., digester 8 proceeds to step vi ii
  • the digester 9 proceeds to step iv.
  • the saturated steam discharged from the digester 5 is used as the saturated steam of the digester 4
  • the third steam discharged from the digester 6 is used as the second steam in the digester 3 until the pressure equalization is reached between the two digester
  • the fourth steam discharged from the digester 7 The steam is used as the first steam in the digester 2 until a pressure equalization is achieved between the two digester.
  • the pressure of the saturated steam (containing non-condensable gas such as volatiles in coal) is 4. OMPa, the temperature is 230 ⁇ 252 ⁇ , and the corresponding saturated steam (100% water vapor) pressure is 2. 7 - 4.
  • step v is carried out for 20 minutes, the temperature of the superheated steam is 400* €, and the pressure is 4 MPa; the relative vacuum in step ix is -0.08 MPa, vacuum treatment for 30 minutes.
  • the properties of the raw coal and the upgraded coal are as shown in Table 2 below, and the temperature of the coal discharged from the step vi ii is 70-80X.
  • each digester is as shown in Figure 1, but nine digester are provided, numbered 1-9, respectively.
  • the water-containing lignite enters the 9 digester separately, and each digester is repeatedly executed in chronological order.
  • Said step i-ix, and at any one time, the operation performed by each digester is as follows: digester 1 performs step i, digester 2 performs step ii, ... and so on..., digester 8 proceeds to step vi ii
  • the digester 9 proceeds to step iv.
  • the saturated steam discharged from the digester 5 is used as the saturated steam of the digester 4
  • the third steam discharged from the digester 6 is used as the second steam in the digester 3 until the pressure equalization is reached between the two digester
  • the fourth steam discharged from the digester 7 is used as the first steam in the digester 2 until a pressure equalization is reached between the two digester.
  • the step vi is carried out for 10 minutes, and the pressure of the saturated steam (containing non-condensable gas such as volatiles in coal) is 4. OMPa, the temperature is 230 ⁇ 252 ⁇ , and the corresponding saturated steam (100%) The water vapor) pressure is 2. 7 - 4.
  • step v is carried out for 10 minutes, the temperature of the superheated steam is 400* €, the pressure is 4 MPa; the relative vacuum in step ix is -0. 08MPa, vacuum treatment 30 minutes.
  • the properties of the raw coal and the upgraded coal are shown in Table 3 below, and the temperature of the coal discharged from step vi ii is 65-75 X.
  • each digester is as shown in Figure 1, but nine digester are provided, numbered 1-9, respectively.
  • the water-containing lignite enters the 9 digester separately, and each digester is repeatedly executed in chronological order.
  • Said step i-ix, and at any one time, the operation performed by each digester is as follows: digester 1 performs step i, digester 2 performs step ii, ... and so on..., digester 8 proceeds to step vi ii
  • the digester 9 proceeds to step iv.
  • the saturated steam discharged from the digester 5 is used as the saturated steam of the digester 4
  • the third steam discharged from the digester 6 is used as the second steam in the digester 3 until the pressure equalization is reached between the two digester
  • the fourth steam discharged from the digester 7 is used as the first steam in the digester 2 until a pressure equalization is reached between the two digester.
  • Step vi is carried out for 20 minutes, and the pressure of the saturated steam (containing non-condensable gas such as volatiles in coal) is 3. OMPa, the temperature is 210 ⁇ 235 ⁇ , and the corresponding saturated steam (100% water vapor) pressure is 1. 8-3.
  • Step v is carried out for 20 minutes, the temperature of the superheated steam is 400" €, the pressure is 3 MPa; the relative vacuum in step ix is -0.08 MPa, vacuum treatment for 30 minutes.
  • Raw coal and shield The properties of the coal after the following table As shown in 4, the temperature of the coal discharged from step vi ii is 70-80X.
  • the enthalpy of superheated steam is used step by step to heat and evaporate the solid material, and the thermal efficiency is high.
  • the utilization of thermal energy has five effects.
  • the first effect is to use the heat of the superheated steam to change to the dry steam to heat the solid material; the second effect is to use the saturated steam to heat the solid material; the third effect, using the first decompression to generate the third The steam heats the solid material; the fourth effect is to heat the solid material by using the fourth steam generated by the second decompression; and the fifth effect, using the condensed water as the hot water to heat the solid material.
  • the evacuation of the present invention causes the process of evaporating residual moisture to additionally correspond to the evaporation effect of the sixth effect, which further reduces the moisture content in the solid material and lowers the temperature of the final discharge.
  • lowering the temperature of the final discharge is advantageous for preventing spontaneous combustion of the lignite after the shield is lifted.
  • the multi-effect evaporation dehydration process of the invention can be carried out continuously by providing a plurality of digester and rationally arranging the pipe connection relationship between them, which is advantageous for industrial applications.

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Description

固体物料蒸发脱水方法
发明领域
本发明涉及使固体物料脱水的方法。 背景技术
褐煤是煤化程度较低的煤种， 其含水量 ^艮高， 在空气中容易风 化， 含有一定量的原生腐殖酸， 挥发份含量一般在 45-55%之间。 由于褐煤水份高， 热值低， 易风化自燃， 单位能量的运输成本高， 不利于长距离输送和储存。 褐煤直接燃烧热效率也很低。 褐煤作为 原料在液化、 干馏和气化过程中都需要把煤中的水份降至 10%以 下。 故褐煤提质加工称为褐煤高效开发利用的关键。 所谓褐煤提质 是指褐煤在脱水、 成型和热分解等过程中， 煤的组成和结构发生变 化， 转化成具有近似烟煤性质的提质煤。 现有的各种褐煤提质技术 在《褐煤^;技术现状及我国褐煤^^技术发展趋势初探》 （神华 科技第二期 作者： 邵俊杰 -2009年 4月）一文中有了比较全面的描 述。
同本发明最相关的主要有 D-K非蒸发脱水工艺和 K-燃料技 术。 日本电源开发公司（D)和川了 /; 21 1, h 崎重工公司（K)从 1976年开始研究并成功开发出了 D— K非蒸发脱水工艺。 D— K脱 水工艺可实现褐煤水份在非蒸发条件下加热，使水份以液体状态从 褐煤中脱出， 其煤质变化类似天然的煤化作用。
K-燃料技术， 即美国 KFx公司的发明专利 《含碳原料热拔 ^ 的方法和装置》 （中国专利公开号： CN 1989227A ) , 该技术方案 中， 对含碳原料在加压蒸汽环境中进行热提质， 以去除水份和其它 副产品。加工容器中可以采用多种水 /固体分离装置， 以尽量多地从 被提质的装料中去除水份。加热介质吸入喷嘴和加工室通气口策略 设计在加工容器壁上， 以尽量减少加热介质至容器排气口的短路， 并连续地从装料和凝结蒸汽中去除热水，使得从加工容器中去除的 原料在排出时不携带游离水份。 后， 可以对装料进行再水 合， 以提高运输和储存过程中的稳定性。
但上述技术都存在着缺点。专利 CN1989227A公开的蒸煮装置 结构复杂， 尤其是其中使气体、 液体和固体彼此分离的设备要靠单 独设置的液体分离器来进行，该液体分离器包括位于装置内部的多 孔旋转台或多孔锥体和多孔管以及位于装置底部的分离台，其中仅 多孔管起到了液固分离作用， 而多孔旋转台和分离台则严重占用了 装置的内部空间， 而且该专利中要求多孔旋转台和分离台可旋转， 则还需要在装置内配备相应的动力设备和传动设备，且还要使这些 动力设备和传动设备能耐受装置内的高温和高压，进一步使装置复 杂化。 此外， 该专利中， 多孔管仅起到排水作用， 而蒸汽的进出则 要依靠沿装置高度方向上设置有多个蒸汽入口和蒸汽出口，这也使 装置复杂化。且该专利方法没有利用蒸煮中产生的闪蒸汽和热水对 原料进行预热， 因此， 生蒸汽（热能）消耗高（大约是本专利技术 的 2-3倍）。 此外， K-燃料技术蒸煮器设有上、 下两个锁斗， 连续 蒸煮， 间断进（排）料， 含有褐煤的物料在差压下通过锁阀， 物料 中的固体物质对阀门磨损大； 下锁斗在排料前， 难以做到将游离水 先排尽， 对^;效率产生负面影响。
而 D - K非蒸发脱水技术目前只能实现半连续操作，这影响了 装置的生产能力和运行稳定性， 且其蒸煮后的褐煤水含量仍然较 高， 有待于进一步降低水含量。
故人们希望能进一步开发褐煤提质技术以克服上述缺点。 发明概述
本发明涉及一种对固体物料进行多效蒸发脱水的方法，包括： 提供多个蒸煮器， 所述多个蒸煮器就所述固体物料的流向来 说为并联连接 , 其中每个蒸煮器反复执行按时间先后顺序排列的 以下步骤：
i、装入所述固体物料和热水，用所述热水对固体物料进行第 一次加热；
i i、 通入第一蒸汽对固体物料进行第二次加热， 并排出此步 骤中所产生的冷凝水；
i i i、通入第二蒸汽以对固体物料进行第三次加热， 并排出此 步骤中所产生的冷凝水；
iv、 通入饱和蒸汽以对固体物料进行第四次加热， 使固体物 料达到预定加热温度， 并排出此步骤中所产生的冷凝水；
v、 通入过热蒸汽对达到预定加热温度的固体物料进行蒸煮， 使固体物料中所含的水份蒸发，同时所述过热蒸汽变为饱和蒸汽， 蒸煮过程中排出该饱和蒸汽；
vi、 对蒸煮器进行第一次减压， 并排出第三蒸汽；
vi i、 对蒸煮器进行第二次减压， 并排出第四蒸汽；
vi i i、 使蒸煮器内的压力恢复至常压， 排出固体物料。
在优选的实施方案中， 至少一部分蒸煮器在其上述步驟 vi i 和步骤 vi i i之间还包括步骤 ix: 对蒸煮器进行抽真空处理， 以 使固体物料中残留的水份继续蒸发， 进一步降低固体物料中的水 份含量。
在更优选的实施方案中， 对于一部分蒸煮器来说， 将来自其 它处于步骤 Π和 /或 i i i和 /或 iv的蒸煮器所排出的冷凝水用作 所述热水和 /或单独由热水器来提供所述热水以使该蒸煮器进行 步骤 i; 和 /或， 将来自其它蒸煮器的所述第四蒸汽用作所述第一 蒸汽来使该蒸煮器进行步骤 i i ; 和 /或， 将来自其它蒸煮器的所 述第三蒸汽用作所述第二蒸汽来使该蒸煮器进行步骤 i i i ; 和 / 或， 将其它蒸煮器的步骤 V中排出的饱和蒸汽用作该蒸煮器的步 骤 iv中的饱和蒸汽。 附图简述
图 1是本发明的实施方案的示意性工艺流程图。附图仅为举 例说明的目的， 不以任何方式限制本发明的范围。 发明详述
以下详细介绍本发明的对固体物料进行多效蒸发脱水的方 法。
其中所述固体物料是含水的固体物质， 例如褐煤。 天然褐煤 中均含有大量的水份。 在优选的实施方案中， 所述褐煤是经过温 度大于 30 的水洗涤浸出后的褐煤， 其也含有大量的水份， 希望 能去除其中的水份。 所述固体物料优选为块状或颗粒状。
本发明中所述的蒸汽是指水蒸气。
为了实现本发明的方法， 要求提供多个蒸煮器， 所述多个蒸煮 器就所述固体物料的流向来说为并联连接， 即， 使来自共同的上 游工序的固体物料并联进入各个蒸煮器， 进入时机可同时进入或 者彼此错开一段时间， 优选彼此错开一段时间。 固体物料分别在 各个蒸煮器内进行处理， 处理完毕后的固体物料则从各个蒸煮器 中排出， 排出时机可同时排出， 或者排出时机也要彼此错开一段 时间， 优选彼此错开一段时间。 所排出的固体物料进入共同的下 游工序。 所述一段时间可以根据下文所述的每个蒸煮器依次执行 的各个步骤所耗费的时间由本领域技术人员具体确定。
本发明中的每个蒸煮器上包含固体物料入口、 固体物料出 口、 蒸汽入口、 蒸汽出口、 热水入口、 冷凝水出口。 其中， 固体 物料入口设置在蒸煮器顶部附近， 固体物料出口和冷凝水出口设 置在蒸煮器的底部附近， 而蒸汽入口和蒸汽出口可以设置在蒸煮 器上的任何合适的位置， 例如设置在蒸煮器的上部。 热水入口也 可以设置在蒸煮器上的任何合适的位置， 例如设置在蒸煮器的中 下部。 在优选的实施方案中， 其中冷凝水出口和蒸汽出口可以合 并成一个出口， 且优选设置在蒸煮器的底部附近。 关于该蒸煮器 内部的更详细构造， 可参见同一申请人申请的另一专利 《一种对 固体物料进行蒸煮的蒸煮器》 ， 通过引用将该专利的全文并入本 文。
有很多辅助设备与本发明的蒸煮器相连。 例如， 该蒸煮器的 固体物料入口处有上锁阀与之连接， 而上锁阀又与三通球阀和下 料斗连接， 固体物料依次经由下料斗、 三通球阀和上锁阀从固体 物料入口进入蒸煮器中， 如图 1所示。 蒸煮器的固体物料出口处 有下锁阀与之连接， 下锁阀又依次与下料斗和布料器连接。 其余 各个出口或入口与相应的排放管线例如排水管线和排汽管线或供 料管线例如供水管线和供汽管线连接。 所有这些辅助设备和相应 管线以能够实现本发明目的的方式进行布置， 这些具体布置方式 不是本发明的内容， 且也并不限于图 1中所示的具体方式。
其中每个蒸煮器反复执行按时间先后顺序排列的以下步驟： i、 装入所述固体物料和热水， 用所述热水对固体物料进行 第一次加热。 其中所述固体物料从所述固体物料入口装入所述蒸 煮器， 装填到一定料位后停止装料并关闭所述固体物料入口。 装 料之前、过程中或之后，通过热水入口向所述蒸煮器中通入热水， 所述热水是温度高于所述固体物料的水。 所述热水可以是单独由 热水器提供的热水或者可以是来自其它处于步骤 i i和 /或 i i i和 / 或 iv的蒸煮器所排放的冷凝水。 优选使用来自其它处于步骤 Π 和 /或 i i i和 /或 iv的蒸煮器所排放冷凝水。待所述热水达到期望 的液位后， 停止供入热水， 并关闭所述热水入口。 在所述热水充 分加热所述固体物料后， 可优选地经由所述冷凝水出口将用毕的 热水排出蒸煮器， 所排出的用毕的热水可以用于其它目的， 例如 用于原始固体物料进行洗涤浸出处理， 以除去其中所含的细粉和 硫份。 或者， 该用毕的热水可以在该步骤 i中暂不排出， 而待进 行以下步骤 Π或 i时，在通入的第一蒸汽或第二蒸汽的压力的 作用下与步驟 i i或 i i i中产生的冷凝水一起排出。
i i、 通入第一蒸汽对固体物料进行第二次加热， 并排出此步 骤中所产生的冷凝水。 其中所述第一蒸汽从所述蒸汽入口通入。 所述第一蒸汽具有第一焓值， 下文将对本发明中所使用的各个蒸 汽的焓值顺序进行比较。 加热过程中， 一部分第一蒸汽会发生相 变而变成冷凝水，该冷凝水在该步骤 Π过程中从所述冷凝水出口 排出。 在本发明的方法中， 对第一蒸汽的来源不做任何限制， 只 要它具有第一焓值即可。 在本发明的优选实施方案中， 将来自其 它蒸煮器的下文所述的第四蒸汽用作所述第一蒸汽。
i i i、通入第二蒸汽以对固体物料进行第三次加热， 并排出此 步骤中所产生的冷凝水； 其中所述第二蒸汽也由所述蒸汽入口通 入。 所述第二蒸汽具有第二焓值， 下文将对本发明中所使用的各 个蒸汽的焓值顺序进行比较。 加热过程中， 一部分第二蒸汽会发 生相变而变成冷凝水， 该冷凝水在该步驟 i i i过程中从所述冷凝 水出口排出。 在本发明的方法中， 对第二蒸汽的来源不做任何限 制， 只要它具有第二焓值即可。 在本发明的优选实施方案中， 将 来自其它蒸煮器的下文所述的第三蒸汽用作所述第二蒸汽。
iv、 通入饱和蒸汽以对固体物料进行第四次加热， 使固体物 料达到预定加热温度， 并排出此步骤中所产生的冷凝水。 其中所 述饱和蒸汽是指在某温度下处于该温度所对应的饱和蒸气压下的 水蒸气。 其中所述预定加热温度可以是任何想要的温度， 该温度 要大于 ιοοχ , 其具体值可以根据需要进行设定。 其中所述饱和 蒸汽也从所述蒸汽入口通入蒸煮器中。 在本发明的方法中， 对饱 和蒸汽的来源不做任何限制， 只要它是饱和蒸汽且其焓值高于所 述第二焓值即可。 在本发明的优选实施方案中， 将其它蒸煮器的 步骤 V中排出的饱和蒸汽用作该蒸煮器的步骤 iv中的饱和蒸汽。
v、 通入过热蒸汽对达到预定加热温度的固体物料进行蒸煮， 使固体物料中所含的水份蒸发，同时所述过热蒸汽变为饱和蒸汽， 蒸煮过程中排出该饱和蒸汽。 所述过热蒸汽是指在饱和蒸汽基础 上继续升高温度所获得的蒸汽， 其焓值比饱和蒸汽高。 在通入过 热蒸汽后， 过热蒸汽可加热固体物料使固体物料中的水份蒸发， 同时过热蒸汽温度降低而变成饱和蒸汽， 所蒸发的水份也变成饱 和蒸汽， 这些饱和蒸汽在蒸煮过程中通过所述饱和蒸汽出口排出 蒸煮器，所排出的饱和蒸汽可通入其它处于步骤 iv的蒸煮器中使 用， 这样可以充分利用这部分饱和蒸汽的热能。 所述过热蒸汽可 由上文所述的蒸汽入口通入， 或者由另设的过热蒸汽入口通入。 理论上此步驟 V中不再产生新的冷凝水， 但实际生产中由于煤灰 堵塞导致排水不畅， 还可能存在一些以前的步骤中所未排尽的冷 凝水， 故在这个步骤中继续通过冷凝水出口排出冷凝水。 步骤 V 进行预定的时间， 该预定的时间可根据过热蒸汽焓值、 期望的固 体物料的水含量以及蒸煮器内压力等诸多具体因素而具体确定。
vi、 对蒸煮器进行第一次减压， 并排出第三蒸汽。 所述减压 通过打开所述蒸汽出口向外排放蒸煮器内的蒸汽来进行， 本文中 将减压过程中所排出的蒸汽称为第三蒸汽， 该第三蒸汽在减压排 出过程中从蒸煮器内的温度条件下的饱和态变为不饱和态。 随着 减压的进行， 固体物料中的水份还会发生闪蒸作用， 又产生一部 分蒸汽， 进一步降低了这些固体物料中的水份含量， 减压闪蒸所 产生的蒸汽也包含在所述第三蒸汽中并随之排出蒸煮器。 该第三 蒸汽可通入处于步骤 i i i的其它蒸煮器中以充当该其它蒸煮器中 的所述第二蒸汽， 这同时使处于步骤 vi的蒸煮器与处于步驟 i i i 的蒸煮器二者之间进行均压， 待此两个蒸煮器压力达到一致后， 所述第一次减压完成。
vi i、对蒸煮器进行第二次减压， 并排出第四蒸汽。 第一次减 压完成后， 蒸煮器内还存在一定的压力， 此时， 通过打开所述蒸 汽出口向外排放蒸煮器内的蒸汽来进行第二次减压， 该减压过程 中所排出的蒸汽称为第四蒸汽。 随着减压的进行， 固体物料中的 水份继续发生闪蒸作用， 产生一部分蒸汽， 再进一步降低了这些 固体物料中的水份含量， 这次减压闪蒸所产生的蒸汽也包含在所 述第四蒸汽中并随之排出蒸煮器。该第四蒸汽可通入处于步驟 Π 的其它蒸煮器中以充当该其它蒸煮器中的所述第一蒸汽， 这同时 使处于步骤 vi i的蒸煮器与处于步驟 i i的蒸煮器二者之间进行均 压， 待此两个蒸煮器压力达到一致后， 所述第二次减压完成， 此 时蒸煮器内的压力已经接近于常压。
vi i i、 使蒸煮器恢复至常压， 排出固体物料。 其中恢复常压 的操作可通过打开任何一个口使蒸煮器与外界大气相通来进行。 待蒸煮器内压力恢复至常压后， 打开固体物料出口， 排出经过充 分脱水的固体物料。 由于该排料操作在常压下进行， 故可减轻固 体物料对出料阀门的磨损。 所排出的固体物料进入后续工段进行 其它处理。
在本发明的优选的实施方案中， 至少一部分蒸煮器在其步骤 V i i和步骤 V i i i之间还包括步骤 i x: 对蒸煮器进行抽真空处理， 以使固体物料中残留的水份继续蒸发， 进一步降低固体物料中的 水份含量。 所述抽真空通过设在蒸煮器上的抽真空口来进行。 该 抽真空口可以是一个单独设置的抽真空口， 也可以利用已有的各 出口或入口来兼作抽真空口。 优选用所述固体物料入口、 蒸汽出 口、 热水入口、 冷凝水出口中的任何一个口兼作抽真空口， 更优 选用所述固体物料出口和所述冷凝水出口来兼作抽真空口， 最优 选用所述冷凝水出口来兼作抽真空口， 这样做的好处是在抽真空 作用下， 能够将在非抽真空条件下难以排尽的冷凝水尽可能多地 排出， 甚至排尽。 通过抽真空使蒸煮器内达到一定程度的负压， 例如表压为 -80 至- 90kPa， 这可促使固体物料中的水份进一步蒸 发， 进一步降低固体物料中的水份含量。 该抽真空处理进行预定 的时间。
在本发明的更优选的实施方案中， 对于一部分蒸煮器来说， 将来自其它处于步骤 Π和 /或 i i i和 /或 iv的蒸煮器所排出的冷 凝水用作所述热水和 /或单独由热水器来提供所述热水以使该蒸 煮器进行步骤 i; 和 /或， 将来自其它蒸煮器的所述第四蒸汽用作 所述第一蒸汽来使该蒸煮器进行步骤 Π ; 和 /或， 将来自其它蒸 煮器的所述第三蒸汽用作所述第二蒸汽来使该蒸煮器进行步骤 i i i ; 和 /或， 将其它蒸煮器的步骤 V中排出的饱和蒸汽用作该蒸 煮器的步骤 iv中的饱和蒸汽。这样做的好处是充分利用了冷凝水 以及各种蒸汽的热能， 实现了热效率的最大化。
本发明中， 各种蒸汽的焓值顺序如下： 过热蒸汽>饱和蒸汽> 第三蒸汽>第四蒸汽； 或者， 过热蒸汽>饱和蒸汽>第二蒸汽〉第一 蒸汽。
对多个蒸煮器的数目和各个蒸煮器所处的步骤进行调节，以 实现每一时刻总有至少一个蒸煮器在进行步骤 i , 至少一个蒸煮 器在进行步骤 i i , ……， 以此类推， ……至少一个蒸煮器正在进 行步骤 vi i i。 在优选的实施方案中， 还使得至少一个蒸煮器正在 进行步骤 ix。并在进行各步骤时对各蒸煮器上的各个出口和入口 进行调节， 以使得其开启或关闭的状态能够满足实现各步骤时的 要求。 且对各蒸煮器之间的蒸汽管路、 水管路和阀门进行布置和 调节， 以使得各蒸煮器之间能够在需要时进行所要求的蒸汽的流 体和冷凝水的流通。 这样的出口、 入口、 管路和阀门的布置和调 节是本领域技术人员公知的， 在此不再赘述。 如此可以实现在整 体上基本连续的蒸煮操作。
图 1 示意性地示出了多个蒸煮器并联连接以及各蒸煮器之 间的管路和阀门布置的示例性图， 其中这些管路和阀门布置方式 以能够实现本发明的目的为要求进行布置， 本领域技术人员能够 实现这种布置， 且布置方式并不限于图中所示的具体方式。
本发明中的所述 "多个" 为至少 2个， 例如 6个， 例如 8个、 9 个或更多个。 值得指出的是， 虽然附图以及以下实施例中以 8 个或 9个蒸煮器为例进行举例说明 , 但这仅仅是为了实施例表述 方便和便于理解本发明起见， 并不意味着一定要 8个或 9个蒸煮 器才能实现或连续实现本发明的方法。 如上文所述， 本发明中所 述多个为至少 2个。 本领域技术人员会根据各个步骤所需要的具 体时间来计算具体采用多少个蒸煮器才能实现本发明的方法的连 续操作。 以下实施例仅用于对本发明的技术方案进行举例说明， 不打 算以任何方式限制本发明的范围。 例如， 虽然以下实施例中以含 水的褐煤作为所述固体物料进行蒸发脱水， 但本领域技术人员会 理解， 本发明的方法不仅仅限于对含水的褐煤进行蒸发脱水， 而 是适用于任何含水的固体物料。 又例如， 实施例中列举的具体数 字仅仅是为了提供实验细节的目的， 并不意图对权利要求有任何 限制。 再例如， 虽然在实施例中列出的是本发明的优选方案， 但 并不意味着本发明的保护范围就仅限于该优选方案。 本专利的保 护范围仅由权利要求确定。
实施例 1
各蒸煮器的步骤按照图 1所示， 提供 8个蒸煮器， 编号分别 为 1-8，含水的褐煤依次经过称量系统、 卸料器和皮带输送机， 从 每个蒸煮器顶部的下料斗、 三通球阀和上锁阀分别进入这 8个蒸 煮器， 每个蒸煮器均按照时间先后的顺序在反复执行本文所述的 步骤 i-vi i i , 且在任意的某一时刻， 各蒸煮器执行的操作如下： 蒸煮器 1进行步骤 i , 蒸煮器 2进行步骤 i i , …依次类推…， 蒸 煮器 8进行步骤 vi i i , 没有进行抽真空处理。 其中， 将蒸煮器 5 排出的饱和蒸汽用作蒸煮器 4的饱和蒸汽， 将蒸煮器 6排出的第 三蒸汽用作蒸煮器 3 中的第二蒸汽直至两个蒸煮器之间达到均 压， 将蒸煮器 7排出的第四蒸汽用作蒸煮器 2中的第一蒸汽直至 两个蒸煮器之间达到均压。 其中步骤 vi进行 30分钟， 通入的饱 和蒸汽（含煤中挥发分等不凝气体）压力为 4. OMPa (表压， 本文 中所有的压力均为表压） , 温度为 230 ~ 252*€, 对应的饱和蒸汽 ( 100%水蒸汽）压力为 2. 7 - 4. OMPa; 步驟 v进行 15分钟， 通入 的过热蒸汽温度为 400 , 压力为 4MPa。 提质后的褐煤从各蒸煮 器的固体物料出口排出并经下锁阀、 下料斗、 布料器达到皮带输 送机， 然后被送往后续工序。 褐煤原煤和提质后的煤的性质如下 表 1所示： 表 1
Figure imgf000014_0001
其中， 化验分析执行依据： 煤中全水份测定依据：
GB/T211-2007; 煤的分析水份、 灰分、 挥发分测定依据： 煤的工 业分析方法 GB/T212- 2008;煤的发热量测定依据： GB/T213- 2008。 其中干燥基是指计算各物质的百分比含量时以干燥至完全脱水后 的煤的质量作为分母， 干燥无灰基是指计算各物质的百分比含量 时以干燥脱水且除去灰份后的煤的质量作为分母， 收到基是指以 收到状态的煤为基准。从步骤 vi i i排出的煤的温度为 100- 110 。
实施例 2
各蒸煮器的布置按照图 1所示， 但提供 9个蒸煮器， 编号分 别为 1-9，含水的褐煤分别进入这 9个蒸煮器，每个蒸煮器均按照 时间先后的顺序在反复执行本文所述的步骤 i-ix，且在任意的某 一时刻， 各蒸煮器执行的操作如下： 蒸煮器 1进行步骤 i， 蒸煮 器 2进行步骤 i i， …依次类推…， 蒸煮器 8进行步骤 vi i i , 蒸煮 器 9进行步骤 iv。 其中， 将蒸煮器 5排出的饱和蒸汽用作蒸煮器 4的饱和蒸汽， 将蒸煮器 6排出的第三蒸汽用作蒸煮器 3中的第 二蒸汽直至两个蒸煮器之间达到均压， 将蒸煮器 7排出的第四蒸 汽用作蒸煮器 2中的第一蒸汽直至两个蒸煮器之间达到均压。 其 中步骤 vi进行 20分钟， 通入的饱和蒸汽（含煤中挥发分等不凝 气体）压力为 4. OMPa,温度为 230 ~ 252 Χ ，对应的饱和蒸汽（100% 水蒸汽）压力为 2. 7 - 4. OMPa, 步骤 v进行 20分钟， 通入的过热 蒸汽的温度为 400*€, 压力为 4MPa; 步骤 ix 中相对真空度为 - 0. 08MPa, 抽真空处理 30分钟。 原煤和提质后的煤的性质如下表 2所示， 从步骤 vi i i排出的煤的温度为 70-80X。
表 2
Figure imgf000015_0001
实施例 3
各蒸煮器的布置按照图 1所示， 但提供 9个蒸煮器， 编号分 别为 1-9，含水的褐煤分别进入这 9个蒸煮器，每个蒸煮器均按照 时间先后的顺序在反复执行本文所述的步骤 i-ix，且在任意的某 一时刻， 各蒸煮器执行的操作如下： 蒸煮器 1进行步骤 i， 蒸煮 器 2进行步骤 i i， …依次类推…， 蒸煮器 8进行步骤 vi i i， 蒸煮 器 9进行步骤 iv。 其中， 将蒸煮器 5排出的饱和蒸汽用作蒸煮器 4的饱和蒸汽， 将蒸煮器 6排出的第三蒸汽用作蒸煮器 3中的第 二蒸汽直至两个蒸煮器之间达到均压， 将蒸煮器 7排出的第四蒸 汽用作蒸煮器 2中的第一蒸汽直至两个蒸煮器之间达到均压。 其 中步骤 vi进行 10分钟， 通入的饱和蒸汽（含煤中挥发分等不凝 气体）压力为 4. OMPa，温度为 230 ~ 252 Π，对应的饱和蒸汽（100% 水蒸汽）压力为 2. 7 - 4. OMPa, 步骤 v进行 10分钟， 通入的过热 蒸汽的温度为 400*€, 压力为 4MPa; 步骤 ix 中相对真空度为 - 0. 08MPa, 抽真空处理 30分钟。 原煤和提质后的煤的性质如下表 3所示， 从步骤 vi i i排出的煤的温度为 65-75 X。
表 3
Figure imgf000016_0001
实施例 4
各蒸煮器的布置按照图 1所示， 但提供 9个蒸煮器， 编号分 别为 1-9，含水的褐煤分别进入这 9个蒸煮器，每个蒸煮器均按照 时间先后的顺序在反复执行本文所述的步骤 i-ix，且在任意的某 一时刻， 各蒸煮器执行的操作如下： 蒸煮器 1进行步骤 i， 蒸煮 器 2进行步骤 i i， …依次类推…， 蒸煮器 8进行步骤 vi i i， 蒸煮 器 9进行步骤 iv。 其中， 将蒸煮器 5排出的饱和蒸汽用作蒸煮器 4的饱和蒸汽， 将蒸煮器 6排出的第三蒸汽用作蒸煮器 3中的第 二蒸汽直至两个蒸煮器之间达到均压， 将蒸煮器 7排出的第四蒸 汽用作蒸煮器 2中的第一蒸汽直至两个蒸煮器之间达到均压。 其 中步骤 vi进行 20分钟， 通入的饱和蒸汽（含煤中挥发分等不凝 气体）压力为 3. OMPa，温度为 210 ~ 235 Π，对应的饱和蒸汽（100% 水蒸汽）压力为 1. 8-3. OMPa; 步骤 v进行 20分钟， 通入的过热 蒸汽的温度为 400"€， 压力为 3MPa; 步骤 ix 中相对真空度为 - 0. 08MPa, 抽真空处理 30分钟。 原煤和提盾后的煤的性质如下表 4所示， 从步骤 vi i i排出的煤的温度为 70-80X 。
表 4
Figure imgf000017_0001
本发明的优点如下：
逐级利用了过热蒸汽的焓值对固体物料进行加热并蒸发脱 水， 热效率高。 在本发明中， 热能的利用有五效。 第一效， 利用 过热蒸汽变化到饱和蒸汽所幹放的热对固体物料进行加热； 第二 效， 利用饱和蒸汽对固体物料进行加热； 第三效， 利用第一次减 压所产生的第三蒸汽对固体物料进行加热； 第四效， 利用第二次 减压所产生的第四蒸汽对固体物料进行加热； 第五效， 利用冷凝 水作为热水对固体物料进行加热。 这样做使得过热蒸汽所含的热 能按照热级别从高到低的顺序得到逐级充分利用。 此外， 本发明 的抽真空使残余水份蒸发的过程还额外地相当于第六效的蒸发作 用， 这进一步降低了固体物料中的水份含量， 且降低了最终出料 的温度。 在出料为提质后的褐煤的情况下， 降低最终出料的温度 有利于防止提盾后的褐煤的自燃。 再一个优点是， 通过设置多个 蒸煮器并合理布置它们之间的管路连接关系， 可以使发明的多效 蒸发脱水方法连续进行， 这有利于工业化应用。

Claims

权利要求
1. 一种对固体物料进行多效蒸发脱水的方法， 包括：
提供多个蒸煮器， 所述多个蒸煮器就所述固体物料的流向来 说为并联连接 , 其中每个蒸煮器反复执行按时间先后顺序排列的 以下步骤：
i、装入所述固体物料和热水，用所述热水对固体物料进行第 一次加热；
i i、 通入第一蒸汽对固体物料进行第二次加热， 并排出此步 骤中所产生的冷凝水；
i i i、通入第二蒸汽以对固体物料进行第三次加热， 并排出此 步骤中所产生的冷凝水；
iv、 通入饱和蒸汽以对固体物料进行第四次加热， 使固体物 料达到预定加热温度， 并排出此步骤中所产生的冷凝水；
v、 通入过热蒸汽对达到预定加热温度的固体物料进行蒸煮， 使固体物料中所含的水份蒸发，同时所述过热蒸汽变为饱和蒸汽， 蒸煮过程中排出该饱和蒸汽；
vi、 对蒸煮器进行第一次减压， 并排出第三蒸汽；
vi i、 对蒸煮器进行第二次减压， 并排出第四蒸汽；
vi i i、 使蒸煮器内的压力恢复至常压， 排出固体物料。
2. 权利要求 1的方法， 其中至少一部分蒸煮器在其步骤 vi i 和步骤 vi i i之间还包括步骤 ix: 对蒸煮器进行抽真空处理， 以 使固体物料中残留的水份继续蒸发， 进一步降低固体物料中的水 份含量。
3. 权利要求 1或 2的方法， 其中对于一部分蒸煮器来说， 将 来自其它处于步骤 i i和 /或 i i i和 /或 iv的蒸煮器所排出的冷凝 水用作所述热水和 /或单独由热水器来提供所述热水以使该蒸煮 器进行步骤 i ; 和 /或， 将来自其它蒸煮器的所述第四蒸汽用作所 述第一蒸汽来使该蒸煮器进行步骤 Π ; 和 /或， 将来自其它蒸煮 器的所述第三蒸汽用作所述第二蒸汽来使该蒸煮器进行步驟 i i i ; 和 /或， 将其它蒸煮器的步骤 V中排出的饱和蒸汽用作该蒸 煮器的步骤 iv中的饱和蒸汽。
4. 权利要求 1或 2的方法， 其中每个蒸煮器上包含固体物料 入口、 固体物料出口、 蒸汽入口、 蒸汽出口、 热水入口和冷凝水 出口。
5. 权利要求 4的方法， 其中所述固体物料入口、 蒸汽出口或 冷凝水出口兼作抽真空口。
6. 权利要求 1的方法： 其中所述固体物料是褐煤， 该褐煤中 含有水份。
7. 权利要求 6的方法： 其中所述褐煤是经过温度大于 30 的 水洗涤浸出后的褐煤。
8. 权利要求 1的方法： 其中所述多个为至少 2个，优选至少 4 个， 更优选至少 6个。
9. 权利要求 4的方法： 其中所述蒸汽出口与所述冷凝水出口 是同一个口。
PCT/CN2011/078819 2011-01-20 2011-08-24 固体物料蒸发脱水方法 WO2012097593A1 (zh)

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