CN102174336B - Hearth temperature control device and control method for multi-nozzle opposed coal water slurry gasification furnace - Google Patents

Abstract

The invention discloses a hearth temperature advanced control method for a multi-nozzle opposed coal water slurry gasification furnace. The method comprises the following steps of: controlling oxygen-coal proportion of the gasification furnace; controlling temperature of a hearth of the gasification furnace and performing balancing control of nozzles; and controlling temperature of the hearth. Byadopting the gasification furnace hearth temperature control scheme, the problems of large oxygen-coal proportion fluctuation of a basic control loop, flow unbalance of four paths of nozzles and deflective flame spouting can be solved; the temperature of the hearth can be stabilized at a set value, the oxygen-coal proportion of each path of nozzle is coordinated and deflective spouting is avoidedunder the conditions of frequent changing of coals and flow fluctuation of the coal water slurry; therefore, running period of the gasification furnace is obviously prolonged and economic benefit of the coal gasification device is increased.

Description

Multi-nozzle opposed type coal slurry gasifier fire box temperature control device and control method

Technical field

The present invention relates to the fire box temperature control method, relate to multi-nozzle opposed type coal slurry gasifier fire box temperature control device and method.

Background technology

Rich coal resources in China, the hydrocarbon resources scarcity, the Energy resources structures shape that this is special coal will be the main energy sources of China for a long time.Yet coal in China utilization ratio overall efficiency is low, seriously polluted at present.Gasification is coal resources cleaning, the efficient important channel that utilizes, and is the important technology basis of development energy industry and chemical industry, and Coal Gasification Technology has the leading position in the coal-based energy of modern times and chemical system.Coal Gasification Technology can be divided into coal water slurry gasification technology and bed pulverized coal gasification technology by the charging form.The coal water slurry gasification technology because of its plant investment economize, reliable and go out the synthetic air water of gasification installation/dry gas than high, under the situation that coal allows, be widely used in systems such as chemical industry is synthetic.

The coal water slurry gasification flow process of various processes is basic identical, comprising: coal water slurry preparation section, gasification and coal gas rough purification operation, slag inclusion water treatment operation, core is gasification technology.The multi-nozzle opposed type vapourizing furnace (device as shown in the patent No. 200520047515.3) that the present invention is directed to designs such as East China University of Science is controlled.Multi-nozzle opposed type coal water slurry gasification technology with respect to the GE of external introduction and Destec coal water slurry gasification technology, dry coal powder gasification technology in facility investment, working cost, efficiency of carbon conversion, effectively the pneumatolytic aspect that grades has very big advantage.

Multi-nozzle opposed type vapourizing furnace fast sprays into vapourizing furnace with coal water slurry and oxygen by four opposed nozzles based on the percussion flow principle, fully mixes by bump.In vapourizing furnace, oxygen and spray water xi coal slurry are subjected to the hyperthermia radiation effect of refractory liner in stove, experiencing physics, the chemical process of a series of complexity such as gasification of the cracking burning of preheating, moisture evaporation, coal carbonization, volatile matter and carbon rapidly, generating at last with carbon monoxide, hydrogen, carbonic acid gas and water vapour and be the wet gas of main component and melt slag.(reducing atmosphere of 3.0～6.5MPa) operational conditions and partial oxidation makes a series of chemical transformation of carrying out in the stove and combustion processes and other gasifying process that basic difference be arranged for the high temperature of air-flow bed coal-gasification (1300～1600 ℃), high pressure.

The fire box temperature of vapourizing furnace is the key factor of the whole coal water slurry gasification process of influence.Too high as temperature in the vapourizing furnace, at first can cause the interior moisture of reaction gas too high, and influence operation and the operation of follow-up workshop section.In addition, the too high life cycle that can influence vapourizing furnace of furnace temperature causes refractory brick etc. to damage.Experience shows, when the service temperature of vapourizing furnace is basic point with 1400 ℃, every variation then changes 10% for 10 ℃ the work-ing life of refractory brick, operating temperature raises 50 ℃ and continues 3～5 days, the arch furnace brick life-span will obviously reduce in addition cause fracture, come off, brickwork joint cracking etc., can cause total system to be stopped when serious.Otherwise, cross when low when temperature in the stove, can cause that CO content increases in the reaction gas, also can influence the operation of follow-up workshop section and the interior water balance of total system.Therefore, the gasifier temperature that control suits is for the work-ing life that prolongs refractory brick, and it is significant to reduce running cost.

Although the importance of vapourizing furnace fire box temperature is very obvious, the on-the-spot automatic control control that still lacks fire box temperature.Operation and control strategy that multi-nozzle opposed type vapourizing furnace adopts at present are: separately coal water slurry and the oxygen flow of each nozzle are controlled; By the set(ting)value of regulating each nozzle oxygen flow fire box temperature is controlled.This control strategy is all implemented at the scene distributed control system (DCS, the Distributed Control Systems) platform, finishes basic control function and production process is monitored.These basic Controlling System have ensured the safe operation of vapourizing furnace, but the temperature control of vapourizing furnace is carried out automatically, generally can not adapt to the frequent variations of coal.The main problem that exists has three.At first, it is moving that basic control scheme can not be carried out the ratio contigency of single-nozzle coal water slurry flow and oxygen flow.When the flow of coal water slurry changed, oxygen flow need carry out corresponding to keep suitable oxygen coal ratio through artificial interference.The second, temperature and oxygen coal ratio are not associated, form control loop, need manually interfere, change fire box temperature by manual regulation oxygen spray amount.The 3rd, because each nozzle is controlled separately, can not guarantee the balance of furnace flame.For the stable long-time running of vapourizing furnace, the roughly balance of injection water coal slurry and amount of oxygen in four nozzles of needs assurance.Otherwise, if injection flow is too high in the single-nozzle, will inevitably cause furnace flame to depart from the center, cause local temperature too high.Not only can influence gasification efficiency, can puncture refractory brick when serious, and burn out nozzle.Therefore, above-mentioned three problems have caused in coal and have changed, during the coal slurry fluctuations in discharge, the operator need carry out long manual regulation to the oxygen spray amount of four groups of nozzles, and stable with the production that reaches again, operation easier is big, time is long, has influenced the efficient of whole gasification.

Therefore, in order to give full play to the potentiality of DCS and operating equipment in the gasification installation, effectively utilize raw material and the energy, increase the economic benefit of device, in conjunction with the technological operation characteristics of gasification production process, the state-of-the-art technology in integrated application chemical engineering and the automatic control science is implemented fire box temperature control and the balanced control of nozzle to vapourizing furnace, make the every processing parameter of vapourizing furnace be stabilized in optimum working order, have extremely important practical value.

Summary of the invention

In order to overcome above mentioned the deficiencies in the prior art part, the invention provides a kind of control method of multi-nozzle opposed type vapourizing furnace, this scheme thes contents are as follows:

Vapourizing furnace oxygen coal ratio control

According to the vapourizing furnace operational requirement, at first single-nozzle spray the coal water slurry enter in the vapourizing furnace and oxygen proportion should all-the-time stable, burn preferably and gasification result thereby reach.The fluctuation of oxygen coal ratio at first can cause flame to depart from the center, secondly can cause the fluctuation of fire box temperature, and then influence the composition of synthetic gas.Therefore, the control method among the present invention at first requirement can in the operating process of vapourizing furnace, stablize the ratio of control oxygen and dry coal emitted dose.Be the oxygen coal ratio control strategy at the single-nozzle exploitation shown in Fig. 1, the control module of solid line (coal slurry flow control and oxygen flow control) and information stream (set(ting)value of two controllers and observed value) are existing basic control loop; Module and the information stream of with dashed lines sign add content for the present invention.When DCS realized, traditional pid control algorithm was all adopted in the flow control on basis.In Fig. 1, the dry coal computing module adopts coal slurry flow, coal-water fluid concentration, and observed values such as dry coal density are input, and indirect calculation enters carbon flow in the vapourizing furnace by this nozzle.The set(ting)value that the dry coal flow that oxygen coal ratio control module basis calculates and given oxygen coal recently calculate the oxygen flow controller:

$O_{\mathrm{sp}}^i={\mathrm{Ratio}}_{o/c}^i\·{\mathrm{Flowrate}}_c^i---\left(1\right)$

Wherein

Being the proportioning controller output of i nozzle, also is the set(ting)value of the oxygen flow controller of i nozzle,

Be the dry coal flow of i nozzle, following calculating

${\mathrm{Flowrate}}_c^i={\mathrm{\ρ}}_{\mathrm{coal}}\·{\mathrm{Flowrate}}_{\mathrm{slurry}}^i\·{\mathrm{Con}}_{\mathrm{slurry}}---\left(2\right)$

ρ _CoalBe dry coal density,

Be the coal water slurry flow of i nozzle, Con _SlurryBe water coal slurry concentration.

The balanced control of the control of vapourizing furnace fire box temperature and nozzle

At first, fire box temperature control of the present invention requires recently to control fire box temperature by regulating the oxygen coal, and the emitted dose that increases oxygen when temperature is on the low side improves temperature, otherwise then reduces the emitted dose of oxygen.Yet, if the direct tandem of ratio control system of fire box temperature and each nozzle is got up, control, cause furnace flame to spray phenomenon partially easily.At first, the coal slurry under meter of each nozzle exists different deviations with oxygen flow meter.If, will inevitably require the ratio control system of different spray nozzles to control oxygen flow according to same ratio value and reach same oxygen flow set(ting)value (the coal water slurry flow of supposing each nozzle is identical) directly as the set(ting)value of proportioning controller with the output of temperature regulator.Yet because the under meter deviation, reality sprays into coal water slurry and the oxygen flow and inequality of burner hearth from each nozzle, so causes inclined to one side spray.Cause second reason of inclined to one side spray to be exactly, the oxygen coal of regulating single boiler tube than the time, can not consider the injection flow of other nozzles, the flow between therefore can not each nozzle of balance causes inclined to one side spray.In a word, when design control scheme, requirement can be got up temperature control and ratio control tandem, and recently controls temperature by the oxygen coal of relative each nozzle of adjusting, rather than the absolute flow that makes each nozzle is consistent.

In order to solve the flow equilibrium problem of temperature control and each nozzle, the present invention has proposed control scheme as shown in Figure 2 on the basis of ratio control.Among Fig. 2, shown solid line module is basic control module and ratio control module, shown in dotted line module the temperature control and the balanced control module of nozzle that propose for the present invention.The fire box temperature controller that the present invention adds adopts traditional pid control module to realize at DCS.The fire box temperature controller is output as with the oxygen coal than corresponding relative value, is generally the real number between the 0-100.The fire box temperature controller changes the output of balance module by regulating the output of this relative value, and then influences the set(ting)value of oxygen coal ratio control module, thereby reaches the purpose to fire box temperature control.And in order to guarantee the flow equilibrium between the nozzle, the oxygen coal of the nozzle balance module of invention by adjusting each nozzle coordinated flow equilibrium between each nozzle than the set(ting)value of control module.Specific algorithm is as follows:

${\mathrm{Ratio}}_{o/c}^i\left(k\right)={\mathrm{Ratio}}_{o/c}^i(k-1)+({\mathrm{OP}}_T\left(k\right)-{\mathrm{OP}}_T(k-1))\·a_i(k-1)---\left(3\right)$

$a_i(k-1)=\frac{4\·{\mathrm{Ratio}}_{o/c}^i(k-1)}{\underset{j=1}{\overset{4}{\mathrm{\Σ}}}{\mathrm{Ratio}}_{o/c}^j(k-1)}---\left(4\right)$

Wherein, k is moment point, OP _T(k) be the k output of temperature regulator constantly.a _i(k-1) adopt constantly for k at i nozzle equalizing coefficient, compare with the ratio of the averaged oxygen coal ratio of four nozzles by the oxygen coal to k-1 i nozzle constantly and to try to achieve, as shown in Equation (4).As seen, i the oxygen coal of current time k be than controller set(ting)value in the formula (3), i.e. the output of i nozzle balance controller, by superposition on the basis of itself k-1 value constantly the relative increment of temperature regulator output.Wherein the output increment of temperature regulator determines the influence degree of each the nozzle oxygen coal ratio equalizing coefficient by each nozzle, and also with last one constantly, the oxygen coal of i nozzle compares relevant with the ratio of averaged oxygen coal ratio.By equalizing coefficient, because the inconsistent problem of each nozzle oxygen coal ratio that measuring error such as under meter cause can be resolved.When nozzle is balanced, improve or reduce the set(ting)value of fire box temperature, the output of temperature regulator increases or reduces, and the relative value of variation is superimposed on the proportioning controller of oxygen coal ratio after by the equalizing coefficient weighting, and then the emitted dose of control oxygen increases or reduces.For the bigger nozzle of oxygen coal that causes owing to the flowmeter survey error, pass through equalizing coefficient, the oxygen coal then can be relatively large than increment or the decrement of the set(ting)value of proportioning controller, otherwise, for the smaller nozzle of oxygen coal, when temperature regulator output changed, the amount that increases or reduce was then less relatively.

According to fire box temperature control provided by the invention and the balanced control of nozzle, to set under the situation that improves and reduce in temperature, the oxygen spray amount of each nozzle will balanced increase and minimizing.Except controlling fire box temperature, can also stop the inclined to one side spray phenomenon of flame in the burner hearth.

Fire box temperature control implementation and operation method

Comprehensive oxygen coal is than ratio control and fire box temperature control, and the balanced control of nozzle, and the control method that the present invention proposes can reach following control effect:

1. the oxygen coal is set by temperature regulator and nozzle balance controller than the ratio of proportioning controller and is determined;

2. after the oxygen coal was stablized than the ratio set(ting)value of proportioning controller, ratio control kept oxygen coal ratio to reach set-point by regulating the oxygen spray amount;

3. when the coal water slurry load variations, at first proportioning controller can move, and regulates the oxygen spray amount and compares ratio to keep given oxygen coal.When the change of load has influenced fire box temperature, temperature regulator will change the oxygen coal of each nozzle than the set(ting)value of control together with the balanced control module of nozzle, will control in set-point, guarantee the unanimity of four nozzle flows, avoid the generation of spray partially.

In order to guarantee that control method that the present invention proposes and original DCS go up the fundamental circuit that exists and cooperate and finish fire box temperature control and control with nozzle is balanced, the invention allows for corresponding control method switching method.

1. under the pattern in basic controlling loop, oxygen and coal slurry flow director are in automatic control state.The oxygen coal is than controller, and nozzle balance controller and fire box temperature controller are in manual state.Under this pattern, the oxygen coal is than the set(ting)value of the corresponding oxygen flow controller of the output tracking of controller; The oxygen coal is tried to achieve divided by the observed value of dry coal flow by the observed value of oxygen flow than the set(ting)value of controller; The output of fire box temperature controller is set to 50 (scope of assumed temperature controller output is 0-100); The corresponding oxygen coal of the output tracking of each nozzle balance controller is than the set(ting)value of controller.The operator regulates the equilibrium between fire box temperature and each nozzle flow by manually changing the set(ting)value of each flow director.

2. after vapourizing furnace control is stable, switch to the balanced master mode of temperature and nozzle.At first, the oxygen coal is broken into tandem control than controller and oxygen flow controller.At this moment, the oxygen coal is than the output of the controller set(ting)value as the oxygen flow controller, and the target of control is for keeping stable oxygen coal ratio.The oxygen coal still can be by manually changing than the set(ting)value of controller.The output of nozzle balance controller is still followed the tracks of the oxygen coal than the set(ting)value of controller.Then, the oxygen coal is arranged to the tandem pattern than controller and nozzle balance controller.At this moment, the output valve of nozzle balance controller is calculated according to formula (3) and (4), and as the set(ting)value of nozzle balance controller.At this moment, can control fire box temperature control by the set(ting)value that the fire box temperature controller manually is set.Regulate load by the coal water slurry emitted dose of regulating each nozzle.

3. when temperature control and the balanced control action kou of nozzle are not good, it can be switched to basic control mode, with the safe operation of assurance vapourizing furnace.At first nozzle balance controller and oxygen coal are arranged to initiation of manual pattern and automatic mode respectively than controller.Then nozzle balance controller output this moment oxygen coal is than the set(ting)value of controller.The fire box temperature controller is set to manually, and output is set to 50.Still can manually arrange the oxygen coal than the set(ting)value of controller this moment.Then, the oxygen flow control module is set to automatically, the oxygen coal is than the set(ting)value of the output tracking oxygen flow control module of controller at this moment.The oxygen coal is tried to achieve divided by the dry coal flow by oxygen flow than the set(ting)value of controller.

In the present invention, the ratio control module of proposition, temperature control modules, nozzle balance module and corresponding implementation and operation method are combined into for multi-nozzle opposed type coal slurry gasifier control method.Wherein the ratio control module has guaranteed the oxygen coal than controlling in set(ting)value, and temperature control modules has guaranteed fire box temperature to be controlled in set(ting)value than the set(ting)value of proportioning controller by regulating the oxygen coal.The nozzle balance module can guarantee respectively to organize the nozzle flow equilibrium on the basis of control fire box temperature, avoids flame to depart from the central position of burner hearth.In addition, the implementation and operation method that the present invention proposes can be on the basis that does not change the original base control loop, and the control method that the interpolation of safety proposes instructs for field conduct improves.

Description of drawings

Fig. 1 is that single mouth oxygen coal is than control module synoptic diagram.

Fig. 2 is the multi-nozzle opposed type coal slurry gasifier fire box temperature control device synoptic diagram of how balanced branch road.

Fig. 3 is that the single nozzle A road coal slurry flow director realized of PKS, dry coal flow rate calculation module, oxygen/coal are than the configuration figure of controller and oxygen flow controller.

Fig. 4 is the configuration figure of the how balanced branch road fire box temperature control device of PKS realization.

Embodiment

Explanation by following example helps to understand the present invention, but does not limit content of the present invention.

Adopt the Process Knowledge System of procedural knowledge system (PKS) of Honeywell, designed control loop is carried out configuration.Controlling System at process be the opposed vapourizing furnaces of four nozzles, total A, B, C, D four road nozzle systems.In the present embodiment, intrinsic functional module has following a few class among the PKS of employing:

Each road coal water slurry flow measurement module FI1203A (B, C, D) _ 1; Each road oxygen flow measurement module FI1303A (B, C, D) _ 1; Each road water coal slurry concentration measurement module FI1403A (B, C, D) _ 1; Each road dry coal density measurement module FI1503A (B, C, D) _ 1; The measurement module TI1304 of fire box temperature;

2. control each road coal water slurry flow valve aperture output module FV1203A (B, C, D) _ 1; Control each road oxygen flow valve opening output module FV1303A (B, C, D) _ 1;

3.DATAACQ module to each observed value filter clamper, low signal by and processing such as warning, finally change the engineering unit output valve of expectation into.

4. the numeral of each road dry coal flow rate calculation is taken advantage of module (COALCLCA, COALCLCB, COALCLCC, COALCLCD), and this module is used for getting rid of the disturbance that control causes to oxygen flow of coal-water fluid concentration and the dry coal density of coal water slurry, specifically can be with reference to formula (2)

5. controller module: the controller module that uses in this programme comprises that pid control module and ratio control module and increment add controller.Wherein (D) _ 1, (B, C is D) _ 1 for adopting the PID module to realize for each road oxygen flow controller FIC1303A for B, C for each road coal water slurry flow director FIC1203A.(B, C D) are proportioning controller to each road oxygen/coal proportioning controller RATIOCTLA, and and each road oxygen flow controller formation tandem control.Each road converter nose balance controller FYI_1303A (B, C, D) _ 1 and Ge Lu oxygen/coal form tandem control than controller, adopt increment to add control module and realize, in order to realize formula (3) and (4) designed control strategy.OP in the formula (3) _T(k) and OP _T(k-1) input value of the last current performance period of corresponding converter nose balance controller and the input value of a last performance period, the just output valve of the current performance period of fire box temperature controller TIC1304 correspondence and the output valve of a last performance period; A in the formula (4) _i(k-1) Biao Shi scale factor (k adopt constantly at i nozzle equalizing coefficient), (B, C D) realize by computing module ENHREGCALCA_A.

Be the annexation that example is introduced above each control module with A road boiler tube, with the fire box temperature control method that realizes proposing.At first, the measurement module TI1304 of fire box temperature is by the observed value of AI passage acquisition fire box temperature, and its output is as the input of module DATAACQ.The fire box temperature measurement signal enters fire box temperature controller TIC1304 through the numerical value that is transformed into quantities unit of DATAACQ module as observed value.The another one of controller TIC1304 is input as its set(ting)value.The output of temperature regulator is connected to the input of balance module FYI_1303A, and its another one is input as the output of computing module ENHREGCALCA_A.The output of module ENHREGCALCA_A has provided the equalizing coefficient of A road boiler tube.The output of FYI_1303A has been connected to the set(ting)value input terminus of A road oxygen coal than proportioning controller RATIOCTLA.What the another one input terminus of RATIOCTLA connected is the output of A road dry coal flow rate calculation module COALCLCA.Module COALCLCA is input as measurement module FI1203A_1, FI1403A, FI1503A, observed value through the output of DATAACQ.Wherein the observed value of FI1503A is through the output of DATAACQ, as the observed value input of coal water slurry flow director FIC1203A.The another one of controller module FIC1203A is input as its set(ting)value.The oxygen coal is connected to the set(ting)value input terminus of oxygen flow controller FIC1303A than the output of proportioning controller RATIOCTLA.The observed value input terminus of FIC1303A comes from measurement module FI1303A through the output port of DATAACQ.The output of controller FIC1303A and FIC1203A all directly is applied on corresponding by-pass valve control module FV1303A and the FV1203A.Above-mentioned annexation has been set up the oxygen coal of A road boiler tube than the part of ratio control and fire box temperature.By the similar foundation to the Controlling System of other three boiler tubes, whole fire box temperature Controlling System can be set up.

Below to how the Controlling System of setting up is carried out switching with the basic controlling circuit pattern:

1. under the pattern in basic controlling loop, oxygen and coal water slurry flow director FIC1303A (B, C, D) and FIC1203A (B, C D) are in automatic control state.(D), (B, C D) are in initial manual state with fire box temperature controller TIC1304 to nozzle balance controller FYI_1303A to proportioning controller RATIOCTLA for B, C.Under this pattern, proportioning controller RATIOCTLA (B, C, the corresponding oxygen flow controller of output tracking D) FIC1303A (B, C, set(ting)value D), its set(ting)value is by observed value FI1303A (B, the C of oxygen flow, D) (observed value D) is tried to achieve for B, C divided by dry coal flow COALCLCA; The output of fire box temperature controller TIC1304 is set to 50 (scope of assumed temperature controller output is 0-100); Each nozzle balance controller FYI_1303A (B, C, D) output tracking corresponding proportion controller RATIOCTLA (B, C, set(ting)value D).

2. after vapourizing furnace control is stable, switch to the balanced master mode of temperature and nozzle.At first, (D) (B, C D) break into tandem control with oxygen flow controller FIC1303A for B, C with proportioning controller RATIOCTLA.At this moment, ((set(ting)value D), the target of control are the oxygen coal ratio that keeps stable to proportioning controller RATIOCTLA for B, C as oxygen flow controller FIC1303A in output D) for B, C.(set(ting)value D) still can be by manually changing for B, C for proportioning controller RATIOCTLA.(proportioning controller RATIOCTLA (B, C, set(ting)value D) are still followed the tracks of in output D) to nozzle balance module FYI_1303A for B, C.Then, (D) (B, C D) are arranged to the tandem pattern with nozzle balance module FYI_1303A for B, C than controller RATIOCTLA with the oxygen coal.At this moment, nozzle balance module FYI_1303A (output valve D) is calculated according to formula (3) and (4) for B, C, and as ratio control module RATIOCTLA (B, C, set(ting)value D).At this moment, can control fire box temperature control by the set(ting)value that temperature control modules TIC1304 manually is set.Regulate load (by regulating FIC1203A (B, C, set(ting)value D)) by the coal water slurry emitted dose of regulating each nozzle.

3. when temperature control and the balanced control action kou of nozzle are not good, it can be switched to basic control mode, with the safe operation of assurance vapourizing furnace.At first (D) (B, C D) are arranged to initiation of manual pattern and automatic mode respectively with ratio control module RATIOCTLA for B, C with the balanced control module FYI_1303A of nozzle.Then this moment nozzle balance module FYI_1303A (B, C, D) output tracking ratio control module RATIOCTLA (B, C, set(ting)value D).Temperature control modules TIC1304 is set to manually, and output is set to 50.Ratio control module RATIOCTLA (B, C, set(ting)value D) still can manually be set this moment.Then, (B, C D) are set to automatically, at this moment ratio control module RATIOCTLA (B, C, D) output tracking oxygen flow control module FIC1303A (B, C, set(ting)value D) with oxygen flow control module FIC1303A.Ratio control module RATIOCTLA (tried to achieve divided by the dry coal flow by oxygen flow for B, C by set(ting)value D).

Only being preferable case study on implementation of the present invention in sum, is not to limit practical range of the present invention.Be that all equivalences of doing according to the content of the present patent application claim change and modification, all should be technology category of the present invention.

Claims (7)

1. multi-nozzle opposed type coal slurry gasifier fire box temperature control device comprises a single mouth oxygen coal than control module, and this module comprises:

The coal slurry flow director, this controller is input with coal water slurry flow setting value and observed value, makes flow reach set(ting)value with regulated valve;

The oxygen flow controller, this controller is input with oxygen flow set(ting)value and observed value, makes flow reach set(ting)value with regulated valve;

It is characterized in that, also comprise:

Dry coal flow rate calculation module, this module is input with coal water slurry flow measurements, water coal slurry concentration observed value and dry coal density measurement, carries out following operation: ${\mathrm{Flowrate}}_c^i={\mathrm{\ρ}}_{\mathrm{coal}}\·{\mathrm{Flowrate}}_{\mathrm{slurry}}^i\·{\mathrm{Con}}_{\mathrm{slurry}},$ Wherein Be the dry coal flow measurements of i nozzle, ρ _CoalBe the dry coal density measurement,

Be the coal water slurry flow measurements of i nozzle, Con _SlurryBe the water coal slurry concentration observed value, with gained dry coal flow

Be output;

This module also comprises:

The oxygen coal is than controller, and than set(ting)value and the output of aforementioned dry coal flow rate calculation module, namely the dry coal flow is input to this controller, carries out following operation with the oxygen coal:

Wherein,

Being the proportioning controller output of i nozzle, also is the set(ting)value of the oxygen flow controller of i nozzle,

Be the dry coal flow of i nozzle,

Be the set(ting)value of this oxygen coal than controller.

2. temperature-control device as claimed in claim 1, it is characterized in that, described single mouth oxygen coal connects a nozzle balance controller than control module input terminus and forms the balanced branch road of a single nozzle, and this nozzle balance controller is output as input with the fire box temperature controller, carries out following operation: ${\mathrm{Ratio}}_{o/c}^i\left(k\right)={\mathrm{Ratio}}_{o/c}^i(k-1)+({\mathrm{OP}}_T\left(k\right)-{\mathrm{OP}}_T(k-1))\·a_i(k-1),$ Wherein

K is moment point, OP _T(k) be the output of k moment point fire box temperature controller, a _i(k-1) for the k moment point adopt at i nozzle equalizing coefficient, with gained oxygen coal ratio

Be output, export the oxygen coal to than controlling mould as set(ting)value; Described temperature-control device is made up of many aforementioned branch roads, and these many branch road input terminuss connect a fire box temperature controller, and this temperature regulator is input with fire box temperature set(ting)value and observed value, and gained exports each nozzle balance controller to.

3. the control method with multi-nozzle opposed type coal slurry gasifier fire box temperature control device as claimed in claim 1 is characterized in that, may further comprise the steps:

Step 1, coal water slurry flow measurements, water coal slurry concentration and dry coal density measurement input dry coal flow module, this module operation, output dry coal flux values to oxygen coal compares controller;

Than controller, this controller operation is exported the oxygen flow set(ting)value to the oxygen flow controller than input oxygen coal for step 2, dry coal flow and oxygen coal.

4. control method with multi-nozzle opposed type coal slurry gasifier fire box temperature control device as claimed in claim 2 is characterized in that this equalization temperature control method may further comprise the steps:

Step 0, the fire box temperature controller exports the nozzle balance controller to, this controller operation, output oxygen coal compares controller than set(ting)value to oxygen coal;

Step 1, coal water slurry flow measurements, water coal slurry concentration and dry coal density measurement input dry coal flow module, this module operation, output dry coal flux values to oxygen coal compares controller;

Than controller, this controller operation is exported the oxygen flow set(ting)value to the oxygen flow controller than input oxygen coal for step 2, dry coal flow and oxygen coal;

Step 3 is controlled fire box temperature control by the set(ting)value that the fire box temperature controller manually is set.

5. control method as claimed in claim 4, it is characterized in that, comprise that also described equalization temperature control method is to the switching of fundamental circuit control method, described fundamental circuit control method, be that nozzle balance controller, oxygen coal are manual mode, manual mode, automatic mode than controller, oxygen flow controller, be that the output tracking oxygen coal of nozzle balance controller is than the set(ting)value of controller, the oxygen coal is than the set(ting)value of the output tracking oxygen flow control module of controller, and the oxygen coal is tried to achieve divided by the dry coal flow by oxygen flow than the set(ting)value of controller.

6. control method as claimed in claim 5 is characterized in that, the equalization temperature control method is switched to the fundamental circuit method, and is further comprising the steps of:

Step 4 is arranged to the initiation of manual pattern with nozzle balance controller and oxygen coal than controller, and the fire box temperature controller is set to manually, and exports a preset value;

Step 5 is set to oxygen flow and coal water slurry flow-control module automatically, and namely the oxygen coal is than the set(ting)value of the output tracking oxygen flow control module of controller, and the oxygen coal is tried to achieve divided by the dry coal flow by oxygen flow than the set(ting)value of controller.

7. control method as claimed in claim 5 is characterized in that, the fundamental circuit method is switched to the equalization temperature control method, may further comprise the steps before described step 0:

Step-2, the oxygen coal is than the output of the controller set(ting)value as the oxygen flow controller, the oxygen coal keeps manual mode than controller, be that the oxygen coal changes by manual than controller carbon ratio set(ting)value, the nozzle balance controller keeps automatic mode, and namely nozzle balance controller output tracking oxygen coal is than the set(ting)value of controller;

Step-1 is arranged to the tandem pattern with the oxygen coal than controller and nozzle balance controller.

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