MXPA01002956A - System and method for integrated gasification control - Google Patents
System and method for integrated gasification controlInfo
- Publication number
- MXPA01002956A MXPA01002956A MXPA/A/2001/002956A MXPA01002956A MXPA01002956A MX PA01002956 A MXPA01002956 A MX PA01002956A MX PA01002956 A MXPA01002956 A MX PA01002956A MX PA01002956 A MXPA01002956 A MX PA01002956A
- Authority
- MX
- Mexico
- Prior art keywords
- oxygen
- flow
- syngas
- signal
- carbon
- Prior art date
Links
- 238000002309 gasification Methods 0.000 title claims abstract description 99
- MYMOFIZGZYHOMD-UHFFFAOYSA-N oxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 451
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 451
- 239000001301 oxygen Substances 0.000 claims abstract description 451
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 306
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 230
- 238000011068 load Methods 0.000 claims abstract description 28
- 238000000926 separation method Methods 0.000 claims abstract description 8
- 238000004519 manufacturing process Methods 0.000 claims description 97
- 239000003245 coal Substances 0.000 claims description 76
- 230000004907 flux Effects 0.000 claims description 65
- 238000006243 chemical reaction Methods 0.000 claims description 41
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 36
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 35
- 239000004215 Carbon black (E152) Substances 0.000 claims description 28
- 150000002430 hydrocarbons Chemical class 0.000 claims description 28
- 238000004364 calculation method Methods 0.000 claims description 24
- 229910052739 hydrogen Inorganic materials 0.000 claims description 24
- 239000001257 hydrogen Substances 0.000 claims description 24
- 150000002431 hydrogen Chemical class 0.000 claims description 24
- 239000010866 blackwater Substances 0.000 claims description 22
- 241001442055 Vipera berus Species 0.000 claims description 19
- 238000009423 ventilation Methods 0.000 claims description 18
- 238000004140 cleaning Methods 0.000 claims description 17
- 239000007788 liquid Substances 0.000 claims description 7
- 238000002485 combustion reaction Methods 0.000 claims description 6
- -1 carbon oxygen Chemical compound 0.000 claims description 5
- 239000000571 coke Substances 0.000 claims description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 4
- 239000001569 carbon dioxide Substances 0.000 claims description 4
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- 235000015927 pasta Nutrition 0.000 claims description 2
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- QAOWNCQODCNURD-UHFFFAOYSA-M hydrogensulfate Chemical compound OS([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-M 0.000 description 6
- 230000003247 decreasing Effects 0.000 description 5
- 206010024855 Loss of consciousness Diseases 0.000 description 4
- 239000003607 modifier Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 238000004590 computer program Methods 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 230000003287 optical Effects 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N oxygen atom Chemical group [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
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- 238000003786 synthesis reaction Methods 0.000 description 2
- 230000002194 synthesizing Effects 0.000 description 2
- BIGPRXCJEDHCLP-UHFFFAOYSA-N Ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 1
- 241000272525 Anas platyrhynchos Species 0.000 description 1
- 235000002918 Fraxinus excelsior Nutrition 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 1
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 1
- LRPCLTPZMUIPFK-UHFFFAOYSA-L methane;sulfate Chemical compound C.[O-]S([O-])(=O)=O LRPCLTPZMUIPFK-UHFFFAOYSA-L 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- HCWPIIXVSYCSAN-UHFFFAOYSA-N radium Chemical compound [Ra] HCWPIIXVSYCSAN-UHFFFAOYSA-N 0.000 description 1
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- 238000011144 upstream manufacturing Methods 0.000 description 1
Abstract
An integrated control system (ICS) for a gasification plant controls the operation of a gasifier and other critical components of the gasification plant. The ICS improves the performance of a gasification plant by controlling the operation of a gasifier and other critical components by an integrated controller, rather than by several independent controllers. The ICS is a sub-system of a larger distributed control system that controls the operation of the gasification plant. The ICS controls the following:(i) oxygen to carbon (O/C) ratio in a gasifier;(ii) syngas demand or the desired output of a gasifier;(iii) load constraints;(iv) moderator flow into a gasifier;(v) air separation unit (ASU);(vi) oxygen header vent valves;and (vii) syngas header pressure.
Description
SYSTEM AND METHOD FOR CONTROL OF INTEGRATED GASIFICATION
BACKGROUND OF THE INVENTION I Field of the Invention The present invention relates to gasification, and more particularly to a system and method for integrated gasification control.
II Related Art Gasification is among the cleanest and most efficient technologies for the production of energy, chemicals and industrial gases from hydrocarbon supplies, such as coal, heavy oil and petroleum coke. Put simply, gasification converts hydrocarbon supplies into clean synthesis gas, or syngas, composed mainly of hydrogen (H2) and carbon monoxide (CO). In a gasification plant, the supply is mixed with oxygen (O2) and injected into a gasifier. Within the gasifier, the supply and O2 are subjected to high temperatures and high pressures. As a result, supply and O2 are broken down into syngas. In addition to H2 and CO, the syngas contains other gases in small amounts, such as ammonia, methane and hydrogen sulfate (H2S). As much as 99% or more of H2S present in the syngas can be recovered and converted into a form of elemental sulfur and can be used in the fertilizer or chemical industry. The ashes and any metal are removed in a slag-like state, and the syngas are cleaned of particles. The clean syngas is then used to generate electricity and produce industrial chemicals and gases. Gasification allows refineries to generate energy and produce additional products. So gasification offers greater efficiency, energy savings and a
cleaner environment. For example, a gasification plant at a refinery in El Dorado, Kansas converts petroleum coke and refinery waste into electricity and steam, making the refinery fully self sufficient for its energy needs and significantly reducing waste costs. and coke management. For these reasons, gasification has become much more popular among refineries worldwide. Currently, there are several hundred gasification plants in operation around the world. The operation of the gasification plant requires several control systems to control the gasifier and other equipment connected to it. At present, gasification plants use independent controllers, for example, proportional integral controllers (PID), to independently control several processes in the gasification plant. Independent controllers operate separately and do not interact with each other. As a consequence, the desired setpoint of each controller must be entered separately. Unfortunately, independent controllers often provide a poor response, which results in increased wear of the gasifier and other associated equipment. Specifically, the poor response of the controller can damage a refractory vessel of the gasifier (a layer of bricks in the gasifier designed to keep the heat inside the gasifier) and the temperature sensors of the thermocouple that measure the temperatures in the gasifier. The poor response of the controller also causes the gasifier to suffer from blackouts and the syngas "just in case" does not meet the required specifications. For these reasons, the need for an integrated control system that controls several critical components of the gasification plant has been recognized. An integrated control system must improve the reliability of the gasification plant to
reduce gasifier blackouts and maximize operating time. Also, an integrated control system must reduce the wear of the gasifier and other associated components.
SUMMARY OF THE INVENTION The present invention is directed to an integrated control system (ICS) for a gasification plant. The ICS controls the operation of a gasifier and other critical components of a gasification plant. The present invention increases the performance of a gasification plant by controlling the operation of a gasifier and other critical components by means of an integrated controller, instead of several independent controllers. The ICS is a subsystem of a larger distributed control system that controls the operation of the gasification plant. Briefly described, the ICS controls the following:
(i) carbon oxygen (O / C) radius in a gasifier; (I) demand for syngas or the desired production of a gasifier; (Ii) cargo restrictions; (iv) moderator flow in a gasifier; (v) air separation unit (ASU); (vi) oxygen head fan valves; (vii) syngas head pressure.
The ICS provides safer operation and increased life of the gasifier equipment and other critical components by controlling the O / C radius. The optimal conversion of
Hydrocarbon occurs when the O / C radius is controlled. According to the present invention, the O / C radius is controlled by controlling the average averages of oxygen and carbon in the gasifier. The demand for syngas is determined from a demand setpoint value and a demand signal. The demand signal is produced by the macro conversion of an average carbon flux. The load restrictions are determined from a feed pump setpoint value, a PV / SP supply pump, where PV / SP is the actual power for the desired power radius, a position of the oxygen valve, and an oxygen ventilation / recycling value. The flow moderators (steam) in the gasifier are controlled by adjusting one or more oxygen line steam valves and carbon line steam valves. If recycled black water is also used as a moderator, the flow of black water is controlled by adjusting the speed of a black water pump. The oxygen discharge of the ASU is controlled by adjusting an oxygen compressor inlet valve. The amount of oxygen ventilated through the oxygen head ventilation valves is controlled by adjusting the position of the ventilation valves. The pressure of the syngas head is controlled by three methods: a high pressure control; a low pressure control; and a "low low" pressure control. The present invention provides a method for controlling a radium of oxygen to carbon (O / C) in a gasification plant. The method comprises the steps of: determining a syngas demand based on load restrictions, the demand of syngas represents a desired production of a gasifier: determination of oxygen and carbon setpoint values based on a setpoint value of oxygen radius to carbon (O / C) and the demand for syngas, and the adjustment of oxygen valves and
coal in the gasification plant based on oxygen and carbon setpoint values, respectively. The present invention provides a method for determining an oxygen setpoint value in a gasification plant. The method comprises the steps of: multiplying an oxygen setpoint value by an average carbon flux to generate a high oxygen setpoint limit; determination of a restricted oxygen demand by an average carbon flow in a low selector from a demand for syngas and the high limit of oxygen setpoint; multiplication of the high limit of oxygen setpoint by a predetermined factor to generate a low limit of oxygen setpoint, and determination of a setpoint value of oxygen restricted in a high selector from the low limit of oxygen setpoint and the oxygen demand restricted by the average carbon flow. The present invention provides a method for determining a setpoint value of coal in a gasification plant. The method comprises the steps of: determining a low limit of carbon setpoint in a high selector from an average oxygen flow and a demand for syngas; multiplication of the average oxygen flow by a predetermined factor to generate a high limit of carbon setpoint; determination of a restricted carbon setpoint value in a low selector from the high carbon setpoint limit and the low carbon setpoint limit; and division of the carbon setpoint restricted by the O / C radio setpoint to generate the carbon control setpoint value. The present invention provides a method for controlling an oxygen flow in a gasification plant. The method comprises the steps of: calculating the oxygen flow compensated from an average oxygen flow and oxygen temperature in a flow compensator; Oxygen flow conversion compensated to a
molar oxygen flow in a molar converter; multiplication of the molar oxygen flow by a value of oxygen purity to generate an oxygen flow signal; reception of the oxygen flow signal and an oxygen control setpoint value in a PID controller and generation of a PID controller production signal: speed that limits the production signal of the PDI controller to a speed limitation; and adjusting an oxygen valve using the limited PID controller speed production signal.
The present invention provides a method for controlling a coal flow in a gasification plant. The method comprises the steps of: calculating the carbon flux compensated from a charge pump speed; selection of an average carbon flux from an average inferred coal flow and average carbon flux measured in a signal selector; conversion of the coal flow to a flow of molar coal in a molar converter; generation of a carbon flow signal from an average molar coal flow, a limited speed paste concentration and a limited speed carbon content; generation of a carbon pump speed signal in a PID controller using a carbon flow signal and a carbon control setpoint value; and adjusting the speed of a carbon pump by the carbon pump speed signal. The present invention provides a method for controlling moderators in a gasification plant. The method comprises the steps of: generating a compensated oxygen line vapor flow signal in a first flow compensator from an average oxygen line vapor flow, a vapor temperature and a vapor pressure; generation of a vapor line signal of carbon line compensated in a second compensator from an average steam flow of
coal line, vapor pressure and vapor temperature; addition of the compensated oxygen line steam flow signal and the carbon line vapor flow signal in a first adder to generate a total steam flow signal: determination of a total moderator flow from a signal of total steam flow and a recited black water flow: division of the total moderator flow by the coal flow in a first divider to determine a moderator / carbon radius; determination of a desired oxygen line vapor average from the moderator / carbon radio signal and a moderator / carbon setpoint value in a radio controller; determination of an oxygen line vapor valve signal from a desired oxygen line vapor average and an oxygen line vapor flow signal; adjustment of an oxygen line steam valve by the oxygen line steam valve signal; determination of a coal line steam valve signal from the compensated carbon line steam flow signal and a coal line vapor flow setpoint value; and adjustment of a coal line steam valve by the coal line steam valve signal. The present invention provides a method for controlling an air separation unit (ASU) that provides oxygen to a gasification plant. The method comprises the steps of; comparing oxygen valve positions of a plurality of gasifiers operating simultaneously in a high selector, and producing a value x; calculating F (x) = 0.002x + 0.08, where F (x) > 0.99, and x is the production of a high selector; and calculating F (y) = 0.002y + 0.81, where F (y) > 1.0, y y is the oxygen valve position of a selected gasifier. The present invention provides a method for controlling high pressure of a syngas head in a gasification plant. The method comprises the steps of: receiving a flow average of syngas head, a head temperature of
syngas and a syngas head pressure signal in a flow compensator, and fan-valve expansion biasing of syngas head from the syngas head flow, the syngas head temperature and maximum allowable flow through of a syngas head valve. The present invention provides a program storage device that a machine can read, tangibly characterizing a program of instructions executable by the machine to perform steps of the control method of a carbon dioxide (O / C) in a plant of gasification, the gasification plant converts the supply of oxygen and hydrocarbon into syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the steps of the method include: determining a demand for syngas based on load restrictions, the syngas demand is representative of a desired production of a gasifier; determination of oxygen and carbon setpoint values, and adjustment of oxygen and carbon valves in the gasification plant based on oxygen and carbon setpoint values, respectively. The present invention provides a program storage device that a machine can read, tangibly characterizing a program of instructions executable by the machine to perform steps of the method of determining an oxygen setpoint value in a gasification plant, the plant of Gasification converts the hydrocarbon supply into syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the steps of the method include: multiplication of an oxygen setpoint value by an average carbon flow to generate a high limit of oxygen setpoint; determination of an oxygen demand restricted by an average carbon flow in a low selector from a demand for syngas and the high oxygen setpoint limit; multiplication of the limit
oxygen setpoint high by a predetermined factor to generate a low oxygen setpoint limit, and determination of a restricted oxygen setpoint value in a high selector from the low limit of oxygen setpoint and the oxygen demand restricted by the average carbon flow. The present invention provides a program storage device that a machine can read, characterizing in a tangible way a program of instructions executable by the machine to perform steps of the method of determining a setpoint value of coal in a gasification plant, the plant of gasification converts the supply of oxygen and hydrocarbon into syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the steps of the method include: determination of a low limit of carbon setpoint in a high selector from an average of oxygen flow and a demand for syngas; multiplication of the average oxygen by a predetermined factor to generate a high limit of carbon setpoint; determination of a restricted carbon setpoint value in a low selector from a high carbon setpoint limit and the low carbon setpoint limit; and division of the carbon setpoint restricted by an O / C radio setpoint to generate the carbon control setpoint value. The present invention provides a program storage device that a machine can read, characterizing in a tangible way a program of instructions executable by the machine to perform steps of the method of controlling an oxygen flow in a gasification plant, the gasification plant converts the supply of oxygen and hydrocarbon in syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the steps of the method include: calculation of a flow of oxygen compensated from an average flow of oxygen and oxygen temperature in a flow compensator; Oxygen flow conversion
compensated for a flow of molar oxygen in a molar converter; multiplication of the molar oxygen flow by a value of oxygen purity to generate an oxygen flow signal: reception of the oxygen flow signal and oxygen control setpoint value in a PID controller and generation of an oxygen production signal PID controller; speed that limits the production signal of PID controller to a speed limiter; and adjusting an oxygen valve using a limited speed PID controller production signal. The present invention provides a program storage device that a machine can read, characterizing in a tangible way a program of instructions executable by the machine to perform steps of the method of controlling a coal flow in a gasification plant, the gasification plant converts the supply of oxygen and hydrocarbon in syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the steps of the method include: calculation of a carbon flux average from a charge pump speed; selection of a real carbon flux average from an average inferred coal flux and an average carbon flux measured in a signal selector: conversion of the average carbon flux to an average flux of coal in a molar converter: generation of a carbon flow signal from an average molar coal flow, a limited speed paste concentration and a limited carbon content of speed: generation of a carbon pump speed signal in a PID controller using the carbon flow signal and a carbon control setpoint value; and adjusting the speed of a carbon pump by a carbon pump speed signal. The present invention provides a program storage device that a machine can read, characterizing in a tangible way a program of
instructions executable by the machine to perform steps of the method of control of moderators in a gasification plant, the gasification plant converts the supply of oxygen and hydrocarbon into syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the steps of the method comprise: generating an oxygen line vapor flow signal in a first flow compensator from an average oxygen line vapor flow, a vapor temperature and vapor pressure; generation of a steam flow signal from coal line in a second flow compensator from an average steam line flow of coal, vapor pressure and steam temperature; adding an oxygen line steam flow signal and the carbon line vapor flow signal compensated in a first adder to generate a total steam flow signal; determination of a total moderator flow from a total steam flow signal and a recycled black water flow: division of the total moderator flow by the coal flow in a first divider to determine a moderator / carbon radius; determination of a desired oxygen line vapor average from a moderator / carbon radio signal and a moderator / carbon setpoint value in a radio controller; determination of an oxygen line vapor valve signal from the desired oxygen line vapor average and oxygen line vapor flow signal; adjustment of an oxygen line steam valve by the oxygen line steam valve signal, determination of a carbon line steam valve signal from the compensated carbon line steam flow signal and a steam line setpoint value of coal line; and adjustment of a coal line steam valve by the coal line steam valve signal. The present invention provides a program storage device that a machine can read, characterizing in a tangible way a program of
instructions executable by the machine to perform steps of the control method of an air separation unit (ASU) that provides oxygen to a gasification plant, the gasification plant converts the supply of oxygen and hydrocarbon into syngas composed mainly of hydrogen (H2 ) and carbon monoxide (CO), the steps of the method comprise: comparison of oxygen valve positions of a plurality of gasifiers operating simultaneously in a high selector, and production of an x value; calculating F (x) = 0.002x + 0.08, where F (x) > 0.99, and x is the production of a high selector; and calculating F (y) = 0.002y + 0.81, where F (y) > 1.0, and 'y' as the oxygen valve position of a selected gasifier. The present invention provides a program storage device that a machine can read, tangibly characterizing an instruction program executable by the machine to perform steps of the high pressure control method of a syngas head in a gasification plant, the syngas head transports syngas from a gasifier, the gasification plant converts the supply of oxygen and hydrocarbon into syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the steps of the method include: reception of an average flow of syngas head, a syngas head temperature signal and a syngas head pressure signal in a flow compensator, and calculation of a compensated syngas head flow; and calculation of the partiality of the syngas head widened ventilation valve from the compensated syngas head flow, the syngas head temperature and a maximum allowable flow through a syngas head valve. Further features and advantages of the present invention, as well as the structure and operation of the present invention, are described in detail below with reference to the accompanying drawings.
BRIEF DESCRIPTION OF THE DRAWINGS In the drawings, as the reference numbers usually indicate identical, functionally similar elements, and / or structurally similar elements. Drawings in which an item appears for the first time is indicated by the last digit (s) in the reference number. The present invention will be described with reference to the accompanying drawings, wherein: FIG. 1 illustrates a gasification system according to a characterization of the present invention; FIG. 2 is a block diagram of a distributed control system according to a characterization of the present invention; FIG. 3 is a high-level block diagram of an integrated control system (ICS) according to a characterization of the present invention; FIG. 4 is a flow chart of a method for controlling a carbon oxygen (O / C) radius according to a characterization of the present invention; FIG. 5 is a flowchart of a method for calculating a demand for syngas according to a characterization of the present invention; FIG. 6 is a flow diagram of a method for determining load restrictions according to a characterization of the present invention; FIG. 7 is a flow chart of a method for determining a setpoint value of (O / C) according to a characterization of the present invention; FIG. 8 is a flow chart of a method for calculating an oxygen setpoint value; FIG. 9 is a flow chart of a method for determining a carbon setpoint value;
FIG. 10 is a flowchart of a method for an oxygen flow control; FIG. 11 is a flowchart of a method for a carbon flow control; FIG. 12 is a flow diagram of a method for a feed injector control; FIGS. 13A and 13B illustrate a flow diagram for controlling a moderator in the gasification system; FIGS. 14A and 14B illustrate a flow chart for an air separation unit control (ASU) according to a characterization of the present invention; FIGS. 15A and 15B illustrate a flow chart for controlling oxygen head vent valves; FIG. 16 is a flowchart of a method for normal pressure control of a syngas head; FIGS. 17A and 17B illustrate a flow chart of a method for high pressure control of the syngas head; FIG. 18 is a flow chart of a method for low pressure control of a sygas head; FIG. 19 is a flow diagram of a method for gasification pressure control; FIG. 20 is a flow chart of a method for determining an automatic demand; and FIG. 21 illustrates a computer system capable of carrying out the functionality of the present invention.
DETAILED DESCRIPTION OF THE PREFERENTIAL CHARACTERIZATIONS FIG. 1 illustrates a gasification system 100 according to a characterization of the present invention. The gasification system 100 comprises an oxygen unit 104, a supply unit 108, a gasifier 112 and a sulfide remover. The oxygen unit 104 may be an air separation unit (ASU) that receives air from the atmosphere and produces oxygen. ASUs are sold with several manufacturers, such as Praxair and Air Products. The oxygen unit 104 is typically connected to the gasifier 112 via one or more oxygen lines 120. Alternatively, the gasification system 100 may be a plurality of gasifiers 11. In said arrangement, the plurality of gasifiers can be connected to an ASU via an oxygen head (a main line). Oxygen is distributed among the various gasifiers via the oxygen head. Oxygen lines 120 terminate in one or more oxygen injectors in gasifier 112. oxygen injectors inject oxygen into gasifier 112. Oxygen lines 120 also include one or more oxygen valves 124. Oxygen valves 124 they are adjusted to control the flow of oxygen to the gasifier 112. The supply unit 108 is connected to the gasifier 112 via one or more feed lines 128. The supply is supplied to the gasifier 112 via the power lines 128. The power lines 128 they terminate in one or more feed injectors in the gasifier 112 which injects the supply into the gasifier 112. The feed lines 120 also include one or more feed valves 132. If gaseous supplies are used, the feed valves 132 are adjusted to control the flow of gas supply in the gasifier 112. In
In contrast, when solid or liquid supplies are used, their flow is controlled by the speed of a variable speed loading pump. The gasification system 100 can be designed to process solids (eg, coal, petroleum coke, plastic, rubber), liquids (e.g., heavy oil, orimulsion, refinery by products) or gases (e.g., natural gas, gas). of Refinery Exhaustion). The gaseous feed stores are fed directly into the gasifier 112, where they are mixed with oxygen. Liquid feedstocks are usually pumped to gasifier 112. In contrast, solid feedstocks are generally milled into fine particles and mixed with water or waste oil to form a paste before being fed into gasifier 112. The paste then it is pumped into the gasifier 112 by a pulp pump and is fed to the gasifier 112 by means of feed injectors. The paste flowing in the gasifier 112 can also be controlled by adjusting the speed of the pulp pump. Moderators, such as steam and recycled black water, are added to the feed store and oxygen before gasification. The addition of moderators increases the efficiency of gasifier 112. Steam is typically supplied via steam lines. The black water is the water collected from the bottom of the gasifier, and is pumped back into the gasifier as a moderator. Referring again to FIG. 1, the supply and oxygen are then fed into the gasifier 112 through the feed injectors. The gasifier 112 is a refractory lined vessel that is designed to withstand high temperatures and high pressures. The gasifier 112 has no moving parts or any point of atmospheric release. In the gasifier 112, the supply and oxygen mixture, or the "feed mixture", is exposed to a temperature of
approximately 2500 degrees F and a pressure of approximately 1200 psi. Upon exposure to these extreme conditions, the feed mix is broken down into a gas mixture that has two main H2 and CO components. This gaseous mixture composed mainly of H2 and CO is known as the synthesis gas or "syngas". The syngas can be passed through a scourer of syngas where the syngas is conditioned. The syngas contains heat that can be used to generate steam. The gas mixture also includes small amounts of hydrogen sulfate (H2S), ammonia, methane, and other products derived from the feed mix. The gaseous mixture is then passed through a sulfide remover 116 where H2S is removed from the gas. The syngas is transported from the sulfide remover 116 by means of a syngas head 136. The syngas can be burned as fuel to generate energy. Alternatively, syngas is used to produce fertilizers, plastics and other chemicals. As described above, the critical control system is a part of a distributed control system that controls the operation of the gasification system 100. FIG. 2 is a block diagram of a distributed control system 200 that controls the operation of the gasification system 100. Referring now to FIG. 2, a distributed control network 204 forms the backbone of the distributed control system 200. One or more cathode ray tube (CRT) stations 208 are connected to the network 204. CRT 208 stations display the current state of the system of gasification 100. Operators monitor the operation of gasifier 112 and other components via CRT 208 stations.
An application station 212 connects to the network 204. Operators usually run monitoring applications, eg. Monitoring alarms, monitoring pumps, via application station 212. An integrated control system (ICS) 216 is connected to network 204. In a characterization, ICS 216 comprises a computer microprocessor and one or more access memories random (RAMs). The ICS 216 controls the operation of the gasifier 112 and other critical components of the gasification system 100. The RAM stores one or more programs specifically developed for the ICS 216. The computer microprocessor executes the programs stored in the RAMs. One or more input / output (I / O) cards are connected to the ICS 216. The I / O cards provide an interface between the microprocessor and various sensors, valves and pump motor speed controllers. One or more non-critical control systems 220 are also connected to the network 204. non-critical control systems 220 control the non-critical components of the gasification system 100. A communication passage 224 is connected to the network 204. The passage
224 allows the network 204 to communicate with third-party systems, for example, a security instrumentation system or an emergency shutdown system. FIG. 3 is a high-level block diagram of the ICS 216 according to a characterization of the present invention. Broadly, the ICS 216 comprises a carbon-oxygen (O / C) 304 radio control system, an ASU control system
308, a moderator control system 312, and a syngas head control system 316. Each of these systems is described in detail below.
1. Radio Control O / C
Described shortly, the optimal hydrocarbon conversion occurs when the O / C radius is controlled during gasification. Preferably, the O / C radius must be monitored continuously and controlled automatically. Without continuous O / C control, the O / C radius may become too high or too low. If the O / C radius becomes too high, the temperature inside the gasifier 112 varies greatly, which reduces the refractory life of the gasifier and the life of the thermocouple. On the other hand, if the O / C radius becomes too low, the hydrocarbon conversion drops, thereby reducing the efficiency of the gasifier 112. An O / C radius also increases to the amount of solids produced in the gasifier 112, which which causes the blackout of a gasifier if the solids are not removed quickly. The present invention provides an O / C radio control that improves the performance of the gasifier 112. Also, the present invention provides a safer operation and increase in the life of the component of the gasification system 100 by minimizing temperature variations in the gas. gasifier 112. If an ASU is integrated with a gasification system 100, the O / C control system must be coupled to the compressor controls O2 in the ASU for stable operation of the gasifier 112 and the compressor O2. Briefly described, according to the present invention, the O / C radius is determined by calculating the flow signal of oxygen and carbon. FIG. 4 is a flow diagram of a method for controlling the O / C radius according to a characterization of the present invention. In a step 404 a demand for syngas is determined based on load restrictions. The demand for syngas is the desired production of the gasifier 112. The actual calculation of the demand for syngas is explained in detail in FIG. 5. Load restrictions are limiting factors in the feed mix that limits the
performance of the gasifier 112. The load restriction calculation is also explained in greater detail in FIG. 6. In a step 408, an oxygen setpoint value is determined based on an O / C setpoint value and the demand for syngas. The calculation of the O / C setpoint value is described in detail later. In a step 412, a carbon setpoint value is determined based on the O / C setpoint value and the demand for syngas. In a step 416, the oxygen flow is controlled by adjusting the oxygen valves. Oxygen valves are adjusted based on the oxygen setpoint value. In a step 420, the coal flow is adjusted based on the carbon setpoint value. (a) Demand Control of Syngas FIG. 5 illustrates step 404 (calculating the demand for syngas) in greater detail. In a step 504, a carbon flux average is converted into a demand controller signal by a macro unit conversion. Alternatively, with an integrated ASU, an average oxygen flux is converted into a demand controller signal by a macro unit conversion to minimize fluctuations in the ASU. The demand controller signal is represented by a mass flow of pure coal in tons / day. The mass flow of pure coal is calculated from the following equation: m = (F) * (12.011) * (24/2000), where, m = mass flow of pure coal in tons / day, and F = flow of elemental paste in Ib-mol / hour. In a characterization, the average carbon flux (the flow of elemental paste) is measured by a magnetic meter or by a variable speed loading pump. In a step 508, the demand controller signal and a setpoint value of
demand controller are received in a proportional integral derivative controller (PID). The demand controller setpoint value is a desired value and is usually entered by an operator. The operation of the PID controller is well understood by persons skilled in the relevant art. The PID controller calculates an error signal that represents the difference between a signal and a setpoint value (or a reference signal), and multiplies the error signal by a gain. The production of the PID controller is a value between 0.0 and 1.0 (0% to 100%). In particular, the PID controller calculates the error signal representing the difference between the demand controller signal and the demand controller setpoint value, and multiplies the error signal by a gain. In a step 512, a signal selector receives the production of the PID controller and an automatic demand value. The determination of the automatic demand value is explained in detail later. Depending on the mode of operation of the gasifier 112, the signal selector selects either the production of the PID controller or the automatic demand value as the selected demand value. During a manual mode, the signal selector selects the production of the PID controller. During an automatic mode, the signal selector selects the automatic demand value. During an automatic override mode, the signal selector selects the larger of the two inputs. In a step 516, a low selector receives the selected demand value, which is, the production of the signal selector, and a value of the automation of demand automation of syngas. The determination of the automation value of syngas demand automation is described later. The low selector selects the lowest of the selected demand value and the demand automation bypass value of syngas as a load-restricted demand value. In a step 520, the demand value
Restricted cargo becomes a sign of bias. The bias signal has a value between -2% and + 2% of a full scale, where the full scale corresponds between 0 and a maximum permissible elementary flow, where the elementary flow refers to the flow in a molecule (1 molecule = 6.02 x 1023 molecules), instead of volumetric flow. Finally, in a step 524, the average oxygen flow is biased by a bias signal. The average biased oxygen flow is the demand signal for syngas. (i) Load Restrictions FIG. 6 is a flow chart of the method for determining load restrictions or the "syngas demand automation bypass value" according to a characterization of the present invention. In a step 604, a high selector selects the highest value among the following values: (1) a feed pump setpoint value; (2) a power PV / SP power pump, where PV / SP is the actual measured power at the maximum allowable power radius; (3) a PV / SP of oxygen compressor power; (4) a gasification oxygen valve position value (this value is only used if an integrated ASU is not used); (5) a compressor suction vent valve position value or an oxygen pump recycle valve position value (this value is used only if the integrated ASU is used); and (6) an oxygen compressor suction valve position value (this value is only used if an integrated ASU is used). The high selector produces the highest value as a restricted controller signal. In a step 608, a restricted controller setpoint value is multiplied by 98% (or 0.98) in a multiplier. Although 0.98 is the preferred factor, other factors (eg 0.95, 0.90) can also be used.
The restricted controller setpoint value is the desired value and is entered by the operator. In a step 612, a PID controller receives the restricted controller signal from the high selector and multiplier production (98% of the restricted controller setpoint value). The production of the PID controller is the value of the automation of demand automation of syngas. Setpoint Control O / C FIG. 7 is a flow diagram of the method for determining the O / C setpoint value according to a characterization of the present invention. In one step 704, the average oxygen flow is divided by the average carbon flux in a divisor to obtain the radius value of O / C. However, if solid or gaseous supplies are used, then the following steps must be performed in addition to step 704 described above.
In a step 708, the measured O / C setpoint value of step 704 is used to infer the temperature of the gasifier. The temperature of the inferred gasifier is the virtual temperature signal. In a step 712, the operator uses the virtual temperature signal to select a virtual temperature setpoint value. In a step 716, the O / C radio setpoint is interleaved from the virtual temperature setpoint. 3. Oxygen Setpoint Control FIG. 8 is a flow diagram of a method for calculating the oxygen setpoint value according to a characterization of the present invention. In step 804, the setpoint value is multiplied by the average carbon flux in a first multiplier. The production of the first multiplier is an average carbon flux in an oxygen base (or a high limit of oxygen setpoint). In a step 808, the syngas demand signal (biased oxygen flow average of step 524 in FIG.5)
and the first production of the multiplier is received in a low selector. The low selector produces an oxygen demand restricted by the average carbon flux. In a step 812, the production of the first multiplier, eg. the high limit of oxygen setpoint is received in a second multiplier, where it is subsequently multiplied by a factor of 0.98. The production of the second multiplier is a low limit of oxygen setpoint. Although the low oxygen setpoint limit is determined at 98% of the high oxygen setpoint limit, it must be understood that other factors (eg 95%, 90%) can also be used to determine the high oxygen setpoint limit. In a step 816, the low oxygen setpoint limit and the low selector production, that is, the oxygen demand restricted by the average carbon flux, are received in a high selector. The high selector produces a restricted oxygen setpoint value. Therefore, the average oxygen flow is restricted between 98% and 100% of the average carbon flux. In other words, the average carbon flow directs the average oxygen flow by no more than 2%. It will be apparent to those skilled in the art that the average oxygen flow can be restricted among other values of the average carbon flux. In other words, the average carbon flux may be allowed to direct the average oxygen flow by other percentage values.
If an ASU is integrated with the gasification system 100, then it will also be necessary to carry out the following steps. In a step 820, the equation F (x) = 0.002x + 0.81 is resolved, where F (x) > 1.0 and x represents the position of the oxygen valve. F (x) is an oxygen setpoint modifier that is used to push the oxygen valves to a fully open position, which is, out of control, when oxygen is controlled in the ASU.
The calculation of the oxygen valve position is described later. In a step 824, F (x) is multiplied by the production of the high selector, that is, the oxygen setpoint value restricted, to obtain the oxygen control setpoint value. 4. Carbon Setpoint Control In accordance with the present invention, the carbon setpoint value is calculated from a restricted carbon setpoint and the O / C radio setpoint. FIG. 9 is a flow diagram of a method for determining the carbon control setpoint value. In a step 904, the oxygen flow average and the demand for syngas is received in a high selector. The high selector produces a low limit of carbon setpoint in an oxygen base. In a step 908, the average oxygen flow is multiplied by 1.02 in a multiplier. The multiplier production is a high carbon setpoint limit. It should be understood that the average oxygen flow can be multiplied by other numbers, that is, 1.05, 1.1, to determine the high limit of the carbon setpoint. In a step 912, the high carbon setpoint limit and the low carbon setpoint limit are received at a select low. The low selector produces the restricted carbon setpoint. Finally, in a step 916, the restricted carbon setpoint is divided by the O / C radio setpoint and the carbon control setpoint value is obtained. 5. Oxygen Flow Control The average oxygen flow is controlled by adjusting the adjustment valve position in the oxygen lines. FIG. 10 is a flow chart for oxygen flow control. In a step 1004, the oxygen temperature, the oxygen pressure and the average oxygen flow are received in a flow compensator. The oxygen temperature is measured from the thermocouples in the oxygen lines. The oxygen pressure is measured by pressure transmitters in the oxygen lines. The average oxygen flow is measured by oxygen flow transmitters in the oxygen lines. He
Flow compensator corrects oxygen flow based on pressure and temperature variations. The compensated oxygen flow is calculated by the following equation:
q = q P ± PS. IR ^
where, q = oxygen flow compensated, q = oxygen flow, P = oxygen pressure in psig, P0 = absolute pressure conversion factor, preferably 14,696 psig, PR = absolute oxygen design pressure in psia, T = oxygen temperature in ° F, T0 = absolute temperature conversion factor, preferably 459.69 ° F, and TR = absolute oxygen design temperature, in ° R. The flow compensator produces a compensated oxygen flow. In a step 1008, the flow of compensated oxygen is converted into a flow of molar oxygen. The oxygen flow is converted into a molar oxygen stream by the following equation: F = q * (2 / 379.5) where, q = volumetric oxygen flow in standard cubic feet / hour (scsh), and F = oxygen flow elementary in 1 b-mol / hour.
In a step 1012, the molar oxygen flux is multiplied by the oxygen purity value in a multiplier. The oxygen purity value (eg, 96%) is obtained from an oxygen purity analyzer. The multiplier produces an oxygen flow signal. In a step 1016, the oxygen flow signal and an oxygen control setpoint value of the PID controller is received by two speed limiters, an increasing speed limiter and a decreasing speed limiter. The production of the PID controller is limited on average by one of the two speed limiters, depending on the average production change. If the production of the PID controller is increasing (ie, positive change rate), then it is limited on average by the increasing speed limiter. On the other hand, if the production of the PID controller is decreasing (ie, negative rate of change), then it is limited on average by the decreasing speed limiter. In a step 1024, the production of the two speed limiters is received in a signal selector, and the signal selector selects one of the signals based on whether the average change of the signal is positive or negative. If the production of the PID controller is increasing, the signal selector selects the increasing signal limiter. If the production of the PID controller is decreasing, the signal selector selects the decreasing speed limiter. The production of the signal selector is used to adjust the position of the oxygen valve. 6. Carbon Flow Control According to the present invention, the average carbon flux in the gasifier 112 is controlled by the carbon pump speed. Briefly stated, the carbon pump speed is controlled by the average measured carbon flux and a desired carbon control setpoint. A PID controller is used to adjust the speed of the coal pump.
FIG. 11 is a flow diagram of a method for carbon flow controls. In a step 1104, the average carbon flux is determined from the load pump speed. The average carbon flux is calculated by the following equation:
q = qr- (s / sr) where, q = change pump flow in gpm, qr = load pump design flow, s = load pump speed in rpm, and sr = pump design speed of load in rpm.
In a step 1108, a signal selector receives the average inferred coal flux and the average carbon flux measured. In a characterization, the measured average carbon flux is obtained from one meter of magnetic flux. The signal selector selects one of the signals depending on the operating condition. The signal selector produces the average real carbon flux. In a step 1112, the average carbon flux is converted into an average flux of molar coal in a molar converter. For solid supplies, the average carbon flux is converted into an average molar coal flow by the following equation:F = [. { (q * 8.021)} /. { 12.01 1 * (0.017-0.000056 * xpasta)} ] *). 01 xpasta) * (- 01Xcoque), Where, F = flow of elemental carbon at 1 b-mol / hour,
q = pulp flow (represents pulp pump speed), Xcoque = pulp coal concentration, between 85% and 92%, and Xpasta = paste coke concentration, between 55% and 65%.
When liquid supplies are used, the average carbon flux is converted to an average carbon flux by the following equation:
F = (q * Sg * 8.02 / 12.011) * .01 * xc Where, Q = coal flow in gal / min, F = elemental coal flow in 1 b-mol / hr, Sg = carbon of specific gravity, and Xc = carbon content of the liquid.
The molar conversion takes into account the limited carbon content of speed and the concentration of limited speed paste. The limited carbon content of speed and the concentration of limited speed pasta is explained below. First, the carbon content is determined from the supply shipment, eg, coke. The carbon content is then limited in speed or "limited in average" by a speed limiter. For example, if the carbon content of the current supply shipment differs significantly, eg, by 20%, from the carbon content of the previous shipment that was used in the gasifier, then the speed limiter limits the average change to , for example, .05% per minute. In other words, the speed limiter informs the coal flow controls that the carbon content is changing only by an average of, for example, .05% per
minute instead of a drastic change of 20%. The concentration of paste is determined by a laboratory analysis and is limited in average in the same way. In a step 1116, the average molar carbon flux is multiplied by the speed limited paste concentration in a first multiplier. In a step 1120, the first multiplier production is again multiplied by the limited carbon content of velocity in a second multiplier. The production of the second multiplier is a carbon flow signal. In a step 1124, a PID controller receives the carbon flow signal and the carbon control setpoint value and produces the carbon pump speed. The PID controller output is usually limited in average by a speed limiter to protect the coal pump. 7. Oxygen Control of Feeding Injector As noted previously, oxygen is supplied by the ASU to the gasifier.
In a characterization of the present invention, an oxygen line is divided into two lines before being fed to gasifier 112. The two oxygen lines and one carbon line (of the supply unit) are joined to form three concentric pipes in a feeding injector. The central pipeline supplies oxygen. The intermediate pipe that surrounds the central pipeline supplies supplies. The external pipe that surrounds the intermediate pipe supplies oxygen. Oxygen is controlled by two valves. A central oxygen valve located before the division, which is upwards, and an annular oxygen valve located in the concentric section, which is, downwards, of the pipe. FIG. 12 is a flow diagram for power injector controls. In a step 1204, an annular oxygen dividing valve is determined. The annular oxygen division value is given by F (x) = 1-x, where x is the division setpoint value of
oxygen. The oxygen division setpoint value is the percentage (ie, 30%) of the total oxygen that is flowing in the center line. If x = 30%, then F (x) = 1 - 0.3 = 0.7. In a step 1208, the oxygen division setpoint value is multiplied by the compensated oxygen flow signal in a first multiplier. The first multiplier produces the oxygen setpoint value. In a step 1212, the annular oxygen division signal is multiplied by the compensated oxygen flow signal in a second multiplier and an annular oxygen setpoint value is obtained. In a step 1216, the oxygen division signal is subtracted from the oxygen flow signal to obtain the annular oxygen flow signal. The oxygen flow signal is measured by transmitters in the oxygen line. In a step 1220, the annular oxygen flow signal and the annular oxygen setpoint is received in a PID controller. The PID controller produces an annular oxygen valve position. In a step 1224, the oxygen flow signal and the oxygen setpoint value is received in a PID controller that produces a central oxygen valve position. 8. Moderator Controls As described above, in a gasification process, the moderators are added to the oxygen and the supplies before they are fed to the gasifier 112. In the present invention, the steam is added to the oxygen and supply. Optionally, black water can be added to the supply. Black water is water collected from the bottom of the gasifier that is then added to the coal as a moderator. Typically, the black water that is collected from the gasifier is pumped back as a moderator by a pump. The amount of moderators in oxygen and coal is controlled by adjusting the oxygen line steam valve and the carbon line steam valve. If the water
Recycled black is also used as a moderator, the amount of black water is controlled by adjusting the speed of a recycled black water pump. FIGS. 13A and 13B illustrate a flow diagram for controlling the moderator in the gasifier 112. In a step 1304, the average oxygen line vapor flow, the vapor temperature and the vapor pressure are received in a first flow compensator . The average steam flow of the oxygen line is measured by one meter of flow in the steam line. The steam temperature is measured by one or more thermocouples in the steam line. The vapor pressure is measured by one or more pressure transmitters in the steam line. The flow compensator produces an oxygen line vapor flow signal that is compensated for vapor pressure and vapor temperature. The compensated vapor flow signal is calculated by the following equation:
PR T + T0 where, q = vapor flow compensated, q = vapor flow, P = vapor pressure in psig, P0 = absolute pressure conversion, usually 14.696 psig, PR = absolute vapor design pressure in psia, T = steam temperature in ° F, T0 = absolute temperature conversion, usually 459.69 ° F, and TR = absolute steam design temperature, in ° R
In a step 1308, the average carbon line vapor flow, the vapor pressure and the vapor temperature are received in a second flow compensator, and the flow compensator produces a carbon line steam flow signal compensated. In a step 1312, the compensated oxygen line steam flow signal and the compensated carbon line vapor flow signal are added in a first adder and a total steam flow signal is generated. In a step 1316, the total steam flow is added to the average recycled black water flow and the average moderator flow is determined. In a characterization, the average black water flow is measured by a magnetic meter in a carbon line. In a step 1320, the average total moderator flow is divided by the average carbon flux in a first divider, and a moderator / carbon radius is generated. In a step 1324, the moderator / carbon radius, the average carbon flux and the moderately / carbon radio setpoint value is received in a first radio controller. The radio controller produces an average desired oxygen line vapor by comparing the moderate / carbon radio signal and the moderator / carbon radio setpoint value. A radio controller typically follows a desired radius when a component of a radius varies while another component of the radius remains fixed until the desired radius is achieved. The following example illustrates the operation of a radio controller. Suppose a desired radius is 2/3 or .666. Now consider that a radio controller receives a radius x / y. The radio controller will vary and while x remains fixed until x / y = .666. Alternatively, the radio controller can vary x while and remains fixed. In a step 1328, the desired oxygen line vapor average can be replaced by a predetermined value in a setpoint automation override of
security system. In a step 1332, the oxygen line vapor flux signal and the production of the safety system setpoint automation bypass are received in a first PID controller. The first PID controller produces the oxygen line steam valve signal that is used to adjust the oxygen line steam valves. In a step 1336, the compensated carbon line vapor flow signal and a coal line steam flow setpoint are received in a second PID controller. The PID controller produces a carbon line steam valve signal that is used to adjust the coal line steam valves. In a 1340 step, the average coal flow is divided by the average black water flow recycled into a second divider. In a step 1344, a second radio controller generates a black water controller setpoint value of the splitter output. In a step 1348, a third PID controller receives the recycled black water flow average and the black water controller setpoint value, ie the production of the second radio controller. The third PID controller produces a recycled black water pump speed signal that is used to control the speed of the recycled black water pump. 9. ASU / Oxygen Controls The present invention provides ASU / Oxygen Controls where an ASU is integrated with the gasification system 100. The oxygen discharge of the ASU is controlled by adjusting an oxygen compressor inlet valve. FIGS. 14A and 14B illustrate a flowchart for the ASU / Oxygen Controls according to a characterization of the present invention. In a step 1404, the position of the oxygen valve of the gasifier 112 and other gasifiers that can operate simultaneously are compared in a high selector. In one step
1408, the following equation is solved: F (x) = 0.002x + 0.08, where F (x) > 0.99, and x is the production of the high selector. F (x) is an oxygen setpoint modifier that is used to restrict oxygen in the ASU to cause the oxygen valves of the downstream gasifier to open to the point where they release oxygen control to the ASU. In a step 1412, the following equation is solved; F (y) = 0.002y + 0.08, where
F (y) > 1.0 yy is the oxygen valve position of the gasifier 112. F (y) is an oxygen setpoint modifier used to counteract the oxygen setpoint modifier F (x) of step 820. In a step 1416, the setpoint value of real oxygen is divided by F (y) into a divisor. The actual oxygen setpoint value is calculated by the operator and entered into the system. In a step 1420, the production of the divider and other similar productions of other gasifiers are added in the first adder. In a step 1424, the production of the first adder is multiplied by a multiplier by F (x) obtained in step 1408. The multiplier yields a setpoint value of the discharge controller. The discharge controller setpoint value represents the combined total oxygen setpoint value, which is, the ASU discharge. In a step 1428, the average oxygen flow of all the gasifiers is added in a second adder and the average total oxygen flow is calculated. In a step 1432, a PID controller receives the discharge controller setpoint and the total oxygen value setpoint. The PID controller produces a discharge controller production signal. In a step 1436, the production of the PID controller is speed limited in a speed limiter. In a step 1440, the speed limited discharge controller production signal is received in a low selector together with the outputs of other ASU controllers (eg, compressor suction flow controller, the suction ventilation controller of ASU) and controllers
compressor protection. The low selector output is the oxygen compressor inlet valve signal. 10. Oxygen Head Vent Valve Controls In the gasification system 100, a common line, known as the "oxygen head", is used to distribute oxygen between gasifying stations. During an emergency condition, the oxygen in the head is vented through head valves. The amount of oxygen ventilated through the head ventilation valves is controlled by adjusting the head ventilation valves. FIGS. 15A and 15B illustrate a flow chart for controlling the oxygen head vent valves. In a step 1504, an oxygen head pressure signal is multiplied by 1.02 in a multiplier. In a step 1508, the production of the multiplier is the limited speed in a speed limiter. The production of the speed limiter is the value of the oxygen head control setpoint. In a step 1512, a predicted oxygen flow is calculated from the oxygen pressure, the oxygen temperature, the oxygen valve position, the average oxygen line vapor flow and the syngas scouring pressure. The oxygen pressure is measured by one or more pressure transmitters in the oxygen line. The oxygen temperature is measured by one or more thermocouples in an oxygen line. The calculation of average steam line flow of oxygen was described above. The scouring pressure of syngas is measured by a pressure transmitter in a syngas scrubber. The predicted oxygen flow can be calculated by treating the oxygen valve of the gasifier and the feed injector of the gasifier as two restrictions in series.
The flow through a restriction is a function of the up and down pressures and the size of the constraints. The downward pressure for the injector
feeding is the syngas gas scrubbing pressure. The upstream pressure for the feed injector can not be measured directly. So instead of this, it is inferred from the steam flow up the oxygen line of the feed injector. The inferred pressure also serves as downward pressure for the oxygen valve restriction. As the oxygen valve opens and closes, the value of its restriction changes. Multiple iterative equations should be used to determine the impact of oxygen valves when they are above or below their designated normal position.
In a characterization, the predicted oxygen flow is calculated by the equation provided below. However, it must be understood that several other types of equations can be easily used to compute the predicted oxygen flow. An expert in the art can easily substitute alternative equations to compute the predicted oxygen flow.
r - P bajoi (a)
When Z < Z, and by: 2 P = P low 2 -2 Z2 + Duck 2 Z2 - 1 (b)
When Z > Z > Z, and by: 2 > - > bass (c)
When Z < Z, where: ° OTlSnP + ° n
under ~ "scourer **" PFI .oxygen .. ()
(and)
Y;
P = the preset feed inlet inlet pressure, in psig,
P = = pressurized injector pressure input of low oxygen flow controller production, in psig, Z = production of oxygen flow controller, in%, Z = NOC production of oxygen flow controller , in% Paito = the injector inlet pressure of production of high oxygen flow controller, in psig, P-fistmcsls: the scouring pressure of syngas, in psig,? PF? = the NOC differential pressure of the feed injector, in psi, Pfflagejja- "the oxygen pressure, in psig,
J_ £ 2Ua £ 0-- the NOC pressure of absolute oxygen, in psia, PfiSltQEajo. : NOC scouring pressure of absolute syngas, in psia,? PF1 = the NOC differential pressure of the oxygen valve, in psi.
The predicted oxygen pressure is restricted by: oxygen - 10 > P < P, scourer + 10, where; 'oxygen the oxygen pressure, in psig, P = the inlet pressure of the predicted feed injector, in psig, and
3estropajo = the scouring pressure syngas, in psig.
The predicted oxygen flow is calculated by:
(9)
When Z < Z, and by: Q = qn, (h)
when Z > Z, where;
(')
Y:
G)
Y:
q = the predicted oxygen flow, in scfh, Z = the production of oxygen flow controller, in%, z = the NOC production of oxygen flow controller, in%, qFv = the oxygen valve flow predicted, in scfh aa = the oxygen flow of the predicted feed injector, in scfh, qp / = the NOC flow of oxygen valve predicted, in scfh, PF1 to the NOC differential pressure of the feed injector, in psi,
Poxigeno = the oxygen pressure, in psig, P = the preset feed inlet inlet pressure, at least 0.3
'oxygenated in pSlg,? PFV = the NOC differential pressure of oxygen valve, in psi, T = the NOC absolute oxygen temperature, in ° R, T = the oxygen temperature, in ° F, the absolute temperature conversion, usually 459.69 ° F, Poxigeno = the NOC pressure of absolute oxygen, in psia, Po_ = the absolute pressure conversion, usually 14.69psi, qF1 = the NOC flow of the feed injector, in scfh, Pgsjrofiaja = the scouring pressure of syngas, of at least 0.3 P , in psig,? P £ 1 = the NOC differential pressure of the feed injector, in psi, P = the absolute predicted feed inlet NOC in psia, m = the vapor mass flow compensated, in " 7b, and T vaporizes the NOC absolute vapor temperature, in ° R.
In a step 1516, the predicted oxygen flow is added for predicted oxygen flows from other gasifier trains in an adder. In a step 1520, the total predicted oxygen flow is subtracted from the design oxygen head flow value and a predicted oxygen head ventilation flow is obtained. The design oxygen flow head value is a constant, which represents the amount of oxygen that the oxygen pipes are designed to carry. In a step 1524, an oxygen head ventilation valve bias value is calculated from the predicted oxygen head ventilation flow and a critical flow of oxygen valve.p.
oxygen head ventilation. The oxygen head ventilation valve bias calculation is described in the Texaco Design Document. The critical flow of oxygen head vent valve is the maximum allowable flow through the vent valve. In a step 1528, a PID controller receives the value of the oxygen head control setpoint and the oxygen head pressure signal. The PID controller produces an impartial oxygen head vent valve signal. Finally, in a step 1532, the production of the PID controller is vised by the oxygen head valve bias value and a biased oxygen head vent valve signal is obtained. The oxygen head vent valve signal is used to adjust the vent valves of the oxygen head. 11. Syngas Head Pressure Control As described above, the syngas is transported from the gasifier by one or more syngas heads. In general, the operator enters a normal pressure control setpoint, also called the syngas head pressure setpoint. The syngas head pressure setpoint is then used for high pressure control, low pressure control and "low low" pressure control. FIG. 16 is a flow diagram of a method for determining the normal pressure control of the syngas head. In a step 1604, the syngas head pressure signal is measured by one or more pressure transmitters in the syngas head. In a step 1608, a PID controller receives the syngas head pressure setpoint and the syngas head pressure signal. The PID controller produces a setpoint value of boiler syngas. The boiler refers to a boiler down the gasifier, which takes the syngas and burns the syngas to generate energy. The setpoint value of boiler syngas represents the number of syngas that the boiler should consume.
The present invention provides for high pressure control in the head of syngas. FIGS. 17A and 17illustrate a flow diagram for a high pressure control of the syngas head. In a step 1704, the average spindle flow of syngas, the head temperature of syngas and the head pressure signal of syngas are received in a flow compensator. The flow compensator calculates a compensated syngas head flow. In a step 1708, a biased vent valve bias of syngas head is calculated from the compensated syngas head flow, the syngas head temperature and the maximum allowable flow through the syngas head valve. The enlarged vent valve of the syngas head is calculated by the following equation:
? Z = q 'PR - I ± IQ - 100, qR P + Po TR
where,
? Z = biased syngas pressure controller production bias, in%, q = predicted balanced syngas flow, in scfh, qR = design flow of syngas, in scfh, PR = design pressure of absolute clean syngas, in psia, P = clean syngas pressure, in psig, Po = absolute pressure conversion, usually 14.696psi, t = clean syngas temperature, in ° F, T0 = absolute temperature conversion, usually 459.69 ° F, and
TR = design temperature of absolute clean syngas, in ° R.
In a step 1712, the biased vent valve bias of syngas head and a combustion turbine trip signal are received in a bias ramp. In a step 1716, the production of the bias ramp is added to other combustion turbine trip signals of other turbines in the adder. In a step 1724, the syngas head pressure setpoint is multiplied by 1.02 in a multiplier. The production of the multiplier is the high pressure setpoint. In a step 1720, the syngas head pressure signal and the high pressure setpoint are received in the PID controller. The PID controller produces when the syngas head pressure increases by more than 2% of the high pressure setpoint. In one step 1728, the production of the PID controller is biased by the production of the adder and the expanded fan valve position of the syngas head is obtained. - FIG 18 is a flow chart of the method for a low pressure control of the syngas head. In a step 1804, a gasifier travel signal and a ramp start signal are received on a bias ramp. The ramp start signal is input by the operator. In a step 1808, the syngas head pressure setpoint is multiplied by 0.98 in a multiplier and in a low pressure setpoint. In other words, the low pressure setpoint is determined at 98% of the syngas head pressure setpoint. In a step 1812, a PID controller receives the syngas head pressure signal and the low pressure setpoint and produces an unbiased low syngas pressure signal. In a step 1816, the unbiased low syngas pressure signal is biased by producing the bias ramp to obtain the low syngas pressure signal.
FIG. 19 is a flowchart of a method for a gasification pressure control. In a step 1904, a gasifier travel signal and a ramp start signal is received on a bias ramp. The travel signal of the gasifier occurs when there is a blackout of a gasifier. The ramp start signal is a constant value. The bias ramp generates a bias signal that will be used to download the syngas inventory from the gasifier in the syngas header. In a step 1908, the high pressure setpoint value is multiplied by 0.98 in a multiplier. In a step 1916, the production of the multiplier is partialized by the production of the bias ramp, that is, the bias signal, and the normal pressure setpoint value is obtained. In a step 1912, a first PID controller receives a scouring pressure at a high pressure setpoint. The scouring pressure is measured by the pressure transmitters on the top of the syngas pad. The first PID controller produces a widened valve position. In a 1920 position, a second PID controller receives the scrub pressure and the normal pressure setpoint and generates a syngas decrease valve controller signal. The automatic demand value noted above is derived from the carbon pump speed and the low syngas pressure signal. FIG. 20 is a flow chart of a method for determining automatic demand. In a step 2004, the differential velocity of two coal pumps (of two gasifier trains) is calculated. The difference represents a differential predicted train. In a 2008 step, a PID controller receives the differential predicted stream and a setpoint value of zero (0). The production of the PID controller is between 0 and 100%. In a 2012 step, the production of the PID controller becomes a bias value. In a characterization, the production of the PID controller becomes a value between -10 and +10. In a 2016 step, the low syngas pressure signal is partialized
by means of the bias value and the automatic demand is generated. In a step 2020, the bias value is multiplied by -1 and the other gasification stream is provided as an automatic demand.
12. Implementation of the ICS in a Computer System In a characterization of the present invention, the ICS 216 is implemented by a computer system capable of carrying out the functionality of the ICS 216 described above, and is shown with more detail in FIG. 21. A computer system 2100 includes one or more processors, such as a processor 2104. The processor 2104 is connected to a communication bus 2108. Several software characterizations are described in terms of this exemplary computer system. After reading this description, it will be apparent to the person skilled in the relevant art how to implement the invention using other computer systems and / or computer architectures. The computer system 2100 also includes a main memory 2112, preferably a random access memory (RAM), and may also include a secondary memory 2116. The secondary memory may include, for example, a hard disk drive 2120 and / or a removable storage unit 2124, representing a floppy disk unit, a magnetic tape unit, an optical disk unit, etc. The removable storage unit 2124 reads and / or writes to a removable storage unit 2132 in a well-known manner. The removable storage unit 2132 represents a floppy disk, a magnetic tape drive, an optical disk drive, etc. which are read and written on a removable storage unit 2124. As will be appreciated, the storage unit
Removable 2132 includes a usable computer storage medium that is stored in this software and / or computer data. In alternative characterizations, the secondary memory 2116 may include other similar means for allowing computer programs or other instructions to be loaded into the computer system 2100. Such means may include, for example, a removable storage unit 2134 and an interface 2128. Examples of this can be included in a cartridge and cartridge interface (such as that found in video game devices), a removable memory chip (such as an EPROM or PROM) and associated socket, and other storage units removable 2134 and interfaces 2128 that allow software and data to be transferred from a removable storage unit 2134 to the 2100 computer system. The 2100 computer system may also include a 2136 communications interface. The 2136 communications interface allows the software and data to be transferred between the computer system and external devices. Examples of the 2100 communications interface may include a modem, a network interface (such as an Ethernet card), a communications port, a slot and PCMCIA and card, etc. The software and data transferred via the communications interface 2136 are in the form of signals 2140 that can be electronic, electromagnetic, optical or other signals capable of being received by the communication interface 2136. The signals 2144 carry the signals 2140 and can be implemented by using cables or cable, fiber optic, telephone line, a cell phone connection, an RF connection and other communication channels. In this document, the terms "computer program medium" and "usable computer medium" are used to generally refer to the media as the removable storage unit 2124, a hard disk installed in the disk drive
hard 2120, and signals 2140. These computer program products are means for providing software to the 2100 computer system. Computer programs (also called computer control logic) are stored in main memory 2112 and / or memory secondary 2116. Computer programs may also be received via communications interface 2136. Such computer programs, when executed, allow computer system 2100 to perform the features of the present invention as discussed herein. In particular, computer programs, when executed, allow the processor 2104 to perform the features of the present invention. In a characterization where the invention is implemented using software, the software can be stored in a computer program product and loaded into a 2100 computer system using the removable storage unit 2124, the hard disk drive 2120 or the communications interface 2136. The control logic (software), when executed by the processor 2104, causes the processor to perform the functions of the invention as described herein. In another characterization, the invention can be implemented primarily in the use of hardware, for example, hardware components such as application-specific integrated circuits (ASICs). The implementation of said hardware state machine to perform the functions described in this document will be apparent to those skilled in the relevant art. Also in another characterization, the invention is implemented by using a combination of both hardware and software. While several characterizations of the present invention have been described above, it should be understood that these were presented by way of example
only, and not as a limitation. Therefore, the breadth and vision of the present invention should not be limited by any of the exemplary characterizations described above, but should be defined only in accordance with the following claims and their equivalents.
Claims (5)
- CHAPTER CLAIMING Having described the invention, it is considered as a novelty and, therefore, the content is claimed in the following: CLAIMS 1. A method to control a carbon dioxide (O / C) radius in a gasification plant by converting the supply of oxygen and hydrocarbon into syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the method comprising the steps of: determining a demand for syngas based on load restrictions, the demand for syngas represents a desired production of a gasifier, determination of oxygen and carbon setpoint values based on a setpoint value of oxygen radius to carbon (O / C) and the demand for syngas, and adjustment of the oxygen and carbon valves in the gasification plant based on oxygen and carbon setpoint values, respectively. The method for controlling a carbon oxygen (O / C) radius as recited in claim 1 comprises the steps of: converting a carbon flux average into a demand controller signal by a macro unit conversion; demand controller signal reception and a demand controller setpoint value in a PID controller and generation of a PID controller signal; reception of the PID controller signal and an automatic demand value in a signal selector and generation of a selected demand value; reception of the selected demand value and a value of automation cancellation of demand of syngas in a low selector and generation d a demand value of restricted load; conversion of the value of restricted demand of load to a value of partiality, and partiality of an average of oxygen flow with the value of partiality. 3. The method as recited in claim 2, wherein the average carbon flux is converted into syngas demand signal by the following equation: m = (F) * (12.011) * (24/2000), Where, m represents the demand for syngas and F is a flow of pasta at 1 b-mol / hour. The method as recited in claim 2, wherein the calculation of the value of the automation of demand automation of syngas comprises the steps of: determining a restricted controller signal in a high selector; 98% calculation of a restricted controller setpoint value; and determination of the syngas demand automation override value of 98% of the restricted controller setpoint value and the restricted controller signal. 5. A method to control a carbon dioxide (O / C) radius in a gasification plant by converting the supply of oxygen and hydrocarbon into syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the method comprises the steps of : multiplication of an oxygen setpoint value by an average carbon flow to generate a high oxygen setpoint limit; determination of an oxygen demand restricted by an average carbon flow in a low selector from a demand for syngas and the high oxygen setpoint limit; multiplication of the high limit of oxygen setpoint by a predetermined factor to generate a low limit of oxygen setpoint, and determination of a setpoint value of oxygen restricted in a high selector from a low limit of oxygen setpoint and the demand of oxygen restricted by the average carbon flux. 6. The method as recited in claim 5, wherein the predetermined factor is, 98. 7. A method to control a carbon dioxide (O / C) radius in a gasification plant by converting the supply of oxygen and hydrocarbon into syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the method comprises the steps of : determination of a low limit of carbon setpoint in a high selector based on an average oxygen flow and syngas demand; multiplication of I average oxygen flow by a predetermined factor to generate a high limit of carbon setpoint; determination of a restricted carbon setpoint value in a low selector from the high limit of the coal setpoint and the low limit of the coal setpoint; Y division of the carbon setpoint restricted by an O / C radio setpoint to generate the carbon control setpoint value. 8. The method as recited in claim 7, wherein the predetermined factor is 1.02. 9. A method to control an oxygen flow in a gasification plant converting the supply of oxygen and hydrocarbon in syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the method includes the steps of: Calculation of an oxygen flow compensated from an average oxygen flow and oxygen temperature in a flow compensator; Conversion of the compensated oxygen flow in a molar oxygen flow in a molar converter; Multiplication of the molar oxygen flow by a value of oxygen purity to generate an oxygen flow signal; Receiving the oxygen flow signal and an oxygen control setpoint value in a PID controller and generating a PID controller production signal; Speed limiting the production signal of PID controller in a speed limiter; and Adjustment of an oxygen valve using the limited PID controller speed production signal. 10. The method as recited in claim 9, wherein the compensated oxygen flow is calculated by the following equation: PR T + T0 where, q = compensated vapor flow, q = vapor flow, P = vapor pressure in psig, P0 = absolute pressure conversion, usually 14.696 psig, PR = absolute vapor design pressure in psia, T = steam temperature in ° F, T0 = absolute temperature conversion, usually 459.69 ° F, and TR = absolute steam design temperature, in ° R 11. The method as recited in claim 9, wherein the flow of compensated oxygen is converted to molar oxygen flow by the following equation: F = q * (2 / 379.5) Where, q = volumetric oxygen flow in standard cubic feet / hour (scsh), and F = elemental oxygen flow in 1 b-mol / hour. 12. A method to control a coal flow in a gasification plant by converting the supply of oxygen and hydrocarbon into syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the method comprises the steps of: calculating a flow average of coal from a charge pump speed; selection of a real carbon flux average from an average inferred coal flux and an average carbon flux measured in a signal selector; conversion of the average carbon flux to an average flow of molar coal in a molar converter; generation of a carbon flow signal from an average molar coal flow, a limited speed paste concentration and a limited speed carbon content; generation of a carbon pump speed signal in a PID controller using the carbon flow signal and a carbon control setpoint value; and adjusting the speed of a carbon pump by the carbon pump speed signal. 13. The method as recited in claim 12, wherein the average carbon flux is calculated by the following equation: q = qr- (s sr) where, q = change pump flow in gpm, qr = load pump design flow, s = load pump speed in rpm, and sr = load pump design speed in rpm. 14. The method as recited in claim 12, wherein the average carbon flux is converted into average molar carbon flux by the following equation: F = [. { (q * 8.021)} /. { 12.01 1 * (0.017-0.000056 * xpasta)} ] *). 01 xpasta) * (. 01Xcoque), Where, F = flow of elemental carbon at 1 b-mol / hour, q = flow of paste (represents pulp pump speed), Xcoque = carbon concentration of paste, and Xpasta = paste coke concentration. 15. The method as recited in claim 12, wherein the average carbon flux is converted into average molar carbon flux by the following equation: F = (q * Sg * 8.02 / 12.011) * .01 Where, Q = coal flow in gal / min, F = flow of elemental carbon in 1 b-mol / hr, Sg = carbon of specific gravity, and Xc = carbon content of the liquid. 16. A method to control moderators in a gasification plant by converting the supply of oxygen and hydrocarbon into syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the method comprises the steps of: generating a steam flow signal from oxygen line compensated in a first flow compensator from an average steam line flow of oxygen, a vapor temperature and a vapor pressure; generation of a vapor line signal of carbon offset line in a second flow compensator from an average steam line flow of coal, vapor pressure and vapor temperature; addition of compensated oxygen line steam flow signal and compensated carbon line steam flow signal in a first adder to generate a total steam flow signal: determination of a total moderator flow from a signal of total steam flow and a recycled black water flow; division of the total moderator flow by the coal flow in a prime divider to determine a moderator / carbon radius; determination of a desired oxygen line vapor average from a moderator / carbon radio signal and a moderator / carbon setpoint value in a radio controller; determination of an oxygen line vapor valve signal from the desired oxygen line vapor average and the oxygen line vapor flow signal; adjustment of a coal line steam valve by the oxygen line steam valve signal; determination of a coal line steam valve signal from the compensated carbon line steam flow signal and a coal line steam flow setpoint value; and adjustment of a coal line steam valve by the coal line steam valve signal. 17. The method as recited in claim 16, wherein the vapor flow of compensated oxygen line is calculated by the following equation: PR T + T0 where, q = compensated vapor flow, q = vapor flow, P = vapor pressure in psig, P0 = absolute pressure conversion, usually 14.696 psig, PR = absolute vapor design pressure in psia, T = steam temperature in ° F, T0 = absolute temperature conversion, usually 459.69 ° F, and TR = absolute steam design temperature, in ° R 18. The method as recited in claim 16, wherein the vapor flow of compensated coal line is calculated by the following equation: PR T + T0 where, q = compensated vapor flow, q = vapor flow, P = vapor pressure in psig, P0 = absolute pressure conversion, usually 14.696 psig, PR = absolute vapor design pressure in psia, T = steam temperature in ° F, To = absolute temperature conversion, usually 459.69 ° F, and TR = absolute steam design temperature, in ° R 19. A method to control an air separation unit (ASU) that provides oxygen to a gasification plant by converting the supply of oxygen and hydrocarbon into syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the method comprises the steps from: comparison of the oxygen valve positions of a plurality of gasifiers that are operating simultaneously in a high selector, and that produce a value x; calculation of F (x) = 0.002x + 0.08, where F (x) > 0.99, and x is the production of the high selector; and calculation of F (x) = 0.002y + 0.81, where F (y) > 1.0, and y is the oxygen valve position of a selected gasifier. 20. The method as recited in claim 19, further comprising the steps of: dividing an actual oxygen setpoint value by F (y) into a divider; addition of the production of the divider and other divider productions of other gasifiers in a first adder: multiplication of the production of the first adder by F (x) in a first multiplier and generation of a discharge controller setpoint value, the value of download controller setpoint representing the download of the ASU; and addition of oxygen flow averages of all gasifiers in a second adder and generation of an average total oxygen flow. 21. The method as recited in claim 20, further comprising the steps of: . reception of the discharge controller setpoint and the total oxygen value setpoint in a PID controller, and production of a discharge controller production signal; speed limitation of discharge controller production signal; and reception of the production signal of limited speed discharge controller in a low selector together with the productions of one or more compressor suction flow controllers, one or more ASU suction ventilation controllers and one or more controllers of compressor protection, and production of an oxygen compressor inlet valve signal. 22. A method to control high pressure of a syngas head in a gasification plant, the syngas head transporting the syngas of a gasifier, the gasification plant converting the supply of oxygen and hydrocarbon into syngas composed mainly of hydrogen (H2) and monoxide of carbon (CO), the method comprises the steps of: receiving a syngas head flow average, a syngas head temperature signal and a syngas head pressure signal, and calculating a head flow compensated syngas; and calculation of a widened fan valve bias of syngas head from a compensated syngas head flow, the syngas head temperature, and a maximum allowable flow through a syngas head valve. 23. The method as recited in claim 22, wherein the biased vent valve bias of syngas head is calculated by the following equation: where, ? Z = high production bias of syngas pressure controller clean of automation override, in%, q = syngas flow compensated predicted, in scfh, qR = design flow of syngas, ¡n scfh, PR = design pressure of absolute clean syngas, in psia, P = clean syngas pressure, in psig, P0 = absolute pressure conversion, T = clean syngas temperature, in ° F, T0 = absolute temperature conversion, and TR = design temperature of Absolute clean syngas, in ° R. 24. The method as recited in claim 22, further comprising the steps of: reception of the partiality of flared ventilation valve of syngas head and a trip signal of combustion turbine in a bias ramp, and production of a bias ramp signal; adding the bias ramp signal for the combustion turbine trip signals of other turbines in an adder, and producing a total bias signal; and multiplication of a setpoint value of syngas head pressure by 1.02 in a multiplier, and generation of a high pressure setpoint. 25. The method as recited in claim 24, further comprising the steps of: reception of a syngas head pressure signal and high pressure setpoint in a PID controller, and production of PID controller production signal; and partiality of the PID controller production signal with the bias signal d} total and generation of a valve position and expanded ventilation of the syngas head. 26. A program storage device readable by a machine, tangentially characterizing a program of instructions executable by the machine to perform the steps of the control method of a carbon oxygen (O / C) radius in a gasification plant, the gasification plant turning the Supply of oxygen and hydrocarbon in syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the steps of the method include: determination of a demand for syngas based on load restrictions, demand for syngas represents a desired production of A gasifier determines oxygen and carbon setpoint values based on a set oxygen value of carbon to oxygen (O / C) and the demand for syngas, and adjustment of the oxygen and carbon valves in the gasification plant based on Oxygen and carbon setpoint values, respectively. 27. The program storage device as recited in claim 26 further performs the steps of: converting a carbon flux average into a demand controller signal by a macro unit conversion; demand controller signal reception and a demand controller setpoint value in a PID controller and generation of a PID controller signal; reception of the PID controller signal and an automatic demand value in a signal selector and generation of a selected demand value; reception of the selected demand value and a value of automation cancellation of demand of syngas in a low selector and generation d a demand value of restricted load; conversion of the value of restricted demand of load to a value of partiality, and partiality of an average of oxygen flow with the value of partiality. 28. The program storage device as recited in claim 26, wherein the average carbon flux is converted into syngas demand signal by the following equation: m = (F) * (12.011) * (24/2000) , Where, m represents the demand for syngas and F is a flow of paste at 1 b-mol / hour. 29. The program storage device as recited in claim 26, wherein the calculation of the demand automation bypass value of syngas comprises the steps of: determining a restricted controller signal in a high selector; 98% calculation of a restricted controller setpoint value; and determination of the syngas demand automation override value of 98% of the restricted controller setpoint value and the restricted controller signal. 30. A program storage device readable by a machine, tangentially characterizing a program of instructions executable by the machine to perform the steps of the method of determining an oxygen setpoint value in a gasification plant, the gasification plant converting the Oxygen and hydrocarbon supply in syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the steps of the method include: multiplication of an oxygen setpoint value by an average carbon flow to generate a high limit of oxygen setpoint; determination of an oxygen demand restricted by an average carbon flow in a low selector from a demand for syngas and the high oxygen setpoint limit; multiplication of the high limit of oxygen setpoint by a predetermined factor to generate a low limit of oxygen setpoint, and determination of a setpoint value of oxygen restricted in a high selector from a low limit of oxygen setpoint and the demand of oxygen restricted by the average carbon flux. 31. The program storage device as recited in claim 30, wherein the predetermined factor is, 98. 32. A program storage device readable by a machine, tangentially characterizing a program of instructions executable by the machine to perform the steps of the method of controlling an oxygen flow in a gasification plant, the gasification plant converting the supply of oxygen and hydrocarbon in syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the steps of the method include: Calculation of a flow of oxygen compensated from an average flow of oxygen and oxygen temperature in a compensator flow; Conversion of the compensated oxygen flow in a molar oxygen flow in a molar converter; Multiplication of the molar oxygen flow by a value of oxygen purity to generate an oxygen flow signal; Receiving the oxygen flow signal and an oxygen control setpoint value in a PID controller and generating a PID controller production signal; Speed limiting the production signal of PID controller in a speed limiter; and Adjustment of an oxygen valve using the limited PID speed controller production signal. 35. The program storage device as recited in claim 34, wherein the compensated oxygen flow is calculated by the following equation: PR T + T0 where, q = vapor flow compensated, q = vapor flow, P = vapor pressure in psig, P0 = absolute pressure conversion, PR = absolute vapor design pressure in psia, T = vapor temperature in ° F, To = absolute temperature conversion, and TR = absolute steam design temperature, in ° R 36. The program storage device as recited in claim 34, wherein the flow of compensated oxygen is converted to a flow of molar oxygen by the following equation: F = q * (2 / 379.5) Where, q = volumetric oxygen flow in standard cubic feet / hour (scsh), and F = elemental oxygen flow in 1 b-mol / hour. 37. A program storage device readable by a machine, tangentially characterizing a program of instructions executable by the machine to perform the steps of the control method of a coal flow in a gasification plant, the gasification plant converting the supply of oxygen and hydrocarbon in syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the steps of the method include: calculation of a coal flow average from a charge pump speed; selection of a real carbon flux average from an average inferred coal flux and an average carbon flux measured in a signal selector; conversion of the average carbon flux to an average flow of molar coal in a molar converter; generation of a carbon flow signal from an average molar coal flow, a limited speed paste concentration and a limited speed carbon content; generation of a carbon pump speed signal in a PID controller using the carbon flow signal and a carbon control setpoint value; and adjusting the speed of a carbon pump by the carbon pump speed signal. 38. The program storage device as recited in claim 37, wherein the average carbon flux is calculated by the following equation: q = qr. (s / sr) where, q = change pump flow in gpm, qr = load pump design flow, s = load pump speed in rpm, and sr = load pump design speed in rpm. 39. The program storage device as recited in claim 37, wherein the average carbon flux is converted into average molar carbon flux by the following equation: F = [. { (q * 8.021)} /. { 12,011 * (0.017-0.000056 * xpasta)} ] *). 01 xpasta) * (. 01x8que), Where, F = flow of elemental carbon at 1 b-mol / hour, q = flow of paste (represents the speed of pulp pump), Xcoque = concentration of carbon from paste, and Xpasta = paste coke concentration. 40. The program storage device as recited in claim 38, wherein the average carbon flux is converted to average carbon flux by the following equation: F = (q * Sg * 8.02 / 12.011) * .01 * Xc: Where, Q = coal flow in gal / min, F = elemental coal flow in 1 b-mol / hr, Sg = specific gravity coal, and Xc = carbon content of the liquid. 41. A program storage device readable by a machine, tangentially characterizing a program of instructions executable by the machine to perform the steps of the moderator control method in a gasification plant, the gasification plant converting the supply of oxygen and hydrocarbon In syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the steps of the method include: generation of a compensated oxygen line steam flow signal in a first flow compensator from an average steam line flow of I oxygen, a vapor temperature and a vapor pressure; generation of a vapor line signal of carbon offset line in a second flow compensator from an average steam line flow of coal, vapor pressure and vapor temperature; addition of compensated oxygen line steam flow signal and compensated carbon line steam flow signal in a first adder to generate a total steam flow signal: determination of a total moderator flow from a signal of total steam flow and a recycled black water flow; division of the total moderator flow by the coal flow in a prime divider to determine a moderator / carbon radius; determination of a desired oxygen line vapor average from a moderator / carbon radio signal and a moderator / carbon setpoint value in a radio controller; determination of an oxygen line vapor valve signal from the desired oxygen line vapor average and the oxygen line vapor flow signal; adjustment of a coal line steam valve by the oxygen line steam valve signal; determination of a coal line steam valve signal from the compensated carbon line steam flow signal and a coal line steam flow setpoint value; Y adjustment of a coal line steam valve by the coal line steam valve signal. 42. The program storage device as recited in claim 41, wherein the vapor flow of compensated oxygen line is calculated by the following equation: PR T + T0 where, q = compensated vapor flow, q = vapor flow, P = vapor pressure in psig, P0 = absolute pressure conversion, usually 14.696 psig, PR = absolute vapor design pressure in psia, T = steam temperature in ° F, T0 = absolute temperature conversion, usually 459.69 ° F, and TR = absolute steam design temperature, in ° R 43. The program storage device as recited in claim 41, wherein the vapor flow of compensated carbon line is calculated by the following equation: q = q P + Pg. Tg_, PR T + T0 where, q = compensated vapor flow, q = vapor flow, P = vapor pressure in psig, P0 = absolute pressure conversion, usually 14.696 psig, PR = absolute vapor design pressure in psia , T = steam temperature in ° F, To = absolute temperature conversion, usually 459.69 ° F, and TR = absolute steam design temperature, in ° R 44. A program storage device readable by a machine, tangentially characterizing a program of instructions executable by the machine to perform the steps of the method of control of an air separation unit (ASU) that provides oxygen to a gasification plant, The gasification plant converting the supply of oxygen and hydrocarbon into syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the steps of the method comprising: comparing the oxygen valve positions of a plurality of gasifiers that are operating simultaneously in a high selector, and that produces a value x; calculation of F (x) = 0.002x + 0.08, where F (x) > 0.99, and x is the production of the high selector; Y calculation of F (x) = 0.002y + 0.81, where F (y) > 1.0, y y is the oxygen valve position of a selected gasifier. 45. The program storage device as recited in claim 44, further comprising the steps of: dividing an actual oxygen setpoint value by F (y) in a divisor; addition of divider output and other splitter outputs from other gasifiers in a first adder: multiplication of first adder output by F (x) in a first multiplier and generation of a discharge controller setpoint value, the value of download controller setpoint representing the download of the ASU; and addition of oxygen flow averages of all gasifiers in a second adder and generation of an average total oxygen flow. 46. The program storage device as recited in claim 44, further comprising the steps of: receiving the discharge controller setpoint and the total oxygen value setpoint in a PID controller, and producing a controller production signal download speed limitation of discharge controller production signal; and receipt of production signal from limited speed discharge controller in a low selector along with the productions of one or more compressor suction flow controllers, one or more ASU suction ventilation controllers and one or more compressor protection controllers, and production of an oxygen compressor inlet valve signal. 47. A program storage device readable by a machine, tangentially characterizing a program of instructions executable by the machine to perform the steps of the high pressure control method of a syngas head in a gasification plant, the head of syngas transports syngas of a gasifier, the gasification plant converting the supply of oxygen and hydrocarbon in syngas composed mainly of hydrogen (H2) and carbon monoxide (CO), the steps of the method include: reception of an average head flow of syngas , a syngas head temperature signal and a syngas head pressure signal, and calculation of a compensated syngas head flow; and calculation of a widened fan valve bias of syngas head from a compensated syngas head flow, the syngas head temperature, and a maximum allowable flow through a syngas head valve. 48. The program storage device as recited in claim 47, wherein the biased fan valve bias of syngas head is calculated by the following equation: qR P + Po TR where, ? Z = high production bias of syngas pressure controller clean of automation override, in%, q = predicted balanced syngas flow, in scfh, qR = design flow of syngas, in scfh, PR = design pressure of absolute clean syngas, in psia, P = clean syngas pressure, in psig, Po = absolute pressure conversion, T = clean syngas temperature, in ° F, To = absolute temperature conversion, and TR = syngas design temperature absolute clean, in ° R. 49. The program storage device as recited in claim 47, which further performs the steps of: reception of the partiality of flared ventilation valve of syngas head and a trip signal of combustion turbine in a bias ramp, and production of a bias ramp signal; addition of the bias ramp signal for the combustion turbine trip signals of other turbines in an adder, and production of a total bias signal; Y multiplication of a setpoint value of syngas head pressure by 1.02 in a multiplier, and generation of a high pressure setpoint. 50. The program storage device as recited in claim 49, further comprising the steps of: reception of a syngas head pressure signal and high pressure setpoint in a PID controller, and production of PID controller production signal; and partiality of the PID controller production signal with the bias signal d} total and generation of a widened ventilation valve position of syngas head.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US09154772 | 1998-09-17 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| MXPA01002956A true MXPA01002956A (en) | 2001-12-04 |
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